CN111701553A - Polymerization reactor suitable for high-viscosity PTT production - Google Patents
Polymerization reactor suitable for high-viscosity PTT production Download PDFInfo
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- CN111701553A CN111701553A CN202010426090.6A CN202010426090A CN111701553A CN 111701553 A CN111701553 A CN 111701553A CN 202010426090 A CN202010426090 A CN 202010426090A CN 111701553 A CN111701553 A CN 111701553A
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/18—Stationary reactors having moving elements inside
- B01J19/1887—Stationary reactors having moving elements inside forming a thin film
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B7/00—Mixing; Kneading
- B29B7/30—Mixing; Kneading continuous, with mechanical mixing or kneading devices
- B29B7/34—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices
- B29B7/38—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary
- B29B7/40—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary with single shaft
- B29B7/44—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary with single shaft with paddles or arms
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
- B01J19/0013—Controlling the temperature of the process
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0053—Details of the reactor
- B01J19/0066—Stirrers
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B7/00—Mixing; Kneading
- B29B7/30—Mixing; Kneading continuous, with mechanical mixing or kneading devices
- B29B7/34—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices
- B29B7/38—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary
- B29B7/40—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary with single shaft
- B29B7/402—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary with single shaft using a rotor-stator system with intermeshing elements, e.g. teeth
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
- C08G63/02—Polyesters derived from hydroxycarboxylic acids or from polycarboxylic acids and polyhydroxy compounds
- C08G63/12—Polyesters derived from hydroxycarboxylic acids or from polycarboxylic acids and polyhydroxy compounds derived from polycarboxylic acids and polyhydroxy compounds
- C08G63/16—Dicarboxylic acids and dihydroxy compounds
- C08G63/18—Dicarboxylic acids and dihydroxy compounds the acids or hydroxy compounds containing carbocyclic rings
- C08G63/181—Acids containing aromatic rings
- C08G63/183—Terephthalic acids
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
- C08G63/78—Preparation processes
- C08G63/785—Preparation processes characterised by the apparatus used
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Abstract
The invention relates to the field of polymer equipment, and discloses a polymerization reactor suitable for producing high-viscosity PTT, which comprises a horizontal cylindrical shell, a first rotating shaft, a second rotating shaft, a plurality of annular discs and a plurality of hollowed annular discs; the first rotating shaft and the second rotating shaft divide the interior of the horizontal cylindrical shell into a low-viscosity area close to the feeding hole and a high-viscosity area close to the discharging hole; a plurality of annular disks in the low-viscosity area are axially fixed on the first rotating shaft in a serial connection mode; a plurality of hollow annular disks in the high-viscosity area are axially fixed on the second rotating shaft in a serial connection mode; a scraper is arranged between two adjacent hollow annular disks. The polymerization reactor is internally provided with two groups of stirrers with different rotating speeds, and the barrel close to the discharge port side is internally provided with the scraper, so that the high-viscosity polymer can continuously update the liquid film under the matching of the two groups of stirrers and the scraper, the effects of mixing and mass transfer are effectively provided, and the production capacity of the polymerization reactor is improved.
Description
Technical Field
The invention relates to the field of polymer reaction equipment, in particular to a polymerization reactor suitable for producing high-viscosity PTT.
Background
PTT, namely polytrimethylene terephthalate, has the characteristics of softness of nylon, bulkiness of acrylic fibers, stain resistance of terylene, inherent elasticity of PTT, normal-temperature dyeing and the like due to the unique molecular structure, and is attracted more attention due to excellent comprehensive performance.
The existing PTT polycondensation reaction device meets the requirement that the viscosity of the PTT used in downstream production is extremely high (more than 0.9 dL/g), when the viscosity reaches 0.8dL/g, small molecules are difficult to separate, the viscosity is slowly increased, and due to poor heat stability of the PTT, the reaction time is increased, the reaction is reversely carried out, the viscosity is reduced, so that early products need solid-phase tackifying, and the production efficiency is low.
With the development of polyester polymerization technology, reactors such as disc and squirrel cage are beginning to be applied to the industrial production of PTT. Chinese patent CN2707362Y discloses a novel polymerization reactor, the barrel is equipped with the feed inlet, the discharge gate, and multiunit ring dish agitator, the lateral part is equipped with between the ring dish and draws the membrane steel sheet, the ring dish can form perpendicular membrane and parallel membrane with axial drawing the membrane steel sheet, to conventional polyester, can increase mass transfer area and stirring efficiency, and can effectual assurance plug flow effect, reduce the backmixing, but to high viscous PTT, because the mobility is poor, the baffle can hinder the flow of material, increase material dwell time, increase degradation probability, thereby be unfavorable for reverse going on, can increase the backmixing phenomenon simultaneously. Because PTT's mobility is poor, the terminal agitator of polycondensation, when the disc draws the membrane, the pole-climbing phenomenon of material is also more serious, 50~80% material is hung on the disc, is difficult to further renewal reaction, and postpones the ejection of compact, and seriously influences production efficiency, increases along with time, the material of hanging the dish is heated and is degraded, viscosity begins to descend again, the polymer of partial degradation flows to the discharge gate gradually, directly influences the hue of product, and the viscosity of material can't obtain further improvement. Chinese patent CN208406979U discloses a novel final polycondensation kettle, which adopts a horizontal structure and comprises a barrel, wherein one end of the barrel is a passive end and a passive end cover, the other end of the barrel is an active end and an active end cover, the barrel is provided with an ear type support, a feed inlet, a discharge outlet and a gas phase port, a squirrel cage type stirring device is arranged in the barrel, the stirring device is connected with a gear reduction box and a motor through a gear coupling, and a supporting surface of the ear type support is positioned in the center of the barrel; the honeycomb jacket structure is adopted at ear type support of barrel, and half pipe jacket structure is adopted at the barrel middle part, and the device can effectual improvement capacity utilization ratio, improves production efficiency. However, the squirrel cage agitator has no baffle or grid, the material is easy to short-circuit, the molecular weight distribution can widen, and the product quality is unstable.
Disclosure of Invention
Aiming at the problems, in order to enable the polymerization reactor to produce higher-viscosity polymers, the invention provides the polymerization reactor suitable for the production of the high-viscosity PTT.
The specific technical scheme of the invention is as follows: a polymerization reactor suitable for producing high-viscosity PTT comprises a horizontal cylindrical shell, wherein a feed inlet and a discharge outlet are respectively formed in two ends of the bottom of the horizontal cylindrical shell, and a gas phase port is formed in the side, close to the discharge outlet, of the horizontal cylindrical shell. The polymerization reactor also comprises a first rotating shaft, a second rotating shaft, a plurality of annular disks and a plurality of hollowed annular disks; the first rotating shaft and the second rotating shaft are axially fixed at two ends in the horizontal cylindrical shell in series and can realize asynchronous rotation, and the first rotating shaft and the second rotating shaft divide the interior of the horizontal cylindrical shell into a low-viscosity area close to the feed inlet and a high-viscosity area close to the discharge outlet; the plurality of annular disks in the low-viscosity area are axially fixed on the first rotating shaft in a serial mode; the plurality of hollow annular discs in the high-viscosity area are axially fixed on the second rotating shaft in a serial connection mode; a scraper is arranged between two adjacent hollow annular disks in the horizontal cylindrical shell, and the top of the scraper is higher than the liquid level of the material.
The polymerization reactor of the invention is internally divided into a low-viscosity area and a high-viscosity area from the feed inlet to the discharge outlet in the axial direction. The working principle is as follows: after a prepolymer from a pre-polycondensation kettle enters a polymerization reactor from a feed inlet, a polymer melt is adhered to the surface of an annular disc under the stirring of the continuously rotating annular disc, the prepolymer is driven by the annular disc to form an adhesive film and form a sagging film under the action of gravity, a stretching film is formed under the action of a transverse plate vertical to the annular disc, a new liquid film interface is continuously generated due to the continuous driving of the annular disc and the continuous sliding of a liquid film, so that the surface of the liquid film is continuously updated, small molecules generated in the polymerization process can be continuously separated from the melt, the polymerization reaction is continuously carried out, the polymerization degree is gradually increased, and the polymer melt with higher viscosity is obtained; the materials sequentially pass through the low-viscosity area and the high-viscosity area, and reach the required viscosity when reaching the discharge hole, so that qualified products are produced.
The higher the viscosity of the polymer melt is, the thicker the liquid film adhered to the annular disc is, when a product with higher viscosity is produced by using the same reactor, the sum of the liquid films adhered between the two hollowed-out annular discs in a high-viscosity area is larger than the axial distance between the two hollowed-out annular discs, so that the polymer liquid films between the two hollowed-out annular discs are connected into a whole, a large amount of high-viscosity polymer is adhered to the hollowed-out annular discs and rotates together with the hollowed-out annular discs, the updating of the liquid films is also reduced sharply, the further progress of polymerization reaction is greatly hindered, and the liquid level at a discharge port is reduced or even the discharge port cannot be discharged; over time, this portion of the melt gradually degrades again, severely affecting product quality. In order to produce a new product with higher viscosity, a plurality of groups of scrapers fixed on the inner wall of the cylinder body are additionally arranged between adjacent hollow annular disks close to a high-viscosity area at the discharge port, and the hollow annular disks move relative to the scrapers in an annular manner when rotating, so that a thick liquid film adhered to the hollow annular disks is cut by the scrapers, the thickness of the liquid film is reduced, the surface updating area is increased, and on the other hand, a high-viscosity melt is pushed by the scrapers to move towards the discharge port, and a product with higher viscosity is successfully produced.
The invention divides the inner cavity of the polymerization reactor into a low-viscosity area and a high-viscosity area, designs stirrers with different structural forms along with the change of material characteristics, not only considers the process requirements of polycondensation reaction, the fluidity and the film forming property of materials under different viscosities, but also considers the maturity and the difficulty coefficient of the manufacturing process.
Specifically, two different stirrers are arranged in the polymerization reactor, and the two stirrers are respectively driven by different motors externally matched with the stirrers, so that the rotation at different rotating speeds can be realized. In the low-viscosity section of the polymerization reaction, the corresponding stirrer can provide a large amount of film-forming surface area, and the functions of mixing, reaction, devolatilization of small molecular components and the like can be well realized. In the polymerization high-viscosity section, the corresponding stirrer and the scraper are matched to complete the surface renewal and axial flow of the corresponding high-viscosity polymer.
Preferably, the ratio of the length of the low-tack region to the length of the high-tack region is from 1:0.2 to 0.5.
The reason for controlling the low-viscosity zone to the high-viscosity zone at the above ratio is that: in a low-viscosity zone in the high-viscosity polycondensation reactor, the viscosity of the PTT can reach 0.6-0.7 dL/g from 0.2-0.3 dL/g, in the process, a large amount of PTT small molecules are separated out through the polycondensation reaction, the molecular weight of the PTT is continuously increased, and the required time is long; in the high-viscosity zone, the molecular weight of the PTT is increased quickly, so that small molecules which need to be removed are reduced, the viscosity of the high-viscosity zone can be increased quickly even if the high-viscosity zone has no large devolatilization area, so that the required stirring time is shortened, namely, the required reaction kettle space is reduced, and the axial length of the reactor required by the cylindrical reaction kettle, namely the high-viscosity zone, is reduced.
Preferably, a plurality of circular arc-shaped hollow holes concentric with the hollow annular disc are formed in the hollow annular disc.
Preferably, the total hollowed-out area of the circular arc-shaped hollowed-out holes accounts for 10-40% of the area of the hollowed-out annular disc.
Preferably, the width of the hollowed-out annular disc is gradually reduced from the feed inlet to the discharge outlet; the total hollow area on the hollow annular disc is gradually increased from the feed inlet to the discharge outlet; the distance between two adjacent hollow annular disks is gradually increased from the feed inlet to the discharge outlet.
Because of the adhesion, annular disc is at the rotatory in-process, the PTT fuse-element adheres to the disc surface, be taken in succession and rotatory along with the disc, it is that the PTT fuse-element begins to droop because of the action of gravity to rotate to a take the altitude, if annular disc is solid, the PTT fuse-element need overcome adhesion and centrifugal force and just can droop, and in fretwork part, the PTT fuse-element only need overcome centrifugal force and can droop, to the higher PTT fuse-element of viscosity, the adhesion effect is stronger, the droop speed is slow, the quantity of flagging membrane is few, the surface renewal rate is low, and the annular disc of fretwork can strengthen the formation of flagging membrane effectively, increase total liquid film surface renewal rate, along with the lasting rising of PTT fuse-element viscosity, fretwork area increases gradually, in order to guarantee higher liquid film surface renewal rate.
Preferably, inclined baffles which are parallel to the annular disks and have tops higher than the liquid level of the material are arranged on two sides of a group of the annular disks on the inner wall of the horizontal cylindrical shell, an inclined angle is arranged between the top edge of each inclined baffle and the horizontal plane, and a plurality of elongated channels for fluid to pass through are arranged at the bottoms of the inclined baffles.
Along with the flowing of the materials from the feed inlet to the discharge outlet, the PTT melt is continuously polymerized, the small molecules are continuously removed, the molecular chain is gradually lengthened, the molecular weight is gradually increased, if the materials have enough surface renewal rate under the action of the stirrer and can realize the effect of plug flow, the molecular weight distribution range of the PTT product is small, and the performance is stable; if the product distribution range is wide, the color value of the product is poor, and the expected performance cannot be ensured. A plurality of baffles are arranged between the annular disks of the reactor, so that the back mixing of the melt can be reduced, and the molecular weight distribution of the product is relatively uniform. The upper surface of the liquid level in the reactor is actually inclined due to the rotation and the driving of the stirrer, so the baffle is also designed to be an inclined baffle. The existence of the baffle can keep the melt liquid level between the two baffles, so that the melt polymerization reaction between the two baffles is completed more fully and uniformly, but the baffle also obstructs the axial flow of the melt, and therefore, a slender channel is arranged between the bottom of the baffle and the inner wall of the reactor barrel to be used as a channel for the axial flow of the melt. Preferably, the outer edges of each set of annular disks are connected by an axial transverse plate.
The transverse plate can form an axial pulling film and strengthen the sagging film.
Preferably, inclined baffles are arranged on two sides of each group of 2-6 adjacent annular disks.
Preferably, the inclined angle between the inclined baffle and the horizontal plane is 10-45 degrees.
Preferably, the root of the scraper is fixed at a position, extending out of the liquid level, of the hollow annular disc on the inner wall of the horizontal cylindrical shell in a rotating manner, and an included angle between the outer diameter of the hollow annular disc and the head of the scraper and a tangent line of the intersection point of the scraper on the cross section of the hollow annular disc is an obtuse angle (an angle alpha is greater than 90 degrees in fig. 2).
Through the position and the angle of strict restriction scraper, when can making polymerization liquid membrane scrape thin, promoted to the inboard flow of fretwork annular disc by the scraper, reduce material resistance (relatively spacious, do not have the blockking of fretwork annular disc) to be favorable to the material to flow to the discharge gate direction, the dwell time of control material effectively prevents that side reaction and adverse reaction from taking place to the overlimit.
Preferably, the longitudinal generatrix of the scraper is parallel to the cross section of the hollowed-out annular disc, and the included angle between the cross section of the scraper and the surface of the hollowed-out annular disc is 15-45 degrees.
The included angle between the cross section of the scraper and the surface of the hollow annular disc is limited at the angle, so that the polymer liquid film can flow to the direction of the discharge port along the axial direction of the reactor while being scraped to be thin, the retention time of materials is effectively controlled, and the side reaction and the reverse reaction are prevented from exceeding the limit.
Preferably, the head of the scraper is close to the second rotating shaft.
The head of the scraper is close to the second rotating shaft and can be used for scraping hanging materials on the second rotating shaft.
Preferably, the scraper is of a hollow structure, and the interior of the scraper is heated by a heat medium.
The fluidity of the high-viscosity polymer can be further increased by heating the scraper with a heat medium.
Preferably, the inner end of the second rotating shaft and the inner end of the first rotating shaft are connected and supported through a sliding bearing seat with two open ends of a self-lubricating bearing, and the sliding bearing seat is fixed through a support frame fixed on the inner wall of the horizontal cylindrical shell.
The invention skillfully selects the sliding bearing seat with two open ends for connecting the stirrers at two sides, and because the two ends of the sliding bearing seat are in open structures, polymer melt in the cylinder body can flow into the sliding bearing during operation, thereby playing a self-lubricating role without adding other lubricants.
Preferably, the horizontal cylindrical shell comprises an inner cylinder, a jacket cylinder arranged on the outer side of the inner cylinder and end covers sealed at two ends of the inner cylinder and the jacket cylinder; and the end cover is provided with a sealing and supporting device for sealing and supporting the cylinder body and the first rotating shaft and the second rotating shaft.
Preferably, the center line of the horizontal cylindrical shell is higher than the axes of the first rotating shaft and the second rotating shaft.
When the inner cylinder is cylindrical, the central line of the stirrer is eccentrically arranged downwards compared with the central line of the inner cylinder, and the space without the stirrer at the upper part of the inner cylinder is a gas phase flowing space, so that micromolecule gas phase components generated in the polymerization reaction process are upwards converged above the inner cylinder and are discharged from a gas phase outlet.
Compared with the prior art, the invention has the beneficial effects that:
(1) the invention arranges two stirrers with different rotating speeds and different structures in the same reactor, and the corresponding stirrers can provide a large amount of film-forming surface area in a low-viscosity zone of polymerization reaction, thereby well realizing the functions of mixing, reaction, devolatilization of micromolecular components and the like. In the high-viscosity area of the polymerization reaction, the surface renewal and axial flow of the corresponding high-viscosity polymer are completed by the matching of the corresponding stirrer and the scraper. Under the cooperation of the two stirrers and the scraper, the polymer can still efficiently update the liquid film when the viscosity is higher, the mixing and mass transfer effects when the viscosity is higher are effectively improved, and the production capacity and the product range of the polycondensation reactor are effectively improved.
(2) The polymerization reactor is internally provided with the scraper, so that a liquid film with large thickness adhered to the hollow annular disc can be scraped into a liquid film with small thickness, the thickness of the scraped liquid film depends on the distance between the edge of the scraper and the hollow annular disc (can be designed/adjusted according to requirements), the surface of the liquid film can be continuously updated when the viscosity is high, and small molecules generated by polymerization reaction continuously separate from a melt, so that the viscosity is continuously increased (at least can reach 0.9-1.0 dL/g).
(3) Through the optimal design of the structure and the position relation of the scraper, the polymeric liquid film is pushed to flow towards the inner side of the hollow annular disc by the scraper while being scraped to be thin, so that the material resistance is reduced, the material is pushed to flow towards the discharge port of the cylinder body, the retention time of the material is effectively controlled, and side reaction and counter reaction are prevented from exceeding the limit.
(4) Because the scraper is internally provided with the heat medium channel, the scraper can be externally connected with the heat medium to carry out temperature regulation, the local temperature increase can accelerate the polymerization reaction in the high-viscosity area on the one hand, and the fluidity of the high-viscosity melt can be improved on the other hand, thereby being beneficial to the production of qualified products.
Drawings
FIG. 1 is a front cross-sectional view of the present invention;
FIG. 2 is a schematic view of a position and structure of the hollowed-out annular disc and the scraper in the present invention;
FIG. 3 is a schematic view of the position and configuration of the inclined baffle of the present invention;
FIG. 4 is a schematic diagram of a position and structure of the annular disk of the present invention.
The reference signs are: the device comprises a horizontal cylindrical shell 1, a feed inlet 2, a discharge outlet 3, a gas phase port 4, a first rotating shaft 5, a second rotating shaft 6, an annular disc 7, a hollowed annular disc 8, a scraper 9, an arc-shaped hollowed hole 10, an inclined baffle 11, a transverse plate 12, a sliding bearing seat 13, a support frame 14, an inner cylinder 15, a jacket cylinder 16, an end cover 17, a sealing and supporting device 18 and a long and thin channel 19.
Detailed Description
The present invention will be further described with reference to the following examples. The devices, connections, and methods referred to in this disclosure are those known in the art, unless otherwise indicated.
Example 1
As shown in FIG. 1, a polymerization reactor suitable for the production of a high viscosity PTT comprises a horizontal cylindrical shell 1, a first rotating shaft 5, a second rotating shaft 6, sixteen annular disks 7 and six hollowed-out annular disks 8.
The horizontal cylindrical shell comprises an inner cylinder body 15, a jacket cylinder body 16 arranged on the outer side of the inner cylinder body and end covers 17 sealed at two ends of the inner cylinder body and the jacket cylinder body; and the end cover is provided with a sealing and supporting device 18 for sealing and supporting the first rotating shaft and the second rotating shaft. The two ends of the bottom of the horizontal cylindrical shell are respectively provided with a feeding hole 2 and a discharging hole 3, and the side of the top of the horizontal cylindrical shell, which is close to the discharging hole, is provided with a gas phase hole 4. As shown in fig. 2, the center line of the horizontal cylindrical shell is higher than the axes of the first rotating shaft and the second rotating shaft (i.e. eccentric design).
The first rotating shaft and the second rotating shaft are axially fixed at two ends in the horizontal cylindrical shell in series and can realize asynchronous rotation (the inner side end of the second rotating shaft and the inner side end of the first rotating shaft are connected and supported through sliding bearing seats 13 with two open ends of a self-lubricating bearing, the sliding bearing seats are fixed through a support frame 14 fixed on the inner wall of the horizontal cylindrical shell), and the first rotating shaft and the second rotating shaft divide the inside of the horizontal cylindrical shell into a low-viscosity area close to a feeding hole and a high-viscosity area close to a discharging hole (the length ratio is 1: 0.35).
As shown in fig. 4, the annular disks in the low-viscosity area are axially fixed on the first rotating shaft in a serial form, and the outer edges of each group of annular disks are connected through an axial transverse plate 12. Inclined baffles 11 which are parallel to the annular disks and the tops of which are higher than the liquid level of the materials are arranged on two sides of a group of 2-5 annular disks on the inner wall of the horizontal cylindrical shell, as shown in fig. 3, an inclined angle (25 degrees) is arranged between the top edge of each inclined baffle and the horizontal plane, and two elongated channels 19 for fluids to pass through are arranged at the bottoms of the inclined baffles.
The hollow annular discs in the high-viscosity area are axially fixed on a second rotating shaft in a series connection mode; as shown in fig. 2, five circular arc-shaped hollow holes 10 concentric with the hollow annular disc are formed in the hollow annular disc, and the total hollow area accounts for 10-40% of the area of the hollow annular disc. The width of the hollowed annular disc of the arc-shaped hollowed hole is gradually reduced from the feed inlet to the discharge outlet; the total hollow area on the hollow annular disc is gradually increased from the feed inlet to the discharge outlet; the distance between two adjacent hollow annular disks is gradually increased from the feed inlet to the discharge outlet.
As shown in fig. 2, a scraper 9 is arranged between two adjacent hollow annular discs in the horizontal cylindrical shell, and the top of the scraper is higher than the liquid level of the material (when in reaction, the liquid level is an inclined plane due to the high viscosity of the material and the rotation of the annular discs, and the head of the scraper is close to the second rotating shaft). The root of the scraper is fixed at the position, on the inner wall of the horizontal cylindrical shell, of the hollow annular disc, which extends out of the liquid level in a rotating manner, and the included angle between the outer diameter of the hollow annular disc and the head of the scraper and the tangent line of the intersection point of the scraper on the cross section of the hollow annular disc is 100 degrees (namely, the alpha angle =100 degrees in fig. 2). The longitudinal generatrix of the scraper is parallel to the cross section of the hollowed-out annular disc, and the included angle between the cross section of the scraper and the surface of the hollowed-out annular disc is 30 degrees (namely, the beta angle in fig. 2 is 30 degrees).
Optionally, the scraper is of a hollow structure, the root of the scraper extends out of the sleeve clamping body, and two pipe orifices are arranged for connecting a heating medium for heating, so that the temperature of the material at the scraper can be slightly increased, and the flowability of the high-viscosity polymer is increased.
The above description is only a preferred embodiment of the present invention, and is not intended to limit the present invention, and all simple modifications, changes and equivalent structural changes made to the above embodiment according to the technical spirit of the present invention still belong to the protection scope of the technical solution of the present invention.
Claims (16)
1. A polymerization reactor suitable for producing high-viscosity PTT comprises a horizontal cylindrical shell (1), wherein a feed inlet (2) and a discharge outlet (3) are respectively arranged at two ends of the bottom of the horizontal cylindrical shell, and a gas phase port (4) is arranged on the horizontal cylindrical shell close to the discharge outlet; the method is characterized in that: the device also comprises a first rotating shaft (5), a second rotating shaft (6), a plurality of annular discs (7) and a plurality of hollowed annular discs (8); the first rotating shaft and the second rotating shaft are axially fixed at two ends in the horizontal cylindrical shell in series and can realize asynchronous rotation, and the first rotating shaft and the second rotating shaft divide the interior of the horizontal cylindrical shell into a low-viscosity area close to the feed inlet and a high-viscosity area close to the discharge outlet; the plurality of annular disks in the low-viscosity area are axially fixed on the first rotating shaft in a serial mode; the plurality of hollow annular discs in the high-viscosity area are axially fixed on the second rotating shaft in a serial connection mode; a scraper (9) is arranged between two adjacent hollow annular disks in the horizontal cylindrical shell, and the top of the scraper is higher than the liquid level of the material; inclined baffles (11) which are parallel to the annular disks and the tops of which are higher than the liquid level of the material are arranged on two sides of a group of the plurality of annular disks on the inner wall of the horizontal cylindrical shell.
2. The polymerization reactor of claim 1, wherein: the length ratio of the low-viscosity area to the high-viscosity area is 1: 0.2-0.5.
3. The polymerization reactor of claim 1, wherein: the hollow annular disc is provided with a plurality of circular arc-shaped hollow holes (10) concentric with the hollow annular disc.
4. The polymerization reactor of claim 3, wherein: the total hollowed-out area of the circular arc hollowed-out holes accounts for 10-40% of the area of the hollowed-out annular disc.
5. The polymerization reactor of claim 4, wherein: the width of the hollow annular disc is gradually reduced from the feed inlet to the discharge outlet; the total hollow area on the hollow annular disc is gradually increased from the feed inlet to the discharge outlet; the distance between two adjacent hollow annular disks is gradually increased from the feed inlet to the discharge outlet.
6. The polymerization reactor of claim 1, wherein: an inclined angle is arranged between the top edge of the inclined baffle plate and the horizontal plane, and a plurality of slender channels (19) for fluid to pass through are arranged at the bottom of the inclined baffle plate.
7. The polymerization reactor of claim 6, wherein: the outer edges of each group of annular disks are connected through an axial transverse plate (12).
8. The polymerization reactor of claim 7, wherein: inclined baffles are arranged on two sides of each group of 2-6 adjacent annular disks.
9. The polymerization reactor of claim 8, wherein: the inclination angle of the inclined baffle and the horizontal plane is 10-45 degrees.
10. The polymerization reactor of claim 1, wherein: the root of the scraper is fixed at the position, extending out of the liquid level, of the hollow annular disc on the inner wall of the horizontal cylindrical shell in a rotating mode, and the included angle between the outer diameter of the hollow annular disc and the included angle between the tangent line of the intersection point of the scraper on the cross section of the hollow annular disc and the head of the scraper is an obtuse angle.
11. The polymerization reactor of claim 10, wherein: the longitudinal generatrix of the scraper is parallel to the cross section of the hollowed-out annular disc, and the included angle between the cross section of the scraper and the surface of the hollowed-out annular disc is 15-45 degrees.
12. The polymerization reactor of claim 10, wherein: the head of the scraper is close to the second rotating shaft.
13. The polymerization reactor of claim 1, wherein: the scraper is of a hollow structure, and the interior of the scraper is heated by a heat medium.
14. The polymerization reactor of claim 1, wherein: the inner side end of the second rotating shaft and the inner side end of the first rotating shaft are connected and supported through a sliding bearing seat (13) with self-lubricating bearings and two open ends, and the sliding bearing seat is fixed through a support frame (14) fixed on the inner wall of the horizontal cylindrical shell.
15. The polymerization reactor of claim 1, wherein: the horizontal cylindrical shell comprises an inner cylinder body (15), a jacket cylinder body (16) arranged on the outer side of the inner cylinder body and end covers (17) sealed at two ends of the inner cylinder body and the jacket cylinder body; and the end cover is provided with a sealing and supporting device (18) for sealing and supporting the cylinder body and the first rotating shaft and the second rotating shaft.
16. The polymerization reactor of claim 1, wherein: the central line of the horizontal cylindrical shell is higher than the axes of the first rotating shaft and the second rotating shaft.
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| CN114210285A (en) * | 2021-12-10 | 2022-03-22 | 福建中锦新材料有限公司 | High-viscosity polyamide 6 continuous polymerization production device |
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| CN111701553B (en) | 2022-05-10 |
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Address after: 311200 29 Chenghu Road, Yaqian Town, Xiaoshan District, Hangzhou City, Zhejiang Province Patentee after: Zhejiang Hengyi Petrochemical Research Institute Co.,Ltd. Address before: 311200 Room 501, 3 Blocks, Pearl Plaza, South Bank of Xiaoshan Economic and Technological Development Zone, Xiaoshan District, Hangzhou City, Zhejiang Province Patentee before: ZHEJIANG HENGLAN TECHNOLOGY Co.,Ltd. |