CN115709555A - Production process of crosslinked polyethylene PE-Xa (polyethylene-Xa) pipe and high-speed raw material mixer - Google Patents
Production process of crosslinked polyethylene PE-Xa (polyethylene-Xa) pipe and high-speed raw material mixer Download PDFInfo
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Abstract
The application discloses a production process of a crosslinked polyethylene PEX-A pipe, which belongs to the field of production of crosslinked polyethylene pipes and is used for pipe production, and the production process comprises the steps of mixing high-density polyethylene resin, pentaerythrityl tetrakis [ beta- (3,5-di-tert-butyl-4-hydroxyphenyl) propionate ] and tris (2,4-di-tert-butyl) phosphite in a high-speed mixer, metering powder, then feeding the mixture into a double-screw extruder to obtain a melt I, continuously mixing the melt I and di-tert-butyl peroxide fed by a liquid metering pump in the double-screw extruder to obtain a melt II, feeding the melt II into the single-screw extruder from the double-screw extruder, mixing and building pressure to obtain a melt III, and feeding the melt III out of a stamping type extruder die for cooling and forming to obtain the crosslinked polyethylene pipe. According to the method, the uniformity of the crosslinking degree of the pipe is improved by optimizing the production process of the PEX-A and the composition and proportion of the raw material formula, the ageing resistance of the pipe can be greatly improved, and the pipe can be endowed with excellent chlorine resistance and oxidation resistance.
Description
Technical Field
The invention belongs to the field of production of crosslinked polyethylene pipes, and particularly relates to a production process of a crosslinked polyethylene PE-Xa pipe and a raw material high-speed mixer.
Background
In the field of cold and hot water transportation and floor heating in life, a cross-linked polyethylene pipe is widely used, and the cross-linked polyethylene pipe has the characteristics of excellent hydraulic pressure resistance and excellent high-temperature resistance. In the production process of the cross-linked polyethylene pipe, peroxide cross-linking (PE-Xa) and silane cross-linking (PE-Xb) are mainly adopted, for example, chinese patent publication No. CN103275274A discloses a method for producing a silane cross-linked polyethylene hot water hose by a one-step method of a single screw extruder, and specifically discloses that raw materials are added into the single screw extruder, grafting reaction and mixing of all components are completed after a melting section and a homogenizing section, then extrusion molding is carried out by a nose grinding, the grafted polyethylene pipe is obtained after the extruded pipe is subjected to vacuum sizing, cooling, traction and curling, and the grafted polyethylene pipe is cross-linked in hot water, so that the silane cross-linked polyethylene hot water hose is obtained. The similar scheme can also refer to a special cross-linked polyethylene for pipes and a preparation process thereof disclosed in Chinese patent publication No. CN 110294884A.
The process can complete crosslinking by means of water vapor, and the difficulty of water molecules entering the inside of the pipe is increased along with the increase of the wall thickness of the pipe, so that the problem of uneven crosslinking degree on the surface and inside of the pipe is solved. In order to overcome the problems, the prior industry mostly adopts an Engel production process to prepare a PE-Xa pipe and extrudes and molds the PE-Xa pipe through a stamping plunger type extruder.
However, PE-Xa pipes extruded by a ram extruder have the problem of uneven dispersion of the antioxidant and the crosslinking agent. Taking the antioxidant as an example, the small antioxidant particles with higher melting point are usually embedded in the pipe wall in the form of independent particles after being melted, and referring to fig. 1, the small antioxidant particles cannot play the role of antioxidation, and the pipe can be cracked due to the defects. Therefore, pipe production enterprises mostly adopt antioxidants with lower melting points and smaller particle sizes, but the production efficiency of the PE-Xa pipe is reduced, and the difficulty of improving the ageing resistance of the pipe is increased.
Disclosure of Invention
The invention aims to provide a production process of a cross-linked polyethylene PE-Xa pipe and a raw material high-speed mixer, which improve the uniformity of the cross-linking degree of the pipe by optimizing the production process of the PE-Xa and the formula composition and proportion of the raw materials, greatly improve the anti-aging performance of the pipe and endow the pipe with excellent chlorine resistance and oxidation resistance.
In order to achieve the purpose, the invention is realized by the following technical scheme:
the application discloses a production process of a cross-linked polyethylene PE-Xa pipe, which comprises the following steps:
1) The health-care food is prepared from the following raw materials in parts by weight: 100 parts of high-density polyethylene resin, 0.2 to 1 part of di-tert-butyl peroxide, 0.2 to 0.6 part of tetra [ beta- (3,5-di-tert-butyl-4-hydroxyphenyl) propionic acid ] pentaerythritol ester and 0.1 to 0.3 part of tri (2,4-di-tert-butyl) phosphite;
2) Mixing high-density polyethylene resin, tetra [ beta- (3,5-di-tert-butyl-4-hydroxyphenyl) propionic acid ] pentaerythritol ester and tri (2,4-di-tert-butyl) phosphite in a high-speed mixer for 5 to 10 minutes, weighing powder, feeding the powder into a main feeding port of a double-screw extruder, and plasticizing and uniformly mixing the powder in the double-screw extruder to form a melt compound I;
3) Feeding 0.2 to 1 part of di-tert-butyl peroxide into a double-screw extruder through a liquid metering pump, and uniformly mixing the di-tert-butyl peroxide and the fusant I in the double-screw extruder to obtain a fusant II;
4) Feeding the molten compound II into a single-screw extruder from a double-screw extruder, and further mixing and pressurizing in the single-screw extruder to obtain a molten compound III;
5) Feeding the melt III from the tail end of the single-screw extruder to a ram extruder die, and forming and crosslinking the melt III in the ram extruder die.
6) And cooling and shaping the pipe in the stamping type extruder die to obtain the cross-linked polyethylene PE-Xa pipe.
Preferably, as one of the technical solutions of the present application, the extrusion temperature of the twin-screw extruder in the step 2) is controlled to be 135 ℃ to 150 ℃, and the screw rotation speed is controlled to be 100rpm to 150rpm.
Preferably, as one of the technical schemes, the basic temperature of the single-screw extruder in the step 4) is 140-150 ℃, and the screw rotating speed is 10rpm-40rpm.
Preferably, as one of the technical schemes, the length of the stamping type extruder die is 0.5m to 2m, and the temperature is 220 ℃ to 240 ℃.
The raw material high-speed mixer applied to the production process of the cross-linked polyethylene PEX-A pipe comprises a mixing tank body, wherein the mixing tank body comprises a mixing feeding port communicated with the interior of the mixing tank body, and the mixing feeding port is positioned at the top of the mixing tank body; a stirring shaft is arranged in the mixing tank body, the central axis of the stirring shaft is superposed with the central axis of the mixing tank body, and the stirring shaft is driven by a stirring driver positioned at the top of the mixing tank body; the stirring shaft is connected with an inner stirring rod through an inner connecting rod, an outer stirring rod is arranged between the inner stirring rod and the inner wall of the mixing tank body, and the outer stirring rod is connected with the stirring shaft through an outer connecting rod; the outer stirring rods and the inner stirring rods are alternately arranged and uniformly distributed around the central axis of the stirring shaft; the mixing material inlet is connected with the primary dispersing tank body, the primary dispersing tank body is provided with a screen drum driving shaft which is coaxial with the primary dispersing tank body, the screen drum driving shaft is fixedly connected with a dispersing screen drum at the position positioned in the primary dispersing tank body, and the outer wall of the dispersing screen drum is provided with a plurality of through holes; the dispersing screen cylinder is positioned below the inlet of the primary dispersing tank body, and a distance enough for passing materials is reserved between the outer wall of the dispersing screen cylinder and the inner wall of the primary dispersing tank body; the inlet of the primary dispersion tank body is connected with a feeding pipe, a feeding auger is arranged inside the feeding pipe, the feeding auger is driven by a feeding auger driver, and the feeding auger driver is positioned at the single-material feeding port of the feeding pipe.
Preferably, as one of the technical solutions of the present application, the bottom of the mixing tank body is a conical discharge end coaxially arranged with the mixing tank body, the mixing discharge port is located at the bottom end of the conical discharge end and is communicated with the interior of the conical discharge end, a spiral stirring blade is fixedly connected to a position where the stirring shaft extends into the conical discharge end, and when the spiral stirring blade extends along the stirring shaft to a position where the mixing tank body is connected with the conical discharge end, the radius of the spiral stirring blade is gradually increased; the outer stirring rod is provided with a vertical section and an inclined section which are arranged in parallel with the inner wall of the mixing tank body and the inner wall of the conical discharge end, and an obtuse angle structure is formed at the connecting position of the vertical section and the inclined section; and a plurality of inclined stirring rods are arranged on the inner stirring rod and the outer stirring rod.
Preferably, as one of the technical scheme of this application, be provided with the blending tank strengthening rib on the outer wall of blending tank body and toper discharge end, the blending tank strengthening rib is around the central axis equipartition of the blending tank body.
Preferably, as one of the technical solutions of the present application, the primary dispersing tank includes a reducing section and a straight cylinder section which are fixed as a whole, the dispersing screen cylinder has a flaring feeding section located in the reducing section, the flaring feeding section is fixed as a whole with the screening cylinder section located in the straight cylinder section, and the connecting position of the flaring feeding section and the screening cylinder section adopts smooth transition; and the screening cylinder section is fixedly connected with the bottom end of the screening cylinder driving shaft through a bottom connecting end.
Preferably, as one of the technical solutions of the present application, the bottom connection end has a triangular cross section, and has an inclined guide surface inclined toward the through hole of the dispersion screen drum.
Compared with the prior art, the invention has the beneficial effects that:
1. according to the invention, high-density polyethylene resin, tetra- [ beta- (3,5-di-tert-butyl-4-hydroxyphenyl) propionic acid ] pentaerythritol ester and tri- (2,4-di-tert-butyl) phosphite in different weight parts are firstly mixed with di-tert-butyl peroxide to form a melt I, then the melt I is mixed with the di-tert-butyl peroxide to form a melt II, the melt II is extruded by a single screw extruder to form a melt III, and the melt III is molded and crosslinked by a stamping type extruder die to form the crosslinked polyethylene PE-Xa (polyethylene) pipe.
2. The invention can effectively make powder additives such as antioxidant and the like more effective and play the role of the antioxidant to a greater extent, so that the powder additives can be completely plasticized and uniformly dispersed in the high-density polyethylene resin in the production process of the PE-Xa pipe.
3. The production speed of the crosslinked polyethylene PE-Xa pipe can be effectively increased by the method, so that the production speed of the crosslinked polyethylene PE-Xa pipe can reach 5-10m/min.
4. The high-speed mixer can improve the mixing efficiency and mixing quality of raw materials, is beneficial to improving the production quality and production speed of the cross-linked polyethylene PE-Xa pipe by matching with the process, and realizes the improvement of the initial distribution efficiency of materials in the mixing tank body by adopting the structures of the feeding pipe and the primary dispersing tank body, which contain the feeding auger, so that the subsequent materials can be stirred and mixed in the mixing tank body conveniently, and the flexibility of the stirring device can be improved.
Drawings
FIG. 1 is an image of small antioxidant particles produced in the form of individual particles embedded in the tube wall.
Fig. 2 is a schematic view of the invention in its entirety and in its installed position.
Fig. 3 is a schematic diagram of the overall structure of the present invention.
Fig. 4 is a schematic diagram of the overall structure of the present invention.
FIG. 5 is a schematic view of the construction of the mixing tank of the present invention.
FIG. 6 is a first schematic view of the structure of the feeding tube and the primary dispersion tank according to the present invention.
FIG. 7 is a second schematic view of the structure of the feeding tube and the primary dispersion tank of the present invention.
FIG. 8 is a schematic view of the internal structure of the feed tube and the primary dispersion tank of the present invention.
FIG. 9 is a schematic view of the positions of the inner stirring rod and the inclined stirring rod of the present invention.
In the figure: 1. a single material inlet; 2. a feeding auger driver; 3. a floor slab; 4. a feeding pipe; 5. a primary dispersion drive; 6. a primary dispersion tank; 7. a mixing feed port; 8. a mixing tank body; 9. a mixing tank reinforcing rib; 10. a conical discharge end; 11. a mixed material outlet; 12. a stirring driver; 13. a stirring shaft; 14. an inner link; 15. an outer link; 16. an inner stirring rod; 17. an outer stirring rod; 18. a diagonal stir bar; 19. feeding a packing auger; 20. a dispersion screen drum; 21. a screen drum drive shaft; 22. a helical mixing blade; 23. a screen drum reinforcing rib; 61. a reducing section; 62. a straight cylinder section; 171. a vertical section; 172. an inclined section; 201. a flaring feeding section; 202. screening the cylinder section; 203. the bottom is connected with the end.
Detailed Description
The technical solution of the present invention will be further described and illustrated with reference to the following examples.
Example 1
The cross-linked polyethylene PE-Xa pipe is produced by the following components, by weight, 100 parts of high-density polyethylene resin, 0.2 part of di-tert-butyl peroxide, 0.2 part of tetra [ beta- (3,5-di-tert-butyl-4-hydroxyphenyl) propionic acid ] pentaerythritol ester and 0.1 part of tris (2,4-di-tert-butyl) phosphite. 100 parts of high-density polyethylene resin, 0.2 part of tetra [ beta- (3,5-di-tert-butyl-4-hydroxyphenyl) propionic acid ] pentaerythritol ester and 0.1 part of tri (2,4-di-tert-butyl) phosphite ester in the raw materials are fed into a high-speed mixer to be mixed for 5 minutes, the mixture is weighed through powder and then fed into a main feeding port of a double-screw extruder, the plasticization and uniform mixing are completed in the double-screw extruder to form a melt I, the extrusion temperature of the double-screw extruder is controlled at 140 ℃, and the rotating speed of the double-screw extruder is 100rpm.
The 0.2 part of di-tert-butyl peroxide is fed into a twin-screw extruder by means of a liquid metering pump and mixed homogeneously with melt II in the twin-screw extruder and melt II is formed.
And (3) sending the uniformly mixed melt II from the double-screw extruder to a single-screw extruder, further mixing and building pressure in the single-screw extruder to form a melt III, wherein the extrusion temperature of the single-screw extruder is 140 ℃, the rotating speed of the single-screw extruder is 10rpm, and the head pressure of the single-screw extruder is 25MPa.
And (3) delivering the molten material III from the single-screw extruder to a mould to complete the forming and crosslinking of the crosslinked polyethylene PE-Xa pipe, wherein the length of the mould is 0.5m, and the temperature of the mould is 220 ℃.
And (4) sending out the die, and cooling and shaping to obtain the cross-linked polyethylene PE-Xa pipe. The drawing speed of the pipe is 6m/min.
Example 2
The production process of the crosslinked polyethylene PE-Xa pipe comprises the following components, by weight, 100 parts of high-density polyethylene resin, 0.7 part of di-tert-butyl peroxide, 0.25 part of pentaerythritol tetrakis [ beta- (3,5-di-tert-butyl-4-hydroxyphenyl) propionate ] and 0.2 part of tris (2,4-di-tert-butylphenyl) phosphite, wherein 100 parts of the high-density polyethylene resin, 0.25 part of pentaerythritol tetrakis [ beta- (3,5-di-tert-butyl-4-hydroxyphenyl) propionate ] and 0.2 part of tris (2,4-di-tert-butylphenyl) phosphite are fed into a high-speed mixer for mixing for 7 minutes, and are weighed by powder and fed into a main feeding port of the twin-screw extruder, so that the materials are plasticized and uniformly mixed in the twin-screw extruder to form a melt body I, the extrusion temperature of the twin-screw extruder is controlled to be 150 ℃, and the rotation speed of the extruder is controlled to be 120rpm.
The 0.7 part of di-tert-butyl peroxide is fed into the twin-screw extruder by means of a liquid metering pump and mixed homogeneously with melt II in the twin-screw extruder and melt II is formed.
And (3) delivering the uniformly mixed melt II from the double-screw extruder to a single-screw extruder, further mixing and building pressure in the single-screw extruder to form a melt III, wherein the extrusion temperature of the single-screw extruder is 150 ℃, and the rotating speed of the single-screw extruder is 20rpm.
And (3) delivering the melt III from the single-screw extruder to a mould to complete the forming and crosslinking of the crosslinked polyethylene PE-Xa pipe, wherein the length of the mould is 1m, the temperature of the mould is 230 ℃, and the head pressure of the single-screw extruder is 28MPa.
And (4) sending out the die, and cooling and shaping to obtain the cross-linked polyethylene PE-Xa pipe. The drawing speed of the pipe is 7.5m/min.
Example 3
The cross-linked polyethylene PE-Xa pipe is prepared from the following components, by weight, 100 parts of high-density polyethylene resin, 1 part of di-tert-butyl peroxide, 0.6 part of tetra [ beta- (3,5-di-tert-butyl-4-hydroxyphenyl) propionic acid ] pentaerythritol ester and 0.3 part of tris (2,4-di-tert-butylphenyl) phosphite. 100 parts of high-density polyethylene resin, 0.6 part of tetra [ beta- (3,5-di-tert-butyl-4-hydroxyphenyl) propionic acid ] pentaerythritol ester and 0.3 part of tri (2,4-di-tert-butyl) phosphite in the raw materials are fed into a high-speed mixer for mixing for 7 minutes, the mixture is weighed by powder and then fed into a main feeding port of a double-screw extruder, plasticizing and uniform mixing are completed in the double-screw extruder to form a melt I, the extrusion temperature of the double-screw extruder is controlled at 140 ℃, and the rotating speed of the double-screw extruder is 120rpm.
Feeding the 1 part of di-tert-butyl peroxide into a twin-screw extruder by a liquid metering pump, and uniformly mixing the di-tert-butyl peroxide and the melt II in the twin-screw extruder to form the melt II.
And (3) delivering the uniformly mixed melt II from the double-screw extruder to a single-screw extruder, further mixing and building pressure in the single-screw extruder to form a melt III, wherein the extrusion temperature of the single-screw extruder is 150 ℃, and the rotating speed of the single-screw extruder is 30rpm.
And (3) delivering the melt III from the single-screw extruder to a mould to complete the forming and crosslinking of the crosslinked polyethylene PE-Xa pipe, wherein the length of the mould is 1.5m, the temperature of the mould is 230 ℃, and the head pressure of the single-screw extruder is 30 MPa.
And (3) sending out the die, cooling and shaping to obtain the cross-linked polyethylene PE-Xa pipe, wherein the traction speed of the pipe is 8m/min.
Example 4
The formula and the process of the production process of the crosslinked polyethylene PE-Xa pipe are similar to those of the production process in the embodiment 3, and the difference is that
The rotating speed of the single screw is 40rpm, the head pressure of the single screw extruder is 33MPa, and the traction speed of the pipe is 9m/min.
Example 5
The production process of the cross-linked polyethylene PE-Xa pipe is similar to that in embodiment 4 in formula and process, except that the single-screw extruder has a head pressure of 35MPa, a die length of 1.8 m, and a pipe drawing speed of 8.5m/min.
On the basis of the above examples, with reference to example 3, comparative example 1 was set up, and the formulation used in comparative document 1 was made up in the same manner as in example 3, and was prepared as follows: mixing high-density polyethylene resin, di-tert-butyl peroxide, tetra [ beta- (3,5-di-tert-butyl-4-hydroxyphenyl) propionic acid ] pentaerythritol ester and tri (2,4-di-tert-butyl phenyl) phosphite in a high-speed mixer for 5 minutes, feeding into a punching type extruder, and finishing pipe extrusion in the extruder. The temperature of the extruder is 220 ℃, and the pipe drawing speed is 1m/s.
The pipes obtained in examples 1 to 3 of the present invention and comparative example 1 were tested according to the test methods of the national standards GB/T18474, GB/T19466 and GB/T6111, and the test results are shown in the following table:
as can be seen from the data in the table, the indexes such as the crosslinking degree and the like of the embodiment of the invention are superior to those of the comparative example, and the oxidation induction time of the comparative example 1 adopting the stamping test extruder is obviously reduced, and the oxidation resistance is greatly reduced. This is because the antioxidant and the crosslinking agent are not uniformly dispersed due to the absence of mixing and shearing action of the punch, and thus the antioxidant performance of the material cannot be effectively improved.
Meanwhile, the rotating speed and the die length of the single-screw extruder have great influence on the performance of the pipe. The rotating speed of the single screw is increased, so that the extrusion speed of the pipe can be obviously increased, but the retention time of the pipe in a mould can be reduced, the cross-linking degree of the pipe can be reduced, and the oxidation induction time can be prolonged; the length of the die is increased, the residence time of the pipe in the die is increased, the degree of crosslinking of the pipe is increased, the oxidation induction time is reduced, and the burst pressure is obviously increased.
As shown in fig. 2 to 9, the invention discloses a high-speed raw material mixer, which comprises a feeding pipe 4, wherein the inlet end and the outlet end of the feeding pipe 4 are both arranged vertical to the horizontal plane, an inclined pipe which is arranged obliquely relative to the horizontal plane is connected between the inlet end and the outlet end of the feeding pipe 4, a feeding auger 19 is arranged in the inclined pipe, and shaft bodies at two ends of the feeding auger 19 respectively penetrate through the inlet end and the outlet end and then extend out. The bearing with a sealing structure is arranged at the position where the shaft body of the feeding auger 19 is connected with the inlet end and the outlet end, the bearing can be positioned in a bearing sleeve, and the bearing sleeve is fixedly connected on the feeding pipe 4 at the inlet end and the outlet end.
In the invention, the feeding auger 19 is driven by the feeding auger driver 2, and the feeding auger driver 2 is a driving motor with a speed reducing mechanism. The feeding auger driver 2 can be arranged on the floor slab 3, the feeding pipe 4 penetrates through the floor slab 3 and then extends out, and the feeding pipe 4 and the floor slab 3 can be hoisted by adopting an auxiliary part at the connecting position of the feeding pipe 4 and the floor slab 3, so that the feeding auger driver can be realized by technical personnel in the field under the prior art.
The outlet of the feeding pipe 4 is connected to the inlet end of the primary dispersion tank body 6, and the inlet end of the primary dispersion tank body 6 is located on the cover body of the primary dispersion tank body 6 and is uniformly distributed around the central axis of the primary dispersion tank body 6. As shown in fig. 6 to 8, the primary dispersion tank 6 is a hollow cylindrical tank body with an open bottom, and includes a reduced diameter section 61 and a straight cylindrical section 62, the reduced diameter section 61 and the straight cylindrical section 62 are integrated, the maximum inner diameter of the reduced diameter section 61 is greater than the inner diameter of the straight cylindrical section 62, the minimum inner diameter of the reduced diameter section 61 is the same as the inner diameter of the straight cylindrical section 62, and a cover body with an inlet end is disposed at the opening at the top end of the reduced diameter section 61.
A screen drum driving shaft 21 is further arranged at the central axis of the primary dispersing tank body 6, the screen drum driving shaft 21 is driven by the primary dispersing driver 5 after extending out of the cover body of the primary dispersing tank 6, and the primary dispersing driver 5 is a driving motor with a speed reducing mechanism. The screen drum driving shaft 21 is fixedly connected with a dispersing screen drum 20 in the inner area of the primary dispersing tank body 6, and a plurality of through holes are distributed on the outer wall of the dispersing screen drum 20 and form screen holes of the dispersing screen drum 20. The dispersing screen drum 20 is constructed as shown in fig. 7 and includes a flared feed section 201, and the flared feed section 201 is located in the reduced diameter section 61 and can be arranged parallel to the inner wall of the reduced diameter section 61 at that location. The flaring feeding section 201 and the screening cylinder section 202 are fixed into a whole, and the connection position of the flaring feeding section 201 and the screening cylinder section 202 adopts smooth transition. The bottom end of the screening cylinder section 202 is provided with a closing structure and is plugged through a bottom connecting end 203, and the bottom connecting end 203 and the screening cylinder driving shaft 21 are fixed into a whole. The cross-section of the screen drum driving shaft 21 in the present invention is triangular, and it has an oblique guide surface inclined in the direction of the through-hole in the dispersion screen drum. Meanwhile, the outer wall of the dispersion screen drum 20 of the invention is also provided with a screen drum reinforcing rib 23 which is integrated with the dispersion screen drum and is coaxially arranged with the dispersion screen drum.
The outlet of the primary dispersion tank 6 is connected to the mixed material inlet 7 through a flange structure, and the mixed material inlet 7 is distributed on the cover body at the top of the mixing tank body 8. The structure of the mixing tank body 8 is shown in fig. 5, and the mixing tank body 8 comprises a cylindrical tank body, a conical discharge end 10 integrated with the mixing tank body is connected to the bottom of the mixing tank body 8, a mixed discharge hole 11 is formed in the bottom end of the conical discharge end 10, a plurality of mixing tank reinforcing ribs 9 are fixedly connected to the outer walls of the mixing tank body 8 and the conical discharge end 10, the mixing tank reinforcing ribs 9 play a role in supporting and strengthening the strength of the mixing tank body and the conical discharge end, and meanwhile, the mixing tank body 8 and the conical discharge end 10 can be connected with a support through bolts and the like to achieve connection of the mixing tank body 8 and the conical discharge end 10 with a base, and enough discharge distance is reserved between the mixed discharge hole 11 and the base.
In the invention, a stirring shaft 13 is arranged at the central axis of the mixing tank 8, the stirring shaft 13 is driven by a stirring driver 12 positioned on the cover body of the mixing tank 8, and the stirring driver 12 drives the stirring shaft 13 to rotate in the mixing tank 8. The stirring shaft 13 extends downwards into the conical discharge end 10, and the spiral stirring blade 22 is fixedly connected to a position in the conical discharge end 10, and the spiral stirring blade 22 has a radius which is enlarged along with the inner wall of the conical discharge end 10, so that the spiral stirring blade 22 has a relatively consistent distance with the inner wall of the conical discharge end 10 in the height direction of the conical discharge end 10.
Connecting rod 14, outer connecting rod 15 in the position department fixedly connected with of (mixing) shaft 13 in the blending tank body 8, interior connecting rod 14 and interior puddler 16 fixed connection, outer connecting rod 15 and outer puddler 17 fixed connection, it has a plurality of stirring down tube 18 to equally divide cloth on interior puddler 16 and the outer puddler 17, leaves between the tip of stirring down tube 18 and the inner wall of blending tank body 8 and supplies stirring pivoted surplus.
As shown in fig. 9, the inclined stirring rod 18 is inclined away from the rotating direction, and the included angle α is an acute angle. The stirring diagonal rods 18 can effectively increase the stirring and dispersing effects of the materials at the edges.
In the invention, the outer stirring rods 17 and the inner stirring rods 16 are alternately arranged in the circumferential direction of the stirring shaft 13 and are uniformly distributed around the central axis of the stirring shaft 13. The inclined stirring rod 18 on the inner stirring rod 16 can dispersedly stir the materials between the outer stirring rod 17 and the stirring shaft 13. Meanwhile, as a preferable technical solution, the inclined stirring rods 18 are distributed on both sides of the inner stirring rod 16.
In the present invention, the outer stirring rod 17 is an L-shaped structure, and includes a vertical section 171 and an inclined section 172, wherein an included angle β is formed at a connection position of the vertical section 171 and the inclined section 172, and the included angle β is an obtuse angle. The vertical section 171 of the present invention is disposed vertically with respect to the horizontal plane, the inclined section 172 is disposed obliquely with respect to the horizontal plane, the inclined section 172 is located in the tapered discharge end 10, and the vertical section 171 is located in the mixing tank 8.
The helical mixing blade 22 of the present invention is capable of turning the material located in the conical discharge end 10 upwards and causing the material, the periphery of which is being stirred by the outer mixing rod 17, to enter into a position close to the central axis of the conical discharge end 10. In the present invention, the inner stirring rod 16 and the inclined stirring rod 18 disposed thereon can convey the material located near the central axis to the outside. The cooperation of above-mentioned three can effectively realize the material at the circulation stirring of blending tank 8, and then effectively increase stirring efficiency.
When the material crusher is used, different raw materials are required to be fed into the feeding pipe 4 through the single material feeding port 1, and are fed into the discharging end of the feeding pipe 4 under the action of the feeding auger 19 driven by the feeding auger driver 2 until the raw materials enter the primary dispersing tank body 6, and the agglomerated materials can be crushed through stirring and feeding of the feeding auger 19. Because the discharge end of pan feeding pipe 4 is located the entry top of the dispersion sieve section of thick bamboo 20 in elementary dispersion jar 6, consequently, the material that enters into in elementary dispersion body 6 can drop in dispersion sieve section of thick bamboo 20.
The dispersing screen drum 20 is driven by a screen drum driving shaft 21 driven by the primary dispersing driver 5 and rotates, the centrifugal force generated by rotation disperses the materials in the dispersing screen drum 20 again, and the dispersed materials enter the primary dispersing tank body 6 through the through holes in the dispersing screen drum 20 and enter the mixing material inlet 7 in a relatively dispersing mode and further enter the mixing tank body 8.
A stirring shaft 13 is arranged in the mixing tank body 8, the stirring shaft 13 can rotate under the driving of a stirring driver 12 and drives an inner stirring rod 16, an outer stirring rod 15 and a plurality of stirring inclined rods 18 distributed on the inner stirring rod and the outer stirring rod to stir and mix materials in the mixing tank body 8, and meanwhile, a spiral stirring blade 22 in the conical discharge end 10 can stir the materials in the conical discharge end 10 to avoid the materials from being deposited at the mixing discharge end 11.
Mix discharge end 11 department and be provided with the blowing valve, after the stirring is accomplished, the blowing valve is opened and can be made the material discharge from mixing discharge end 11 department.
Finally, although the present description refers to embodiments, not every embodiment contains only a single technical solution, and such description of the present description is for clarity reasons only, and those skilled in the art should make the description as a whole, and the technical solutions in the embodiments can be appropriately combined to form other embodiments that can be understood by those skilled in the art.
Claims (10)
1. A production process of a crosslinked polyethylene PEX-A pipe is characterized by comprising the following steps: the process comprises the following steps of 1) preparing the raw materials in parts by weight: 100 parts of high-density polyethylene resin, 0.2 to 1 part of di-tert-butyl peroxide, 0.2 to 0.6 part of tetra [ beta- (3,5-di-tert-butyl-4-hydroxyphenyl) propionic acid ] pentaerythritol ester and 0.1 to 0.3 part of tri (2,4-di-tert-butyl) phosphite;
2) Mixing high-density polyethylene resin, tetra [ beta- (3,5-di-tert-butyl-4-hydroxyphenyl) propionic acid ] pentaerythritol ester and tri (2,4-di-tert-butyl) phosphite in a high-speed mixer for 5 to 10 minutes, weighing the powder, feeding the powder into a main feeding port of a double-screw extruder, and plasticizing and uniformly mixing the powder in the double-screw extruder to form a molten compound I;
3) Feeding 0.2-1 part of di-tert-butyl peroxide into a double-screw extruder through a liquid metering pump, and uniformly mixing the di-tert-butyl peroxide and the fusant I in the double-screw extruder to obtain a fusant II;
4) Feeding the molten compound II into a single-screw extruder from a double-screw extruder, and further mixing and pressurizing in the single-screw extruder to obtain a molten compound III;
5) Feeding the melt III from the tail end of the single-screw extruder to a ram extruder die, and forming and crosslinking the melt III in the ram extruder die.
2.6 Cooling and shaping the pipe in the stamping type extruder die to obtain the cross-linked polyethylene PEX-A pipe.
3. The process for producing a crosslinked polyethylene PEX-a pipe according to claim 1, wherein: the extrusion temperature of the twin-screw extruder in the step 2) is controlled to be 135-150 ℃, and the screw rotating speed is controlled to be 100-150 rpm.
4. The process for producing a crosslinked polyethylene PEX-a pipe according to claim 1, wherein: the extrusion temperature of the single-screw extruder in the step 4) is 140-150 ℃, and the screw rotation speed is 10rpm-40rpm.
5. The process for producing a crosslinked polyethylene PEX-a pipe according to claim 1, wherein: the length of the stamping type extruder die is 0.5m to 2m, and the temperature is 220 ℃ to 240 ℃.
6. A high-speed mixer of raw materials for the process of producing a PEX-A pipe of crosslinked polyethylene according to any one of claims 1 to 4, characterized in that: the raw material high-speed mixer comprises a mixing tank body (8), the mixing tank body (8) comprises a mixing feeding port (7) communicated with the inside of the mixing tank body, and the mixing feeding port (7) is positioned at the top of the mixing tank body (8); a stirring shaft (13) is arranged in the mixing tank body (8), the central axis of the stirring shaft (13) is superposed with the central axis of the mixing tank body (8), and the stirring shaft (13) is driven by a stirring driver (12) positioned at the top of the mixing tank body (8); the stirring shaft (13) is connected with an inner stirring rod (16) through an inner connecting rod (14), an outer stirring rod (17) is arranged between the inner stirring rod (16) and the inner wall of the mixing tank body (8), and the outer stirring rod (17) is connected with the stirring shaft (13) through an outer connecting rod (15); the outer stirring rods (17) and the inner stirring rods (16) are alternately arranged and uniformly distributed around the central axis of the stirring shaft (13); the mixing feeding port (7) is connected with the primary dispersing tank body (6), the primary dispersing tank body (6) is provided with a screen drum driving shaft (21) which is coaxial with the primary dispersing tank body, the screen drum driving shaft (21) is fixedly connected with a dispersing screen drum (20) at the position positioned in the primary dispersing tank body (6), and the outer wall of the dispersing screen drum (20) is provided with a plurality of through holes; the dispersing screen cylinder (20) is positioned below the inlet of the primary dispersing tank body (6), and a distance enough for materials to pass is reserved between the outer wall of the dispersing screen cylinder (20) and the inner wall of the primary dispersing tank body (6); the entry linkage of the elementary dispersion jar body (6) has pan feeding pipe (4), and the inside of pan feeding pipe (4) is provided with pan feeding auger (19), and pan feeding auger (19) are driven by pan feeding auger driver (2), just pan feeding auger driver (2) are located single material pan feeding mouth (1) department of pan feeding pipe (4).
7. The high-speed mixer of raw materials according to claim 5, wherein: the bottom of the mixing tank body (8) is a conical discharge end (10) which is coaxial with the mixing tank body, a mixing discharge hole (11) is positioned at the bottom end of the conical discharge end (10) and is communicated with the interior of the conical discharge end (10), a spiral stirring blade (22) is fixedly connected to the position where the stirring shaft (13) extends into the conical discharge end (10), and when the spiral stirring blade (22) extends to the connecting position of the mixing tank body (8) and the conical discharge end (10) along the stirring shaft (13), the radius of the spiral stirring blade (22) is gradually increased; the outer stirring rod (17) is provided with a vertical section (171) and an inclined section (172) which are arranged in parallel with the inner wall of the mixing tank body (8) and the inner wall of the conical discharge end (10), and an obtuse angle structure is formed at the connecting position of the vertical section (171) and the inclined section (172); a plurality of inclined stirring rods (18) are arranged on the inner stirring rod (16) and the outer stirring rod (17).
8. The high-speed mixer of raw materials according to claim 6, wherein: mixing tank reinforcing ribs (9) are arranged on the outer walls of the mixing tank body (8) and the conical discharge end (10), and the mixing tank reinforcing ribs (9) are uniformly distributed around the central axis of the mixing tank body (8).
9. The high-speed mixer of raw materials as claimed in claim 7, wherein: the primary dispersing tank body (6) comprises a reducing section (61) and a straight cylinder section (62) which are fixed into a whole, the dispersing screen cylinder (20) is provided with a flaring feeding section (201) which is positioned in the reducing section (61), the flaring feeding section (201) and the screening cylinder section (202) which is positioned in the straight cylinder section (62) are fixed into a whole, and the connecting position of the flaring feeding section (201) and the screening cylinder section (202) adopts smooth transition; the screening cylinder section (202) is fixedly connected with the bottom end of the screening cylinder driving shaft (21) through a bottom connecting end (203).
10. The high-speed mixer of raw materials according to claim 8, characterized in that: the cross section of the bottom connecting end (203) is triangular, and the bottom connecting end has an inclined guide surface inclined towards the through hole on the dispersion screen drum.
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|---|---|---|---|
| CN202211410871.1A CN115709555B (en) | 2022-11-11 | 2022-11-11 | Raw material high-speed mixer applied to production process of crosslinked polyethylene PE-Xa (polyethylene-x) pipe |
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|---|---|---|---|
| CN202211410871.1A CN115709555B (en) | 2022-11-11 | 2022-11-11 | Raw material high-speed mixer applied to production process of crosslinked polyethylene PE-Xa (polyethylene-x) pipe |
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| CN115709555B CN115709555B (en) | 2023-07-21 |
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