CN114369234A - Polyester on-line production transfer equipment and method for performing production transfer by using same - Google Patents
Polyester on-line production transfer equipment and method for performing production transfer by using same Download PDFInfo
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- CN114369234A CN114369234A CN202111502884.7A CN202111502884A CN114369234A CN 114369234 A CN114369234 A CN 114369234A CN 202111502884 A CN202111502884 A CN 202111502884A CN 114369234 A CN114369234 A CN 114369234A
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- 229920000728 polyester Polymers 0.000 title claims abstract description 60
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 46
- 238000000034 method Methods 0.000 title claims abstract description 24
- 238000005886 esterification reaction Methods 0.000 claims abstract description 80
- 230000032050 esterification Effects 0.000 claims abstract description 79
- 238000006068 polycondensation reaction Methods 0.000 claims abstract description 70
- 239000002994 raw material Substances 0.000 claims abstract description 42
- 239000007788 liquid Substances 0.000 claims abstract description 37
- 239000000835 fiber Substances 0.000 claims abstract description 34
- 239000002002 slurry Substances 0.000 claims abstract description 22
- 238000006243 chemical reaction Methods 0.000 claims abstract description 21
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 17
- 239000006224 matting agent Substances 0.000 claims abstract description 4
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims description 160
- 238000001914 filtration Methods 0.000 claims description 23
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims description 22
- 239000000463 material Substances 0.000 claims description 22
- 238000009987 spinning Methods 0.000 claims description 20
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 claims description 19
- 230000007246 mechanism Effects 0.000 claims description 16
- 239000000155 melt Substances 0.000 claims description 15
- 238000006116 polymerization reaction Methods 0.000 claims description 12
- 238000011084 recovery Methods 0.000 claims description 11
- 239000004408 titanium dioxide Substances 0.000 claims description 11
- 238000000746 purification Methods 0.000 claims description 10
- 239000006185 dispersion Substances 0.000 claims description 8
- 230000008569 process Effects 0.000 claims description 8
- 238000005507 spraying Methods 0.000 claims description 8
- 238000007599 discharging Methods 0.000 claims description 7
- 238000003860 storage Methods 0.000 claims description 7
- 238000003756 stirring Methods 0.000 claims description 6
- 238000009826 distribution Methods 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims description 4
- 238000002360 preparation method Methods 0.000 claims description 4
- 239000000126 substance Substances 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 238000012643 polycondensation polymerization Methods 0.000 claims 1
- 239000002699 waste material Substances 0.000 abstract description 5
- 238000002347 injection Methods 0.000 abstract 1
- 239000007924 injection Substances 0.000 abstract 1
- 238000010586 diagram Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 230000008901 benefit Effects 0.000 description 2
- 230000007704 transition Effects 0.000 description 2
- 230000001174 ascending effect Effects 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 230000010485 coping Effects 0.000 description 1
- 238000010036 direct spinning Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000007380 fibre production Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- 238000003908 quality control method Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000004044 response Effects 0.000 description 1
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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
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
- C08J11/00—Recovery or working-up of waste materials
- C08J11/02—Recovery or working-up of waste materials of solvents, plasticisers or unreacted monomers
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Polyesters Or Polycarbonates (AREA)
Abstract
The application discloses polyester on-line production conversion equipment and a method for performing production conversion by using the same, wherein the equipment comprises an esterification system, a reaction system and a reaction system, wherein the esterification system comprises two esterification reactors connected in series and used for esterifying a raw material; a slurry configuration system comprising a slurry tank for configuring a feedstock to be fed into the esterification system; the polycondensation systems are provided with two sets and are respectively used for producing semi-dull polyester fibers and bright polyester fibers; a matting agent addition system disposed between the esterification system and one of the polycondensation systems; the three-way connecting pipeline is used for communicating the esterification system and the two sets of polycondensation systems, a three-way valve is installed at a node, and through the arrangement of the esterification system and the polycondensation systems and the injection of the delustering agent in front of different polycondensation systems, semi-delustering polyester fibers and super-bright polyester fibers can be flexibly produced and converted at the same time, the liquid level of the slurry tank is controlled to be 68-70%, the rapid production conversion is realized, the resource waste is reduced, and the production cost is reduced.
Description
Technical Field
The invention belongs to the technical field of polyester fiber production, and particularly relates to polyester on-line production conversion equipment and a method for performing production conversion by using the same.
Background
The polyester melt direct spinning has the advantages of high productivity, high efficiency, low energy consumption and low cost, is the most advanced international leading process, and has the problems of wide process regulation influence range, difficult quality control and the like. In particular, polyester fiber manufacturers need frequent product changes to meet market demands. At present, there are two ways for the polyester fiber device to be converted in the industry:
1. the production is stopped, the system is cleaned and then the production is transferred, for example, a polyester device which produces 40 ten thousand tons of capacity per year takes about 10 days for the production transfer, the production is influenced by 11000 tons of capacity, a large amount of transition materials for stopping and starting are generated, the benefit is influenced by about ten million, and the capacity of a single type product is excessive due to the integral switching;
2. the production is carried out on line without stopping, and by taking the example of semi-extinction production of large bright polyester fibers, the melt pipeline contains a titanium dioxide delustering agent, particularly titanium dioxide at the dead corner of the melt pipeline, so that the large bright polyester fibers produced for a long time can not meet the requirements of customers, and the product quality is seriously influenced.
Therefore, in order to increase the response speed for coping with market variation and improve the flexible capability of product conversion, the problem of on-line switching of semi-dull and large bright polyester fibers needs to be solved urgently, and therefore improvement is needed.
Disclosure of Invention
The invention aims to overcome the problems in the prior art and provide a production method and equipment for on-line switching of semi-dull and large bright polyester fibers, which can carry out production switching without stopping and shorten the transition time of production switching.
The application provides a polyester on-line transfer production equipment, includes:
an esterification system comprising two esterification reactors in series for esterifying a feedstock;
a slurry configuration system comprising a slurry tank for configuring a feedstock to be fed into the esterification system;
the polycondensation systems are provided with two sets and are respectively used for producing semi-dull polyester fibers and bright polyester fibers;
a matting agent addition system disposed between the esterification system and one of the polycondensation systems;
and the three-way connecting pipeline is used for communicating the esterification system and the two sets of polycondensation systems, and a three-way valve is arranged at a node.
By adopting the polyester on-line production conversion equipment, one esterification system and two polycondensation systems are arranged, and the delustering agent is injected in front of different polycondensation systems, so that semi-delustering polyester fibers and bright polyester fibers can be flexibly produced and converted at the same time, the liquid level of the slurry tank is controlled to be 68-70%, the rapid production conversion is realized, the resource waste is reduced, and the production cost is reduced.
The polycondensation system includes:
a pre-shrinking reactor;
pre-shrinking a filter;
a pre-shrinking object booster pump;
a finishing reactor;
a final polycondensation filter;
a final polycondensation booster pump;
wherein the pre-shrinking reactor, the pre-shrinking filter, the pre-shrinking object booster pump, the final polycondensation reactor, the final polycondensation filter and the final polycondensation booster pump are sequentially connected in series through pipelines.
Further comprising:
an ethylene glycol recovery purification system for reducing the titanium dioxide content in each of the precondensation reactors and each of the final polycondensation reactors.
The ethylene glycol recovery and purification system comprises:
the upper part of the scraper condenser is connected with a vacuum system, and a scraper and a spraying system are arranged in the scraper condenser;
the liquid seal tank comprises an inner chamber filter and an outer chamber filter;
a glycol storage tank;
a pre-pump filter;
a heat exchanger;
a booster pump;
wherein, two layers of filter screens are arranged in the inner chamber, and the basket type filter is arranged in the outer chamber.
Further comprising:
and the spinning conveying systems are provided with two sets and are respectively communicated with the discharge ends of the polycondensation systems.
The esterification reactor comprises:
a body with an interior cavity and a top cover;
a feed tube mounted on the top cover;
a discharge pipe with a discharge valve and mounted on the body;
the dispersion disc is arranged at the top of the inner cavity of the body and is provided with a plurality of material distributing holes;
and the dredging mechanism is used for dredging the material distribution hole.
Dredge mechanism includes:
the dredging ring is arranged between the top cover and the body;
the dredging pipe sleeves are arranged at the bottom of the dredging ring along the axial direction;
the lifting cylinder is used for driving the dredging ring to lift;
wherein each dredging pipe sleeve corresponds to each distributing hole.
The dispersion impeller includes:
the fixed disc is fixedly arranged at the top of the inner cavity of the body;
the ring groove is arranged on the outer side of the top of the fixed disc;
the movable ring is driven by the rotary driving mechanism to be rotatably installed in the annular groove;
wherein, the material distributing hole penetrates through the inner side of the movable ring and the fixed disc.
Also discloses a production transferring method of the polyester on-line production transferring equipment, which comprises the following steps:
s1, blending raw materials: starting a slurry preparation system to prepare raw materials, and conveying the prepared raw materials to an esterification system;
s2, esterification raw material: the raw materials enter a first esterification reactor to carry out first esterification, and are stirred at the speed of 30-50rpm, after the first esterification is finished, the raw materials enter a second esterification reactor to carry out second esterification, and are stirred at the speed of 30-40 rpm;
wherein the esterification temperature in the first esterification reactor is 260-280 ℃, the liquid level is 80-90 percent, and the pressure is 100-110MPa, the temperature in the second esterification reactor is 270-280 ℃, the liquid level is 80-90 percent, and the pressure is 30-40 MPa;
s3, production of large bright polyester fibers: after the second esterification is finished, adjusting a three-way valve to enable a second esterification reactor to be communicated with a pre-shrinking reactor far away from a delustering agent adding system, discharging the esterified raw materials from the second esterification reactor, enabling the esterified raw materials to enter the pre-shrinking reactor for pre-shrinking, stirring at the speed of 25-30rpm, filtering the esterified raw materials through a pre-shrinking filter after the pre-shrinking is finished, sending the esterified raw materials into a final polycondensation reactor through a pre-shrinking substance booster pump for final shrinking, filtering a melt obtained after the final shrinking through a final polycondensation filter, and then sending the melt into a spinning conveying system through the final polycondensation booster pump for spinning;
wherein the pre-polymerization temperature is 275-285 ℃, the liquid level of an upper chamber of the pre-polymerization reactor is 35-38 percent, the pressure of the upper chamber is 13-15MPa, the liquid level of a lower chamber of the pre-polymerization reactor is 74-80 percent, and the pressure of the lower chamber is 2-3 MPa;
s4, production of semi-dull polyester fibers: after the second esterification is finished, adjusting a three-way valve to enable a second esterification reactor to be communicated with a pre-shrinking reactor close to a delustering agent adding system, discharging the esterified raw materials from the second esterification reactor, entering the pre-shrinking reactor for pre-shrinking, stirring at the speed of 4-5rpm, outputting a titanium dioxide delustering agent from the delustering agent adding system to the pre-shrinking reactor, filtering the pre-shrinking raw materials through a pre-shrinking filter, sending the pre-shrinking raw materials into a final polycondensation reactor through a pre-shrinking substance booster pump for final shrinking, filtering a melt obtained after the final shrinking through the final polycondensation filter, and then sending the melt into a spinning conveying system through a final polycondensation booster pump (306) for spinning;
wherein the pre-polycondensation temperature is 286-290 ℃, and the liquid level of the upper chamber of the pre-polycondensation reactor is 45-50%.
Also comprises a glycol recovery step:
a1, glycol bleed: starting a vacuum system, and feeding ethylene glycol containing oligomers in each prepolymerization reactor and each final polycondensation reactor into a scraper condenser;
a2, recovering ethylene glycol: after the glycol containing the oligomer is sprayed and cooled by a spraying system, a part of the oligomer and the glycol directly fall to the bottom of the scraper, the part of the oligomer and the glycol is brought into the liquid seal tank through a pipeline by the scraper in the rotation process, the glycol containing the oligomer flows into a basket filter of an outer chamber of the liquid seal tank after passing through two layers of filter screens of an inner chamber of the liquid seal tank, and the glycol enters a glycol storage tank;
a3, circulating filtration: and the ethylene glycol containing the oligomer in the outer chamber continuously passes through the pre-pump filter, the booster pump and the heat exchanger and then enters the scraper condenser again for circulating cooling and filtering.
The advantageous effects of the present invention will be explained in detail in the embodiments, thereby making the advantageous effects more apparent.
Drawings
FIG. 1 is a schematic structural diagram of an on-line polyester production conversion apparatus in an embodiment of the present application;
FIG. 2 is a schematic diagram of a specific structure of an ethylene glycol recovery purification system in an embodiment of the present application;
FIG. 3 is a schematic diagram of the structure of an esterification reactor in the example of the present application.
Fig. 4 is a schematic structural diagram of a movable ring in the embodiment of the present application.
Reference numerals
1-esterification system, 2-slurry preparation system, 3-polycondensation system, 301-preshrinking reactor, 302-preshrinking filter, 303-preshrinking object booster pump, 304-final polycondensation reactor, 305-final polycondensation filter, 306-final polycondensation booster pump, 4-delustering agent adding system, 5-ethylene glycol recovery and purification system, 501-scraper condenser, 502-liquid seal tank, 503-ethylene glycol storage tank, 504-pre-pump filter, 505-heat exchanger, 6-body, 7-top cover, 8-feeding pipe, 9-discharging pipe, 10-dispersion disc, 1001-fixed disc, 1002-ring groove, 1003-movable ring, 1004-rotary driving mechanism, 11-material distribution hole, 12-dredging ring, 13-dredging pipe sleeve, 14-lifting cylinder, 15-spinning conveying system.
Detailed Description
The technical solutions in the embodiments of the present application will be described clearly below with reference to the drawings in the embodiments of the present application, and it is obvious that the described embodiments are some, but not all, embodiments of the present application. All other embodiments that can be derived by one of ordinary skill in the art from the embodiments given herein are intended to be within the scope of the present disclosure.
The terms first, second and the like in the description and in the claims of the present application are used for distinguishing between similar elements and not necessarily for describing a particular sequential or chronological order. It will be appreciated that the data so used may be interchanged under appropriate circumstances such that embodiments of the application may be practiced in sequences other than those illustrated or described herein, and that the terms "first," "second," and the like are generally used herein in a generic sense and do not limit the number of terms, e.g., the first term can be one or more than one. In addition, "and/or" in the specification and claims means at least one of connected objects, a character "/" generally means that a preceding and succeeding related objects are in an "or" relationship.
The server provided by the embodiment of the present application is described in detail below with reference to the accompanying drawings through specific embodiments and application scenarios thereof.
Example 1:
as shown in fig. 1 to 4, an embodiment of the present application provides an on-line polyester production conversion apparatus, including:
an esterification system 1 comprising two esterification reactors in series for esterifying a feedstock;
a slurry configuration system 2, which includes a slurry tank, for configuring the raw material to be fed into the esterification system 1;
the polycondensation system 3 is provided with two sets and is respectively used for producing semi-dull polyester fibers and bright polyester fibers;
a matting agent addition system 4 disposed between the esterification system 1 and one of the polycondensation systems;
and the three-way connecting pipeline is used for communicating the esterification system 1 with the two sets of polycondensation systems, and a three-way valve is arranged at a node.
In the embodiment of the application, by adopting the polyester on-line production conversion equipment, one set of esterification system 1 and two sets of polycondensation systems 3 are arranged, and the delustering agent is injected in front of different polycondensation systems 3, so that semi-delustering polyester fibers and bright polyester fibers can be flexibly produced and converted at the same time, the liquid level of the slurry tank is controlled to be 68-70%, the rapid production conversion is realized, the resource waste is reduced, and the production cost is reduced.
Example 2:
in the present embodiment, in addition to the structural features including the foregoing embodiment, the polycondensation system 3 includes:
a pre-shrinking reactor 301;
a pre-shrinking filter 302;
a preshrinking booster pump 303;
a finishing reactor 304;
a finishing polymerization filter 305;
a final polycondensation booster pump 306;
wherein, the pre-shrinking reactor 301, the pre-shrinking filter 302, the pre-shrinking object booster pump 303, the final polycondensation reactor 304, the final polycondensation filter 305 and the final polycondensation booster pump 306 are connected in series in sequence through pipelines.
In this embodiment, due to the above structure, the raw material after the second esterification is discharged from the second esterification reactor and enters the pre-shrinking reactor 301 for pre-shrinking, after the pre-shrinking is completed, the raw material is filtered by the pre-shrinking filter 302 and then sent to the final polycondensation reactor 304 through the pre-shrinking booster pump 303 for final shrinking, and the melt obtained after the final shrinking is filtered by the final polycondensation filter 305 and then sent to the spinning conveying system 15 through the final polycondensation booster pump 306 for spinning.
Example 3:
in this embodiment, in addition to the structural features of the foregoing embodiment, the method further includes:
an ethylene glycol recovery purification system 5 for reducing the titanium dioxide content in each pre-polycondensation reactor 301 and each final polycondensation reactor.
In this embodiment, because of the structure, the arrangement of the ethylene glycol recovery and purification system 5 can effectively remove the content of titanium dioxide in the recycle ethylene glycol system, thereby ensuring the purity of the recycle ethylene glycol used for producing semi-dull and highly bright polyester fibers simultaneously and ensuring the brightness of the highly bright polyester fibers.
Example 4:
in this embodiment, in addition to the structural features of the foregoing embodiment, the ethylene glycol recovery purification system 5 includes:
the scraper condenser 501 is connected with a vacuum system above, and a scraper and a spraying system are arranged in the scraper condenser;
a liquid seal tank 502 including inner chamber filtration and outer chamber filtration;
an ethylene glycol storage tank 503;
a pre-pump filter 504;
a heat exchanger 505;
a booster pump 506;
wherein, two layers of filter screens are arranged in the inner chamber, and the basket type filter is arranged in the outer chamber.
In this embodiment, because the above structure is adopted, the vacuum system is started, the ethylene glycol containing oligomers in each pre-polymerization reactor and each final polymerization reactor enters the scraper condenser 501, after the ethylene glycol containing oligomers is cooled by spraying of the spraying system, a part of oligomers and ethylene glycol directly fall to the bottom of the scraper, the part of oligomers and ethylene glycol is brought into the liquid seal tank 502 through a pipeline by the scraper in rotation, the ethylene glycol containing oligomers flows into the basket filter outside the liquid seal tank 502 after passing through the two layers of filter screens in the inner chamber of the liquid seal tank 502, the ethylene glycol enters the ethylene glycol storage tank 503, the ethylene glycol containing oligomers in the outer chamber continues to pass through the pre-pump filter 504, the booster pump 506 and the heat exchanger 505 and then enters the scraper condenser 501 again for circulating cooling and filtering, and through this way, the content of titanium dioxide in the ethylene glycol system for recycling can be effectively removed, ensures the purity of the recycled ethylene glycol used for simultaneously producing the semi-dull and bright polyester fibers and ensures the brightness of the bright polyester fibers.
Example 5:
in this embodiment, in addition to the structural features of the foregoing embodiment, the method further includes:
and two spinning conveying systems 15 are provided and are respectively communicated with the discharge ends of the polycondensation systems 3.
In the embodiment, due to the adoption of the structure, the spinning system is provided with different threads, so that the individual thread can be transferred according to the market industry, the rapid production transfer is realized, the resource waste is reduced, and the production cost is reduced.
Example 6:
in this embodiment, in addition to including the structural features of the previous embodiment, the esterification reactor includes:
a body 6 with an internal cavity and a cap 7;
a feed pipe 8 mounted on the top lid 7;
a discharge pipe 9 with a discharge valve and mounted on the body 6;
the dispersion disc 10 is arranged at the top of the inner cavity of the body 6 and is provided with a plurality of material distributing holes 11;
and the dredging mechanism is used for dredging the material distribution hole 11.
In this embodiment, owing to adopted foretell structure, during the thick liquids got into body 6 through inlet pipe 8, evenly got into 6 inner chambers bottoms of body through a plurality of branch material holes 11 on the dispersion impeller 10, set up through mediation mechanism, regularly dredges branch material hole 11, avoids blockking up branch material hole 11 because of the thick liquids condenses, makes thick liquids dispersion effect descend, and the phenomenon that feed rate reduces takes place, has improved work efficiency.
Example 7:
in this embodiment, in addition to the structural features of the preceding embodiment, the dredging mechanism includes:
a dredging ring 12 mounted between the top cover 7 and the body 6;
a plurality of dredging pipe sleeves 13 which are axially arranged at the bottom of the dredging ring 12;
a lifting cylinder 14 for driving the dredging ring 12 to lift;
wherein, each dredging pipe sleeve 13 corresponds to each distributing hole 11.
In the embodiment, because the structure is adopted, when the distributing hole 11 is blocked, the lifting cylinder 14 drives the dredging ring 12 to descend, each dredging pipe sleeve 13 is respectively stabbed into each distributing hole 11, then the lifting cylinder 14 drives the dredging ring 12 to ascend, so that a dredging pipeline is far away from the distributing hole 11, dredging of the distributing hole 11 is completed, blocking of the distributing hole 11 due to condensation of slurry is avoided, the guide post is arranged on the inner wall of the top cover 7, the outer wall of the bottom end of the guide post is in sliding fit with the inner wall of the dredging pipe sleeve 13, stability of the dredging pipe sleeve 13 during ascending and descending can be improved, slurry entering the dredging pipe sleeve 13 can be pushed out from the dredging pipe sleeve 13 and falls into the distributing hole 11, the dredging pipe sleeve 13 is prevented from being blocked by the slurry, descending of a slurry dispersing effect of the distributing hole 11 is avoided, the phenomenon of reduction of the feeding speed occurs, and the working efficiency is improved.
Example 8:
in this embodiment, in addition to the structural features of the previous embodiment, the dispersion board 10 includes:
a fixed disk 1001 fixedly mounted on the top of the inner cavity of the body 6;
a ring groove 1002 provided outside the top of the fixed disk 1001;
a movable ring 1003 rotationally mounted in the ring groove 1002 by a rotary driving mechanism 1004;
wherein, the material distributing hole 11 penetrates through the inner side of the movable ring 1003 and the fixed disc 1001.
In the embodiment, due to the adoption of the structure, when slurry falls to the bottom of the inner cavity of the body 6 through each material distributing hole 11, the rotary driving mechanism 1004 continuously operates to drive the movable ring 1003 to rotate in the annular groove 1002, one half of the upper part of each material distributing hole 11 always rotates along with the movable ring 1003, so that the part of the material distributing hole 11 arranged on the fixed disc 1001 and the part of the material distributing hole 11 arranged on the movable ring 1003 are continuously separated and combined in a coaxial manner, the coagulation speed of the slurry in the material distributing hole 11 is reduced, when thick slurry is coagulated on the inner wall of the material distributing hole 11, the driving mechanism stops operating, the material distributing hole 11 is dredged through the dredging mechanism, the rotary driving mechanism comprises a gear ring arranged on the outer peripheral wall of the movable ring 1003 and a gear which is in transmission connection with the gear ring 1003 and drives the gear ring to rotate through a motor, the motor drives the gear ring to rotate with the movable ring 1003, and through the manner, the running frequency of the dredging mechanism is reduced, so that the material distributing hole 11 is kept dredged for a long time.
Example 9:
in the embodiment, a production transfer method of the polyester on-line production transfer equipment is also disclosed, which comprises the following steps:
s1, blending raw materials: starting the slurry preparation system 2 to prepare raw materials, and conveying the prepared raw materials to the esterification system 1;
s2, esterification raw material: the raw materials enter a first esterification reactor to carry out first esterification, and are stirred at the speed of 30-50rpm, after the first esterification is finished, the raw materials enter a second esterification reactor to carry out second esterification, and are stirred at the speed of 30-40 rpm;
wherein the esterification temperature in the first esterification reactor is 260-280 ℃, the liquid level is 80-90 percent, and the pressure is 100-110MPa, the temperature in the second esterification reactor is 270-280 ℃, the liquid level is 80-90 percent, and the pressure is 30-40 MPa;
s3, production of large bright polyester fibers: after the second esterification is finished, adjusting a three-way valve to enable a second esterification reactor to be communicated with a pre-shrinking reactor 301 far away from a delustering agent adding system 4, discharging the esterified raw materials from the second esterification reactor to enter the pre-shrinking reactor 301 for pre-shrinking, stirring at the speed of 25-30rpm, filtering the pre-shrinking raw materials through a pre-shrinking filter 302, sending the pre-shrinking raw materials into a final polycondensation reactor 304 through a pre-shrinking substance booster pump 303 for final shrinking, filtering the melt obtained after the final shrinking through a final polycondensation filter 305, and then sending the melt into a spinning conveying system 15 through a final polycondensation booster pump 306 for spinning;
wherein the pre-polymerization temperature is 275-285 ℃, the liquid level of an upper chamber of the pre-polymerization reactor is 35-38 percent, the pressure of the upper chamber is 13-15MPa, the liquid level of a lower chamber of the pre-polymerization reactor is 74-80 percent, and the pressure of the lower chamber is 2-3 MPa;
s4, production of semi-dull polyester fibers: after the second esterification is finished, adjusting a three-way valve to enable a second esterification reactor to be communicated with a pre-shrinking reactor 301 close to a delustrant adding system 4, discharging the esterified raw materials from the second esterification reactor, enabling the esterified raw materials to enter the pre-shrinking reactor 301 for pre-shrinking and stirring at the speed of 4-5rpm, simultaneously outputting a titanium dioxide delustrant from the delustrant adding system 4 to the pre-shrinking reactor 301, filtering the pre-shrinking raw materials through a pre-shrinking filter 302, sending the pre-shrinking raw materials into a final-shrinking reactor 304 through a pre-shrinking product booster pump 303 for final shrinking, filtering a melt obtained after the final shrinking through a final-shrinking filter 305, and then sending the melt into a spinning conveying system 15 through the final-shrinking booster pump 306 for spinning;
wherein the pre-polycondensation temperature is 286-290 ℃, and the liquid level of the upper chamber of the pre-polycondensation reactor is 45-50%.
In the embodiment, due to the adoption of the structure, the arrangement of one esterification system 1 and two polycondensation systems 3 is adopted, and the delustering agent is injected in front of different polycondensation systems 3, so that the semi-delustering polyester fiber and the bright polyester fiber can be flexibly produced and converted at the same time, and meanwhile, in the spinning system, the different conversion of single lines can be realized according to the market industry by arranging different lines, so that the rapid conversion is realized, the resource waste is reduced, and the production cost is reduced.
Example 10:
in this embodiment, in addition to the structural features of the previous embodiment, the method further includes the step of recovering ethylene glycol:
a1, glycol bleed: starting a vacuum system, and feeding ethylene glycol containing oligomers in each prepolymerization reactor and each final polycondensation reactor into a scraper condenser 501;
a2, recovering ethylene glycol: after the glycol containing the oligomer is sprayed and cooled by a spraying system, a part of the oligomer and the glycol directly fall to the bottom of the scraper, the part of the oligomer and the glycol is brought into the liquid seal tank 502 by the scraper through a pipeline in the rotation process, the glycol containing the oligomer flows into a basket filter of an outer chamber of the liquid seal tank 502 after passing through two layers of filter screens of an inner chamber of the liquid seal tank 502, and the glycol enters a glycol storage tank 503;
a3, circulating filtration: the glycol containing oligomer in the outer indoor part continues to pass through a pre-pump filter 504, a booster pump 506 and a heat exchanger 505 and then enters the scraper condenser 501 again for circulating cooling and filtering.
In this embodiment, because of the structure, the arrangement of the ethylene glycol recovery and purification system 5 can effectively remove the content of titanium dioxide in the recycle ethylene glycol system, thereby ensuring the purity of the recycle ethylene glycol used for producing semi-dull and highly bright polyester fibers simultaneously and ensuring the brightness of the highly bright polyester fibers.
It should be noted that, in this document, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising an … …" does not exclude the presence of other like elements in a process, method, article, or apparatus that comprises the element. Further, it should be noted that the scope of the methods and apparatus of the embodiments of the present application is not limited to performing the functions in the order illustrated or discussed, but may include performing the functions in a substantially simultaneous manner or in a reverse order based on the functions involved, e.g., the methods described may be performed in an order different than that described, and various steps may be added, omitted, or combined. In addition, features described with reference to certain examples may be combined in other examples.
While the present embodiments have been described with reference to the accompanying drawings, it is to be understood that the invention is not limited to the precise embodiments described above, which are meant to be illustrative and not restrictive, and that various changes may be made therein by those skilled in the art without departing from the spirit and scope of the invention as defined by the appended claims.
Claims (10)
1. An online polyester production conversion device is characterized by comprising:
an esterification system (1) comprising two esterification reactors in series for esterifying a feedstock;
a slurry configuration system (2) comprising a slurry tank for configuring the feed of the feedstock to the esterification system (1);
the polycondensation systems (3) are provided with two sets and are respectively used for producing semi-dull polyester fibers and bright polyester fibers;
a matting agent addition system (4) arranged between the esterification system (1) and one of the polycondensation systems;
and the three-way connecting pipeline is used for communicating the esterification system (1) with the two sets of polycondensation systems, and a three-way valve is arranged at a node.
2. The polyester on-line converting apparatus according to claim 1, wherein said polycondensation system (3) comprises:
a preshrinking reactor (301);
a pre-shrinking filter (302);
a preshrinking booster pump (303);
a finishing reactor (304);
a final polycondensation filter (305);
a final polycondensation booster pump (306);
wherein the pre-shrinking reactor (301), the pre-shrinking filter (302), the pre-shrinking object booster pump (303), the final shrinking reactor (304), the final shrinking filter (305) and the final shrinking booster pump (306) are connected in series in sequence through pipelines.
3. The on-line polyester converting apparatus according to claim 2, further comprising:
an ethylene glycol recovery purification system (5) for reducing the titanium dioxide content in each of the pre-polycondensation reactors (301) and the final polycondensation reactors.
4. The on-line polyester converting equipment according to claim 3, wherein said ethylene glycol recovery and purification system (5) comprises:
the scraper condenser (501) is connected with a vacuum system above the scraper condenser, and a scraper and a spraying system are arranged in the scraper condenser;
a liquid seal tank (502) including inner chamber filtration and outer chamber filtration;
a glycol tank (503);
a pre-pump filter (504);
a heat exchanger (505);
a booster pump (506);
wherein, be equipped with two-layer filter screen in the inner room, the outer room is basket filter.
5. The on-line polyester production conversion equipment as claimed in claim 4, further comprising:
and the spinning conveying systems (15) are provided with two sets and are respectively communicated with the discharge ends of the polycondensation systems (3).
6. The on-line polyester production conversion equipment according to claim 5, wherein the esterification reactor comprises:
a body (6) with an inner cavity and a cap (7);
a feed pipe (8) mounted on the top cover (7);
a discharge pipe (9) which is provided with a discharge valve and is mounted on the body (6);
the dispersion disc (10) is arranged at the top of the inner cavity of the body (6) and is provided with a plurality of material distribution holes (11);
and the dredging mechanism is used for dredging the material distribution hole (11).
7. The on-line polyester production conversion equipment as claimed in claim 6, wherein the dredging mechanism comprises:
a pull through ring (12) mounted between the top cover (7) and the body (6);
a plurality of dredging pipe sleeves (13) which are axially arranged at the bottom of the dredging ring (12);
the lifting cylinder (14) is used for driving the dredging ring (12) to lift;
wherein each dredging pipe sleeve (13) corresponds to each distributing hole (11).
8. The polyester on-line converting apparatus according to claim 6, wherein said dispersing plate (10) comprises:
the fixed disc (1001) is fixedly arranged on the top of the inner cavity of the body (6);
a ring groove (1002) provided outside the top of the fixed disk (1001);
the movable ring (1003) is rotationally mounted in the annular groove (1002) through a rotary driving mechanism (1004);
wherein, the material distributing hole (11) penetrates through the inner side of the movable ring (1003) and the fixed disc (1001).
9. A method for converting polyester in-line to the polyester production line of claim 8, comprising the steps of:
s1, blending raw materials: starting the slurry preparation system (2) to prepare raw materials, and conveying the prepared raw materials into the esterification system (1);
s2, esterification raw material: the raw materials enter a first esterification reactor to carry out first esterification, and are stirred at the speed of 30-50rpm, after the first esterification is finished, the raw materials enter a second esterification reactor to carry out second esterification, and are stirred at the speed of 30-40 rpm;
wherein the esterification temperature in the first esterification reactor is 260-280 ℃, the liquid level is 80-90 percent, and the pressure is 100-110MPa, the temperature in the second esterification reactor is 270-280 ℃, the liquid level is 80-90 percent, and the pressure is 30-40 MPa;
s3, production of large bright polyester fibers: after the second esterification is finished, adjusting a three-way valve to enable a second esterification reactor to be communicated with a pre-shrinking reactor (301) far away from a delustering agent adding system (4), discharging the esterified raw materials from the second esterification reactor, pre-shrinking the esterified raw materials into the pre-shrinking reactor (301), stirring the esterified raw materials at the speed of 25-30rpm, filtering the esterified raw materials by a pre-shrinking filter (302) after the pre-shrinking is finished, sending the esterified raw materials into a final polycondensation reactor (304) through a pre-shrinking substance booster pump (303) for final shrinking, filtering the melt obtained after the final shrinking by a final polycondensation filter (305), and then sending the melt into a spinning conveying system (15) through a final polycondensation booster pump (306) for spinning;
wherein the pre-polymerization temperature is 275-285 ℃, the liquid level of an upper chamber of the pre-polymerization reactor is 35-38 percent, the pressure of the upper chamber is 13-15MPa, the liquid level of a lower chamber of the pre-polymerization reactor is 74-80 percent, and the pressure of the lower chamber is 2-3 MPa;
s4, production of semi-dull polyester fibers: after the second esterification is finished, adjusting a three-way valve to enable a second esterification reactor to be communicated with a pre-shrinking reactor (301) close to a delustering agent adding system (4), discharging the esterified raw materials from the second esterification reactor, entering the pre-shrinking reactor (301) for pre-shrinking, stirring at the speed of 4-5rpm, outputting a titanium dioxide delustering agent from the delustering agent adding system (4) to the pre-shrinking reactor (301), filtering the pre-shrinking agent by a pre-shrinking filter (302), sending the pre-shrinking agent into a final condensation polymerization reactor (304) for final shrinking by a pre-shrinking object booster pump (303), filtering the melt obtained after the final shrinking by a final condensation filter (305), and sending the melt into a spinning conveying system (15) for spinning by the final condensation booster pump (306);
wherein the pre-polycondensation temperature is 286-290 ℃, and the liquid level of the upper chamber of the pre-polycondensation reactor is 45-50%.
10. The method for converting polyester into polyester on-line conversion equipment according to claim 9, further comprising the step of recovering ethylene glycol:
a1, glycol bleed: starting a vacuum system, and feeding ethylene glycol containing oligomers in each prepolymerization reactor and each final polycondensation reactor into a scraper condenser (501);
a2, recovering ethylene glycol: after the ethylene glycol containing the oligomer is sprayed and cooled by a spraying system, a part of the oligomer and the ethylene glycol directly fall to the bottom of the scraper, the part of the oligomer and the ethylene glycol are brought into the liquid seal groove (502) through a pipeline by the scraper in the rotation process, the ethylene glycol containing the oligomer flows into a basket filter of an outer chamber of the liquid seal groove (502) after passing through two layers of filter screens of an inner chamber of the liquid seal groove (502), and the ethylene glycol enters an ethylene glycol storage tank (503);
a3, circulating filtration: the ethylene glycol containing the oligomer in the outer chamber continuously passes through a pre-pump filter (504), a booster pump (506) and a heat exchanger (505) and then enters the scraper condenser (501) again for circulating cooling and filtering.
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