CN205650186U - Two cauldron systems of polymerization esterify - Google Patents

Abstract

The utility model relates to a two cauldron systems of polymerization esterify, polycondensation reactor's the preshrunk in advance of esterifying gathers the discharge gate and gathers the polymerization ware feed inlet that fluid level control valve or preshrunk gathers the melt -conveying pump and do not have a stirring polymerization ware through preshrunk and link to each other. The upper portion of polymerization ware inner chamber is equipped with cloth liquid dish, is equipped with the falling liquid film pipe in the cloth liquid hole, and it has the heat medium heating pipe to peg graft in the intraductal chamber of falling liquid film, and barrel upper portion outer wall is equipped with polymerization ware feed inlet and evacuation mouth, and the bottom of polymerization ware is equipped with ejection of compact spiral and polymer discharge gate, and the barrel inner wall is equipped with cyclic annular liquid tank with the corresponding position of polymerization ware feed inlet, and liquid tank's lower extreme leaves even cyclic annular gap, the lower part inner wall of barrel is equipped with the collecting tank, be equipped with on the barrel outer wall with collecting tank fuse -element export in the middle of communicating, the export of middle fuse -element is located the top of cloth liquid dish through middle melt -conveying pump and middle fuse -element access connection, middle fuse -element import. This two cauldron systems of polymerization esterify compact structure, area is little, and production efficiency is high.

Description

A kind of fat polymerization two still system

Technical field

This utility model relates to a kind of fat polymerization two still system, belongs to polyester producing process field.

Background technology

In prior art, esterification and polycondensation reaction during production of polyester are typically carried out in separate reaction tower or reactor, Chinese utility model patent such as Publication No. CN101618304B, disclose a kind of esterifier, it is made up of polylith column plate, all installing a downspout and a riser on every block of column plate, riser connects rotatable gas distributor, and gas distributor is made up of air entraining pipe, fan blades and nozzle.Every block of column plate all retains the liquid of certain liquid level, has solid catalyst in liquid.Liquid phase is the component containing carboxylic acid, in the reactor downwards by one block of esterification column plate current to next block column plate, react with the alcohol steam counter-flow risen.

The Chinese utility model patent of Publication No. CN2741645, disclose a kind of polycondensation reaction tower in polycondensation reaction device field, including the double Shell being made up of inner housing and shell body, it it is chuck between inner housing and shell body, the heating agent being communicated with chuck on shell body enters, outlet, the steam outlet port of inner housing inner chamber it is communicated with on double Shell, charging aperture and discharging opening, described double Shell is uprightly arranged, charging aperture is arranged at double Shell top and stretches in inner housing, discharging opening is arranged at the bottom of double Shell, some horizontally disposed tower trays it are provided with between charging aperture and discharging opening, described tower tray includes housing, some material leakage passages it are provided with in housing.Esterification and polycondensation reaction are divided into two reactors and carry out traditionally, and structure is the compactest, and floor space is big, and production efficiency is low.

Traditional polymer reactor includes the cylinder of vertical setting and closed at both ends, the top of polymer reactor inner chamber is provided with horizontal material distribution plate, material distribution plate is provided with material distribution hopper, material distribution hopper is provided with film supplying tube and the gap uniformity between the two of closed at both ends, film supplying tube extends straight down and upper end is stretched out outside the top of polymer reactor, the inner chamber of film supplying tube is provided with heating medium for heating pipe, the external wall of upper portion of polymer reactor is provided with polymer reactor charging aperture and vacuum orifice, the conical lower portion of polymer reactor is provided with polymer discharge mouth, the periphery of polymer reactor is provided with heating jacket.

After PET melt enters polymer reactor inner chamber, fall on material distribution plate, the gap between material distribution hopper and film supplying tube from material distribution plate flows downward out, outer wall at film supplying tube forms wall built-up falling liquid film, in film supplying tube under the heating of thermal medium, after melt completes polymerization, fall bottom polymer reactor, then the polymer discharge mouth bottom polymer reactor flows out.In course of reaction, pumped vacuum systems keeps vacuum state in making polymer reactor by vacuum orifice.

After PET melt enters polymer reactor inner chamber, the Area comparison heated is little, and only carries out a polyreaction, and response speed is slow, and production efficiency is low；The little molecule that reaction produces, easily in still wall carbonization, falls in the middle of material, produces stain material, it is often necessary to stopping and wash still, unstable product quality, cycle of operation is short.

Utility model content

The purpose of this utility model is, overcomes problems of the prior art, it is provided that a kind of fat polymerization two still system, compact conformation, and production efficiency is high.

nullFor solving above technical problem，A kind of fat polymerization two still system of the present utility model，Including esterification Prepolycondensating reactor with without stirring polymer reactor，Described esterification Prepolycondensating reactor is provided with material inlet and precondensation discharging opening，Described nothing stirring polymer reactor is provided with polymer reactor charging aperture and polymer discharge mouth，Described precondensation discharging opening is connected with precondensation discharge nozzle by precondensation fluid level control valve or precondensation melt delivery pump，Described precondensation discharge nozzle is connected with described polymer reactor charging aperture，The described cylinder including vertical setting and closed at both ends without stirring polymer reactor，The top of cylinder lumen is provided with cloth liquid dish that is horizontal and that laterally cut off by cylinder，Described cloth liquid dish is provided with up big and down small liquid distributing hole，Described liquid distributing hole is provided with film supplying tube and both coaxial lines，Described film supplying tube extends straight down，The inner chamber of described film supplying tube is plugged with polymer reactor heating medium for heating pipe，The external wall of upper portion of described cylinder is provided with polymer reactor vacuum orifice and described polymer reactor charging aperture，The lower end of described cylinder is provided with conical head，The lower end of described conical head is provided with discharging spiral，Described polymer discharge mouth is positioned at the lower end of described discharging spiral；The periphery of described cylinder is provided with polymer reactor chuck, the periphery of described conical head is provided with conical head chuck, described polymer reactor charging aperture is positioned at the lower section of described cloth liquid dish, the inwall of described cylinder is provided with ring-type cloth liquid bath with the described corresponding position of polymer reactor charging aperture, leaves uniform annular slot between lower end and the cylinder inboard wall of described cloth liquid bath；The lower inner wall of described cylinder is provided with ring-type collecting tank, the upper end open of described collecting tank and lower end closed；The outer wall of described cylinder is provided with the middle melt outlet communicated with the bottom of described collecting tank, described middle melt outlet is connected with the entrance of middle melt delivery pump, described middle melt conveying delivery side of pump is connected with middle melt inlet, and described middle melt inlet is positioned on cylinder body outer wall and is positioned at the top of described cloth liquid dish.

Relative to prior art, this utility model achieves following beneficial effect: when using precondensation fluid level control valve, and precondensation melt enters polymer reactor charging aperture by potential difference；When using precondensation melt delivery pump, precondensation melt delivery pump carry to polymer reactor charging aperture.nullPrecondensation melt enters cloth liquid bath from polymer reactor charging aperture，It is uniformly distributed on the circumference of cylinder inboard wall with cloth liquid bath，Then the annular slot from cloth liquid bath lower end flows out，Cylinder inboard wall is formed uniform falling liquid film，In flow process，In chuck under the heating of heating agent，Melt intensification is able to prepolymerization and becomes melt in the middle of prepolymerization，Then flow in the collecting tank of cylinder inboard wall bottom，Then flow out from middle melt outlet，The middle melt inlet on polymer reactor top is sent into again by middle melt delivery pump，After middle melt inlet enters polymer reactor inner chamber，Fall on cloth liquid dish，The gap between liquid distributing hole and film supplying tube from cloth liquid dish flows downward out，Outer wall at film supplying tube forms wall built-up falling liquid film again，In film supplying tube under the heating of thermal medium，In the middle of prepolymerization, melt has been polymerized further，Polymer discharge mouth bottom polymer reactor flows out.This polymer reactor uses without stirring structure, power consumption and failure rate is low；Using ring-type cloth liquid bath cloth liquid at polymer reactor inner chamber, the falling liquid film of formation is uniform, and has carried out twice polymerization at polymer reactor inner chamber, improves reaction efficiency；During reaction and discharging, being bled by polymer reactor vacuum orifice, polymer reactor inner chamber remains at vacuum state, does not results in melt degraded, product with stable quality.

As improvement of the present utility model, described cloth liquid dish be arranged over film supplying tube dividing plate, described film supplying tube dividing plate be arranged over polymer reactor heating medium for heating pipe dividing plate, cylinder is laterally cut off by described film supplying tube dividing plate and described polymer reactor heating medium for heating pipe dividing plate respectively, described polymer reactor heating medium for heating pipe dividing plate be arranged over polymer reactor upper cover；The upper port of described film supplying tube is connected on the pore of described film supplying tube dividing plate, and the upper port of described polymer reactor heating medium for heating pipe is connected on the pore of described polymer reactor heating medium for heating pipe dividing plate；Connecting on described polymer reactor upper cover and have film supplying tube Heating medium, the barrel wall between described film supplying tube dividing plate with polymer reactor heating medium for heating pipe dividing plate is connected has film supplying tube heating agent to export.Thermal medium such as conduction oil enters the oil suction chamber between polymer reactor upper cover and polymer reactor heating medium for heating pipe dividing plate from film supplying tube Heating medium, then arrive bottom polymer reactor heating medium for heating pipe along polymer reactor heating medium for heating pipe is directly lower, it is upwardly into the ring cavity between film supplying tube and polymer reactor heating medium for heating pipe after flowing out polymer reactor heating medium for heating pipe, up along this ring cavity, enter from the upper port of film supplying tube and go out oil pocket between film supplying tube dividing plate and polymer reactor heating medium for heating pipe dividing plate, finally flow out from the outlet of film supplying tube heating agent.When material has just enter into liquid distributing hole, temperature is relatively low, forms falling liquid film tailing edge film supplying tube and flows downward, is constantly heated by heating agent in film supplying tube, and temperature gradually rises, and when arriving bottom film supplying tube, the temperature of material reaches the highest.The highest heating agent of temperature first under to bottom film supplying tube because the heating agent that periphery is return of polymer reactor heating medium for heating pipe, temperature is higher, and the heating agent thermal loss descending along polymer reactor heating medium for heating pipe is the least；The up heating agent of return is owing to constantly carrying out heat release to material falling liquid film, and temperature is gradually reduced.Therefore the temperature of the outer material of film supplying tube is the most gradually incremented by, heat medium temperature in film supplying tube the most gradually successively decreases, material that temperature the is minimum heating agent relatively low with temperature carries out heat exchange, the heating agent that the highest material of temperature is the highest with temperature carries out heat exchange, heat exchange both sides remain the bigger temperature difference, and heat exchange efficiency is high.

As further improvement of the utility model, described cylinder inboard wall is provided with the barrel material distribution ring that downward spiral extends, the upper end of described barrel material distribution ring is positioned at below the outlet of described cloth liquid bath, the lower end of described barrel material distribution ring is positioned at above the upper port of described collecting tank, and described barrel material distribution ring is semi-circular cross-section and plane is connected on described cylinder inboard wall.The melt annular slot from cloth liquid bath lower end flows out, after flow downward formation falling liquid film along cylinder inboard wall, need to cross the barrel material distribution ring of multiple tracks semi-circular cross-section, being blocked when crossing barrel material distribution ring, the falling liquid film thickness making the whole circumferencial direction of cylinder inboard wall and short transverse is more uniform；Semi-circular cross-section smooth surface makes melt flows highly uniform gently, the most there is not material dead angle, it is to avoid it is overheated that material stagnation causes.

As further improvement of the utility model, the film supplying tube outer wall below described liquid distributing hole is uniformly provided with at least one film supplying tube material distribution ring, and the cross section of described film supplying tube material distribution ring is the little cydariform broad in the middle in two.Gap between middle melt liquid distributing hole and film supplying tube from cloth liquid dish flows downward out, after the outer wall of film supplying tube forms wall built-up falling liquid film again, during flowing downward, need to cross the film supplying tube material distribution ring of multiple tracks cydariform, being blocked when crossing film supplying tube material distribution ring, the falling liquid film thickness making the whole circumferencial direction of film supplying tube outer wall and short transverse is more uniform；The smooth surface arc-shaped transition of film supplying tube material distribution ring makes melt flows highly uniform gently, the most there is not material dead angle, it is to avoid it is overheated that material stagnation causes.

As further improvement of the utility model, described esterification Prepolycondensating reactor includes the vertical tower body closed, it is separated into room under the upper room of esterification and precondensation by arc-shaped partition in described vertical column body, in described esterification, the barrel of room is externally provided with esterification heating jacket, and under described precondensation, the barrel of room is externally provided with precondensation heating jacket；In described esterification, the top of room is provided with the upper room gaseous phase outlet of esterification and described material inlet, and the bottom centre of described arc-shaped partition is provided with nitrogen inlet, and in described esterification, the sidewall of room is provided with esterification material outlet；Under described precondensation, the bottom of room connects esterification material preheater, it is provided with preheater charging aperture bottom the low head of described esterification material preheater, described esterification material outlet is connected with described preheater charging aperture with carboxylate discharge nozzle by esterifying liquid level control valve, connecting on described carboxylate discharge nozzle has auxiliary agent import, the preheater discharging opening of described esterification material preheater upper end to be connected with the bottom inlet of room under described precondensation；Under described precondensation, the inner chamber of room is provided with multilamellar tower tray from bottom to top, and described precondensation discharging opening is positioned on the top barrel of room under described precondensation, described precondensation discharging opening be arranged over room vacuum orifice under precondensation.Room esterification is entered from material inlet after PTA powder and ethylene glycol mixing making beating, nitrogen nitrogen inlet bottom arc-shaped partition enters room esterification, it is stirred material making its mix homogeneously, in esterification under the hot environment of room, PTA powder and ethylene glycol generation esterification, in esterification, the operating pressure of room is 0.5～2bar(gauge pressure), the gaseous substance that esterification produces room gaseous phase outlet from esterification is discharged, esterification material is discharged from esterification material outlet, carboxylate discharge nozzle is entered by esterifying liquid level control valve, auxiliary agent is added in carboxylate discharge nozzle by auxiliary agent import；Under the effect of potential difference and pressure reduction, esterification material and auxiliary agent enter preheater charging aperture, and in esterification material preheater, in auxiliary agent, the ethylene glycol gasification of excess produces bubble, and bubble from bottom to top moves to material with motive force, simultaneously works as stirring action；It is upwardly into room under precondensation after esterification material is heated, proceeds partial esterification reaction, simultaneously enter polycondensation process；Under precondensation, under the precondensation of room, room vacuum orifice is positioned at topmost, more the highest toward upper strata vacuum, under precondensation, the vacuum in ceiling portion is 1～10kpa(absolute pressure), material progressively carries out polyreaction when through tower tray layer by layer, make material degree of polymerization during from bottom to top incrementally increase, finally discharge from precondensation discharging opening.Esterification room and precondensation room are connected as a single entity by this reactor, compact conformation, and floor space is little, heat loss is few, it is not necessary to extra power material can flow to room under precondensation, mechanical agitating device in room from esterification, save energy consumption, reduced fault rate, improve production efficiency.

As further improvement of the utility model, in described esterification, the bottom centre of room is provided with the cyclone agitator disk being horizontally disposed with and being centrosymmetric, described cyclone agitator disk is hollow cylinder plate, the bottom centre of described cyclone agitator disk is connected with described nitrogen inlet, multiple nitrogen jet mouth it is evenly distributed with in the circumferential wall of described cyclone agitator disk, the outside of each described nitrogen jet mouth is respectively equipped with the nitrogen water conservancy diversion arc making nitrogen tangentially penetrate, and the root of each described nitrogen water conservancy diversion arc is connected in the circumferential wall of described cyclone agitator disk.Nitrogen enters the inner chamber of cyclone agitator disk from the bottom centre of cyclone agitator disk, spray from each nitrogen jet mouth, water conservancy diversion through nitrogen water conservancy diversion arc, nitrogen all penetrates along the tangential direction of nitrogen water conservancy diversion arc tip circle everywhere, in esterification, horizontal vortex is formed on the bottom of room, fully material can be stirred, also to move upward after nitrogen injection and material is formed secondary stirring, it is ensured that material is thoroughly mixed uniformly.

As further improvement of the utility model, in described esterification, the inner wall lower of room is provided with circumferentially and the external flow guiding cylinder of upper end open, esterification discharging annular groove is formed between described external flow guiding cylinder and the upper chamber interior walls of esterification, described external flow guiding cylinder is provided with external flow guiding cylinder material outlet and communicates with described esterification discharging annular groove, and described esterification material outlet communicates with the bottom of described esterification discharging annular groove；The inner chamber of described external flow guiding cylinder is provided with the inner draft tube of line coaxially therewith, and the annular section between described inner draft tube and described external flow guiding cylinder is positioned at above the excircle of described cyclone agitator disk, and the upper port of described inner draft tube is less than the upper port of external flow guiding cylinder；In described esterification, the inner chamber of room is provided with and extends downward the center material pipe in the middle part of inner draft tube along axis, and the upper end of described center material pipe is connected with described material inlet；Between described external flow guiding cylinder and inner draft tube, annulus is provided with many group esterification heating coils, and often group heating medium for heating coil pipe is respectively equipped with esterification heating coil Heating medium and esterification heating coil heating agent outlet.The nitrogen of cyclone agitator disk injection makes in esterification the material bottom room form strong circulation, and under the thermal convection current dual function of nitrogen and heating coil, material moves upward along the annulus between inner draft tube and external flow guiding cylinder；Material within inner draft tube flows downward, and forms the state of inside and outside stream circulation, and new material, after the lower port of center material pipe flows downward out, is i.e. involved in stream circulation and is stirred；At high temperature PTA powder and ethylene glycol generation esterification, along with new material constantly enters, the material reacted enters esterification discharging annular groove from the external flow guiding cylinder material outlet of external flow guiding cylinder, continuing reaction thoroughly during flowing under the heating of heating agent in esterification heating jacket, finally the esterification material outlet bottom esterification discharging annular groove is discharged.PTA powder and ethylene glycol between external flow guiding cylinder and inner draft tube in annulus while stirring, esterified still heating coil heats, and can need, according to technique, the group number of esterifying kettle heating coil that determines to put into heating.

As further improvement of the utility model, described external flow guiding cylinder material outlet extends vertically downwards along the short transverse of described external flow guiding cylinder, the inner chamber room of being provided with of described esterification discharging annular groove radially diaphragm, described external flow guiding cylinder material outlet and described esterification material outlet lay respectively at the both sides of described upper room radially diaphragm；Top tray be arranged over discharging annular groove in room under precondensation, under described precondensation, the bottom of room discharging annular groove is connected under described precondensation on the barrel of room, under described precondensation, room discharging annular groove is provided with flash mouth in room under vertically extending precondensation, described precondensation discharging opening communicates with the bottom of room discharging annular groove under described precondensation, under described precondensation, the inner chamber of room discharging annular groove is provided with room radially diaphragm under precondensation, and under described precondensation, room flash mouth and described precondensation discharging opening lay respectively at the both sides of room radially diaphragm under described precondensation.Esterification material outlet is separated by upper room radially diaphragm with external flow guiding cylinder material outlet, it is possible to prevent the material being esterified in discharging annular groove that short stream occurs, material is made to have the stroke of maximum in esterification discharging annular groove, material enters form in laminar flow after esterification discharging annular groove, along tower body inner wall surrounding one week, material advance during continue esterified heating jacket heating, finally from esterification material outlet flow out, this structure extend material esterification discharging annular groove in heat time heating time.Under precondensation, flash mouth in room under precondensation is separated by room radially diaphragm with precondensation discharging opening, there is short stream in the material being possible to prevent under precondensation in room discharging annular groove, make material that discharging annular groove in room to have under precondensation the stroke of maximum, material enters under precondensation the form after room discharging annular groove in laminar flow, along tower body inner wall surrounding one week, material continues to be heated by precondensation heating jacket during advancing, finally flowing out from precondensation discharging opening, this structure extends material heat time heating time under precondensation in room discharging annular groove.

As further improvement of the utility model, the material tedge of multiple through tower tray it is respectively uniformly distributed on the described tower tray of each layer, the top of each described material tedge is covered each by the material deflector cup of line coaxially therewith, each described material deflector cup is fornix shape and lower port is connected on described tower tray, and the lower circumference of each described material deflector cup is uniformly provided with deflector cup discharging opening.Material is advanced into the inner chamber of material deflector cup from material tedge, and then the baffling deflector cup discharging opening from material deflector cup lower circumference downwards flows out.Due to the swabbing action of room vacuum orifice and the polycondensation process of material under top, room precondensation under precondensation, air cavity is formed at the top of each layer of material deflector cup, vacuum in last layer material deflector cup air cavity is the highest, the most down the vacuum in material deflector cup air cavity is progressively successively decreased, material progressively carries out polyreaction during from bottom to top passing sequentially through each layer tower tray and material deflector cup, and material degree of polymerization during from bottom to top incrementally increases.

As further improvement of the utility model, under described precondensation room discharging annular groove be arranged over foam trapping dish, described foam trapping dish is horizontally set under described precondensation on the cross section of room and is positioned at the lower section of room vacuum orifice under described precondensation；The low head inner chamber of described esterification material preheater is respectively equipped with horizontally disposed material distribution plate, and described material distribution plate is evenly distributed with multiple material dispensing orifice.Polymerization process can produce a large amount of bubble, foam trapping dish can stop the bubble of room under precondensation enter above precondensation under room vacuum meter interface under room vacuum orifice and precondensation.Esterification material and auxiliary agent, after numerous material dispensing orifices of material distribution plate, can more uniformly enter each heat exchanging pipe of top.

Accompanying drawing explanation

Being described in further detail this utility model with detailed description of the invention below in conjunction with the accompanying drawings, accompanying drawing only provides reference and explanation use, is not used to limit this utility model.

Fig. 1 is the schematic diagram of this utility model fat polymerization two still the first embodiment of system.

Fig. 2 is the schematic diagram of this utility model fat polymerization two still system the second embodiment.

Fig. 3 is the structural representation of this utility model polymer reactor.

Fig. 4 is the enlarged drawing of aminoacyl site in Fig. 3.

Fig. 5 is the structural representation being esterified Prepolycondensating reactor in Fig. 1.

Fig. 6 is the flow direction of material figure being esterified discharging annular groove in Fig. 5.

Fig. 7 is the sectional view of cyclone agitator disk in Fig. 5.

Fig. 8 is the structural representation of material distribution plate in Fig. 5.

Fig. 9 is the enlarged drawing at B position in Fig. 5.

Figure 10 is the flow direction of material figure of room discharging annular groove under precondensation in Fig. 5.

In figure: 1. the upper room of esterification；1a. material inlet；Room gaseous phase outlet in 1b. esterification；1c. nitrogen inlet；1d. external flow guiding cylinder；1d1. external flow guiding cylinder material outlet；1e. is esterified discharging annular groove；The upper room of 1e1. radially diaphragm；1f. is esterified material outlet；1g. inner draft tube；1h. cyclone agitator disk；1h1. nitrogen jet mouth；1h2. nitrogen water conservancy diversion arc；Room interface of the level gauge in 1j. esterification；Chamber pressure table interface in 1k. esterification；Room Heating medium in 1m. esterification；Heating agent outlet in room in 1n. esterification；1p. is esterified heating coil.

2. room under precondensation；2a. tower tray；2a1. material tedge；2a2. material deflector cup；2a3. deflector cup discharging opening；Discharging annular groove in room under 2b. precondensation；Flash mouth in room under 2b1. precondensation；Room radially diaphragm under 2b2. precondensation；2c. precondensation discharging opening；2d. foam trapping dish；Room vacuum orifice under 2e. precondensation；Room interface of the level gauge under 2f. precondensation；Vacuum meter interface in room under 2g. precondensation；Room Heating medium under 2h. precondensation；Heating agent outlet in room under 2j. precondensation.

3. esterification material preheater；3a. preheater charging aperture；3b. preheater discharging opening；3c. preheater Heating medium；3d. preheater heating agent exports；3e. material distribution plate；3e1. material dispensing orifice.

B1. precondensation melt delivery pump；G1. carboxylate discharge nozzle；G1a. auxiliary agent import；G2. precondensation discharge nozzle；V1. esterifying liquid level control valve；V2. precondensation fluid level control valve.

4. without stirring polymer reactor；401a. polymer reactor charging aperture；401b. polymer reactor vacuum orifice；Melt inlet in the middle of 401c.；Melt outlet in the middle of 401d.；401e. polymer reactor heating medium for heating pipe dividing plate；401f. film supplying tube dividing plate；402. cloth liquid dishes；402a. liquid distributing hole；403. film supplying tube；403a. film supplying tube material distribution ring；404. cloth liquid baths；405. collecting tank；406. middle melt delivery pumps；407. polymer reactor chucks；407a. polymer reactor chuck Heating medium；407b. polymer reactor chuck heating agent exports；408a. film supplying tube Heating medium；408b. film supplying tube heating agent exports；409a. conical head chuck Heating medium；409b. conical head chuck heating agent exports；410. discharging spirals；410a. polymer discharge mouth；411. polymer reactor heating medium for heating pipes；412. barrel material distribution ring；413. collecting tank interface of the level gauge；414. conical head interface of the level gauge.

Detailed description of the invention

Shown in Fig. 1, fat polymerization two still system of the present utility model includes being esterified Prepolycondensating reactor and without stirring polymer reactor 4, esterification Prepolycondensating reactor is provided with material inlet 1a and precondensation discharging opening 2c, it is provided with polymer reactor charging aperture 401a and polymer discharge mouth 410a without stirring polymer reactor 4, precondensation discharging opening 2c is connected with precondensation discharge nozzle G2 by precondensation fluid level control valve V2, and precondensation discharge nozzle G2 is connected with polymer reactor charging aperture 401a.

Shown in Fig. 2, fat polymerization two still system of the present utility model includes being esterified Prepolycondensating reactor and without stirring polymer reactor 4, esterification Prepolycondensating reactor is provided with material inlet 1a and precondensation discharging opening 2c, it is provided with polymer reactor charging aperture 401a and polymer discharge mouth 410a without stirring polymer reactor 4, precondensation discharging opening 2c is connected with precondensation discharge nozzle G2 by precondensation melt delivery pump B1, and precondensation discharge nozzle G2 is connected with polymer reactor charging aperture 401a.

As shown in Figure 3 and Figure 4, the cylinder of vertical setting and closed at both ends is included without stirring polymer reactor 4, the top of cylinder lumen is provided with cloth liquid dish 402 that is horizontal and that laterally cut off by cylinder, and cloth liquid dish 402 is provided with liquid distributing hole 402a, is provided with film supplying tube 403 and both coaxial lines in liquid distributing hole 402a.Liquid distributing hole 402a is up big and down small infundibulate, it is simple to enough materials flow in liquid distributing hole 402a, the thickness of the clearance control falling liquid film of the small end of liquid distributing hole 402a and film supplying tube 403.Film supplying tube 403 extends straight down, the inner chamber of film supplying tube 403 is plugged with polymer reactor heating medium for heating pipe 411, cylinder external wall of upper portion without stirring polymer reactor 4 is provided with polymer reactor charging aperture 401a and polymer reactor vacuum orifice 401b, lower end without stirring polymer reactor 4 is provided with conical head, the lower end of conical head is provided with discharging spiral 410, and the lower end of discharging spiral 410 is provided with polymer discharge mouth 410a.

Cylinder periphery without stirring polymer reactor 4 is provided with polymer reactor chuck 407, and the bottom of polymer reactor chuck 407 is provided with polymer reactor chuck Heating medium 407a, and the top of polymer reactor chuck 407 is provided with polymer reactor chuck heating agent outlet 407b.Heating agent enters in polymer reactor chuck 407 from polymer reactor chuck Heating medium 407a, then flows out from polymer reactor chuck heating agent outlet 407b.

The periphery of conical head is provided with conical head chuck, and the bottom of conical head chuck is provided with conical head chuck Heating medium 409a, and the top of conical head chuck is provided with conical head chuck heating agent outlet 409b.Heating agent enters in conical head chuck from conical head chuck Heating medium 409a, then flows out from conical head chuck heating agent outlet 409b.

Polymer reactor charging aperture 401a is positioned at the lower section of cloth liquid dish 402, cylinder inboard wall without stirring polymer reactor 4 is provided with ring-type cloth liquid bath 404 with the corresponding position of polymer reactor charging aperture 401a, leaves uniform annular slot between lower end and the cylinder inboard wall of cloth liquid bath 404；Lower inner wall without stirring polymer reactor 4 is provided with ring-type collecting tank 405, the upper end open of collecting tank 405 and lower end closed；Outer wall without stirring polymer reactor 4 is provided with the middle melt outlet 401d communicated with the bottom of collecting tank 405, middle melt outlet 401d is connected with the entrance of middle melt delivery pump 406, the outlet of middle melt delivery pump 406 is connected with middle melt inlet 401c, and middle melt inlet 401c is positioned on cylinder body outer wall and is positioned at the top of cloth liquid dish 402.

Middle melt outlet 401d and middle melt inlet 401c can be evenly arranged with one group, two groups or more than three groups on the circumference without stirring polymer reactor 4.

Can be provided with multiple liquid distributing hole 402a on cloth liquid dish 402, the center of each liquid distributing hole 402a is respectively equipped with film supplying tube 403.Film supplying tube 403 is at least provided with one group, and often group is equipped with polymer reactor heating medium for heating pipe 411.

Cloth liquid dish 402 be arranged over film supplying tube dividing plate 401f, film supplying tube dividing plate 401f is arranged over polymer reactor heating medium for heating pipe dividing plate 401e, cylinder is laterally cut off by polymer reactor heating medium for heating pipe dividing plate 401e and film supplying tube dividing plate 401f respectively, and polymer reactor heating medium for heating pipe dividing plate 401e is arranged over polymer reactor upper cover；The upper port of film supplying tube 403 is connected on the pore of film supplying tube dividing plate 401f, and the upper port of polymer reactor heating medium for heating pipe 411 is connected on the pore of polymer reactor heating medium for heating pipe dividing plate 401e；Connecting on polymer reactor upper cover to have on the barrel wall between film supplying tube Heating medium 408a, film supplying tube dividing plate 401f with polymer reactor heating medium for heating pipe dividing plate 401e to be connected has film supplying tube heating agent to export 408b.

Polymer reactor vacuum orifice 401b is positioned at the lower section of cloth liquid dish 402, during reaction and discharging, is bled by polymer reactor vacuum orifice 401b, and polymer reactor inner chamber remains at vacuum state.

Position corresponding with the lower end of collecting tank 405 on polymer reactor is provided with collecting tank interface of the level gauge 413, and the lower end of conical head is provided with conical head interface of the level gauge 414, in order to control the liquid level of polymer reactor materials inside.

nullMelt enters cloth liquid bath 404 from polymer reactor charging aperture 401a，It is uniformly distributed on the circumference of cylinder inboard wall with cloth liquid bath 404，Then the annular slot from cloth liquid bath 404 lower end flows out，Cylinder inboard wall is formed uniform falling liquid film，In flow process，In polymer reactor chuck under the heating of heating agent，Melt intensification is able to prepolymerization and becomes melt in the middle of prepolymerization，Then flow in the collecting tank 405 of cylinder inboard wall bottom，Then flow out from middle melt outlet 401d，The middle melt inlet 401c on polymer reactor top is sent into again by middle melt delivery pump 406，After middle melt inlet 401c enters polymer reactor inner chamber，Fall on cloth liquid dish 402，The gap between liquid distributing hole 402a and film supplying tube 403 from cloth liquid dish 402 flows downward out，Outer wall at film supplying tube 403 forms wall built-up falling liquid film again，In film supplying tube 403 under the heating again of thermal medium，In the middle of prepolymerization, melt has been polymerized further，Conical head bottom polymer reactor enters discharging spiral 410，Polymer discharge mouth 410a from discharging spiral 410 lower end discharges again.The esterification yield of polymer discharge mouth 410a is more than 99%, and the degree of polymerization is more than 100.

Thermal medium such as conduction oil enters the oil suction chamber between polymer reactor upper cover and polymer reactor heating medium for heating pipe dividing plate 401e from film supplying tube Heating medium 408a, then arrive bottom polymer reactor heating medium for heating pipe 411 along polymer reactor heating medium for heating pipe 411 is directly lower, it is upwardly into the ring cavity between film supplying tube 403 and polymer reactor heating medium for heating pipe 411 after flowing out polymer reactor heating medium for heating pipe 411, up along this ring cavity, enter from the upper port of film supplying tube 403 and go out oil pocket between film supplying tube dividing plate 401f and polymer reactor heating medium for heating pipe dividing plate 401e, finally flow out from film supplying tube heating agent outlet 408b.

When material has just enter into liquid distributing hole 402a, temperature is relatively low, forms falling liquid film tailing edge film supplying tube 403 and flows downward, is constantly heated by heating agent in film supplying tube 403, and temperature continues to raise, and when arriving bottom film supplying tube 403, the temperature of material reaches the highest.And the highest heating agent of temperature is first lower bottom film supplying tube 403, because the heating agent that periphery is return of polymer reactor heating medium for heating pipe 411, temperature is higher, and the heating agent thermal loss descending along polymer reactor heating medium for heating pipe 411 is the least；The up heating agent of return is owing to constantly carrying out heat release to material falling liquid film, and temperature is gradually reduced.Therefore the temperature of the outer material of film supplying tube is the most gradually incremented by, heat medium temperature in film supplying tube the most gradually successively decreases, the relatively low material of the temperature heating agent relatively low with temperature carries out heat exchange, the heating agent that the highest material of temperature is the highest with temperature carries out heat exchange, heat exchange both sides remain the bigger temperature difference, and heat exchange efficiency is high.This polymer reactor uses ring-type cloth liquid bath 404 cloth liquid at polymer reactor inner chamber, at film supplying tube 403 outer employing liquid distributing hole 402a cloth liquid, the falling liquid film of formation is the most visibly homogeneous, and has carried out twice polymerization at polymer reactor inner chamber, increase heat exchange area, improve reaction efficiency.

Cylinder inboard wall is provided with the barrel material distribution ring 412 that downward spiral extends, the upper end of barrel material distribution ring 412 is positioned at below the outlet of cloth liquid bath 404, the lower end of barrel material distribution ring 412 is positioned at above the upper port of collecting tank 405, and barrel material distribution ring 412 is connected on cylinder inboard wall for semi-circular cross-section and plane.The melt annular slot from cloth liquid bath 404 lower end flows out, after flow downward formation falling liquid film along cylinder inboard wall, need to cross the barrel material distribution ring 412 of multiple tracks semi-circular cross-section, being blocked when crossing barrel material distribution ring 412, the falling liquid film thickness making the whole circumferencial direction of cylinder inboard wall and short transverse is more uniform；Semi-circular cross-section smooth surface makes melt flows highly uniform gently, the most there is not material dead angle, it is to avoid it is overheated that material stagnation causes.

Film supplying tube 403 outer wall below liquid distributing hole is uniformly provided with at least one film supplying tube material distribution ring 403a, and the cross section of film supplying tube material distribution ring 403a is the little cydariform broad in the middle in two.Gap between middle melt liquid distributing hole and film supplying tube 403 from cloth liquid dish 402 flows downward out, after the outer wall of film supplying tube 403 forms wall built-up falling liquid film again, during flowing downward, need to cross film supplying tube material distribution ring 403a of multiple tracks cydariform, being blocked when crossing film supplying tube material distribution ring 403a, the falling liquid film thickness making the whole circumferencial direction of film supplying tube outer wall and short transverse is more uniform；The smooth surface arc-shaped transition of film supplying tube material distribution ring 403a makes melt flows highly uniform gently, the most there is not material dead angle, it is to avoid it is overheated that material stagnation causes.

As shown in Fig. 5 to Figure 10, esterification Prepolycondensating reactor includes the vertical tower body closed, being separated into room 2 under the upper room 1 of esterification and precondensation by arc-shaped partition in vertical column body, in esterification, the barrel of room 1 is externally provided with esterification heating jacket, and under precondensation, the barrel of room 2 is externally provided with precondensation heating jacket；In esterification, the top of room 1 is provided with material inlet 1a and the upper room gaseous phase outlet 1b of esterification, and the bottom centre of arc-shaped partition is provided with nitrogen inlet 1c, and in esterification, the sidewall of room 1 is provided with esterification material outlet 1f, and in esterification, the top of room 1 is provided with the upper chamber pressure table interface 1k of esterification.

Under precondensation, the bottom of room 2 connects esterification material preheater 3, it is provided with preheater charging aperture 3a bottom the low head of esterification material preheater 3, esterification material outlet 1f is connected with carboxylate discharge nozzle G1 by esterifying liquid level control valve V1 or precondensation melt delivery pump B1, carboxylate discharge nozzle G1 is connected with preheater charging aperture 3a, on carboxylate discharge nozzle G1, connection has auxiliary agent import G1a, the preheater discharging opening 3b of esterification material preheater 3 upper end to be connected with the bottom inlet of room under precondensation 2.

Under precondensation, the inner chamber of room 2 is provided with multilamellar tower tray 2a from bottom to top, under precondensation, the top barrel of room 2 is provided with precondensation discharging opening 2c, precondensation discharging opening 2c is connected with precondensation discharge nozzle G2 by precondensation fluid level control valve V2 or precondensation melt delivery pump B1, and precondensation discharging opening 2c is arranged under precondensation room vacuum meter interface 2g under room vacuum orifice 2e and precondensation.

Room 1 esterification is entered from material inlet 1a after PTA powder and ethylene glycol mixing making beating, nitrogen nitrogen inlet 1c bottom arc-shaped partition enters room 1 esterification, it is stirred material making its mix homogeneously, in esterification under the hot environment of room 1, PTA powder and ethylene glycol generation esterification, in esterification, the operating pressure of room 1 is 0.5～2bar(gauge pressure), the gaseous substance that esterification produces room gaseous phase outlet 1b from esterification discharges, esterification material is discharged from esterification material outlet 1f, carboxylate discharge nozzle G1 is entered by esterifying liquid level control valve V1, auxiliary agent is added in carboxylate discharge nozzle G1 by auxiliary agent import G1a.Under the effect of potential difference and pressure reduction, esterification material and auxiliary agent enter preheater charging aperture 3a, and in esterification material preheater 3, in auxiliary agent, the ethylene glycol gasification of excess produces bubble, and bubble from bottom to top moves to material with motive force, simultaneously works as stirring action.It is upwardly into room 2 under precondensation after esterification material is heated, proceeds partial esterification reaction, simultaneously enter polycondensation process.Under precondensation, under the precondensation of room 2, room vacuum orifice 2e is positioned at topmost, more the highest toward upper strata vacuum, under precondensation, the vacuum in ceiling portion is 1～10kpa(absolute pressure), material progressively carries out polyreaction when through tower tray layer by layer, make material degree of polymerization during from bottom to top incrementally increase, finally discharge from precondensation discharging opening 2c.

In esterification, the bottom centre of room 1 is provided with the cyclone agitator disk 1h being horizontally disposed with and being centrosymmetric, cyclone agitator disk 1h is hollow cylinder plate, the bottom centre of cyclone agitator disk 1h is connected with nitrogen inlet 1c, multiple nitrogen jet mouth 1h1 it is evenly distributed with in the circumferential wall of cyclone agitator disk 1h, the outside of each nitrogen jet mouth 1h1 is respectively equipped with the nitrogen water conservancy diversion arc 1h2 making nitrogen tangentially penetrate, and the root of each nitrogen water conservancy diversion arc 1h2 is connected in the circumferential wall of cyclone agitator disk 1h.Nitrogen enters the inner chamber of cyclone agitator disk 1h from the bottom centre of cyclone agitator disk 1h, spray from each nitrogen jet mouth 1h1, water conservancy diversion through nitrogen water conservancy diversion arc 1h2, nitrogen all penetrates along the tangential direction of nitrogen water conservancy diversion arc tip circle everywhere, in esterification, horizontal vortex is formed on the bottom of room 1, fully material can be stirred, also to move upward after nitrogen injection and material is formed secondary stirring, it is ensured that material is thoroughly mixed uniformly.

In esterification, the inner wall lower of room 1 is provided with circumferentially and the external flow guiding cylinder 1d of upper end open, esterification discharging annular groove 1e is formed between external flow guiding cylinder 1d and esterification upper room 1 inwall, external flow guiding cylinder 1d is provided with external flow guiding cylinder material outlet 1d1 and communicates with esterification discharging annular groove 1e, and esterification material outlet 1f communicates with the bottom of esterification discharging annular groove 1e；The inner chamber of external flow guiding cylinder 1d is provided with the inner draft tube 1g of line coaxially therewith, and the annular section between inner draft tube 1g and external flow guiding cylinder 1d is positioned at above the excircle of cyclone agitator disk 1h, the upper port of the inner draft tube 1g upper port less than external flow guiding cylinder 1d；In esterification, the inner chamber of room 1 is provided with and extends downward the center material pipe in the middle part of inner draft tube 1g along axis, and the upper end of center material pipe is connected with material inlet 1a.

The nitrogen of cyclone agitator disk 1h injection makes in esterification the material bottom room form strong circulation, and under the thermal convection current dual function of nitrogen and heating coil, material moves upward along the annulus between inner draft tube 1g and external flow guiding cylinder 1d；Material within inner draft tube 1g flows downward, and forms the state of inside and outside stream circulation, and new material, after the lower port of center material pipe flows downward out, is i.e. involved in stream circulation and is stirred；At high temperature PTA powder and ethylene glycol generation esterification, along with new material constantly enters, the material reacted enters esterification discharging annular groove 1e from the external flow guiding cylinder material outlet 1d1 of external flow guiding cylinder 1d, continuing reaction thoroughly during flowing under the heating of heating agent in esterification heating jacket, finally the esterification material outlet 1f bottom esterification discharging annular groove 1e discharges.

Between external flow guiding cylinder 1d and inner draft tube 1g, annulus is provided with many group esterification heating coil 1p, and often group heating medium for heating coil pipe is respectively equipped with esterification heating coil Heating medium and esterification heating coil heating agent outlet.PTA powder and ethylene glycol between external flow guiding cylinder 1d and inner draft tube 1g in annulus while stirring, esterified still heating coil heats, and can need, according to technique, the group number of esterifying kettle heating coil that determines to put into heating.

External flow guiding cylinder material outlet 1d1 extends vertically downwards along the short transverse of external flow guiding cylinder 1d, the inner chamber room of being provided with of esterification discharging annular groove 1e radially diaphragm 1e1, external flow guiding cylinder material outlet 1d1 and the both sides being esterified the material outlet 1f room of laying respectively at radially diaphragm 1e1；Top tray be arranged over discharging annular groove 2b in room under precondensation, under precondensation, the bottom of room discharging annular groove 2b is connected under precondensation on the barrel of room 2, under precondensation, discharging annular groove 2b in room is provided with flash mouth 2b1 in room under vertically extending precondensation, precondensation discharging opening 2c communicates with the bottom of room discharging annular groove 2b under precondensation, under precondensation, the inner chamber of room discharging annular groove 2b is provided with room radially diaphragm 2b2 under precondensation, and under precondensation, room flash mouth 2b1 and precondensation discharging opening 2c lays respectively at the both sides of room radially diaphragm 2b2 under precondensation.

Esterification material outlet 1f is separated by upper room radially diaphragm 1e1 with external flow guiding cylinder material outlet 1d1, it is possible to prevent the material being esterified in discharging annular groove 1e that short stream occurs, material is made to have the stroke of maximum in esterification discharging annular groove 1e, material enters form in laminar flow after esterification discharging annular groove 1e, along tower body inner wall surrounding one week, material continues the heating of esterified heating jacket during advancing, finally flowing out from esterification material outlet 1f, this structure extends material heat time heating time in esterification discharging annular groove 1e.Under precondensation, flash mouth 2b1 in room under precondensation is separated by room radially diaphragm 2b2 with precondensation discharging opening 2c, there is short stream in the material being possible to prevent under precondensation in room discharging annular groove 2b, make material that discharging annular groove 2b in room to have under precondensation the stroke of maximum, material enters under precondensation the form after room discharging annular groove 2b in laminar flow, along tower body inner wall surrounding one week, material continues to be heated by precondensation heating jacket during advancing, finally flowing out from precondensation discharging opening 2c, this structure extends material heat time heating time under precondensation in room discharging annular groove 2b.

Under precondensation, be arranged over the foam trapping dish 2d, foam trapping dish 2d of room discharging annular groove 2b are horizontally set under precondensation on the cross section of room 2 and are positioned at the lower section of room vacuum orifice 2e under precondensation.Polymerization process can produce a large amount of bubble, foam trapping dish 2d can stop the bubble of room 2 under precondensation enter above precondensation under room vacuum meter interface 2g under room vacuum orifice 2e and precondensation.

The material tedge 2a1 of multiple through tower tray it is respectively uniformly distributed on each layer tower tray 2a, the top of each material tedge 2a1 is covered each by the material deflector cup 2a2 of line coaxially therewith, each material deflector cup 2a2 is fornix shape and lower port is connected on tower tray 2a, and the lower circumference of each material deflector cup 2a2 is uniformly provided with deflector cup discharging opening 2a3.Material is advanced into the inner chamber of material deflector cup 2a2 from material tedge 2a1, and then the baffling deflector cup discharging opening 2a3 from material deflector cup 2a2 lower circumference downwards flows out.Due to the swabbing action of room vacuum orifice 2e and the polycondensation process of material under top, room precondensation under precondensation, air cavity is formed at the top of each layer of material deflector cup 2a2, vacuum in last layer material deflector cup air cavity is the highest, the most down the vacuum in material deflector cup air cavity is progressively successively decreased, material progressively carries out polyreaction during from bottom to top passing sequentially through each layer tower tray and material deflector cup 2a2, and material degree of polymerization during from bottom to top incrementally increases.

The low head inner chamber of esterification material preheater 3 is respectively equipped with horizontally disposed material distribution plate 3e, and material distribution plate 3e is evenly distributed with multiple material dispensing orifice 3e1.Esterification material and auxiliary agent, after numerous material dispensing orifice 3e1 of material distribution plate 3e, can more uniformly enter each heat exchanging pipe of top.

In esterification, the barrel of room 1 is provided with the bottom of the upper room interface of the level gauge 1j of esterification and esterification discharging annular groove 1e and communicates, and the aperture of esterifying liquid level control valve V1 is controlled by the liquid level being esterified discharging annular groove 1e；Under precondensation, the barrel of room 2 is provided with interface of the level gauge 2f in room under precondensation and communicates with the bottom of room discharging annular groove 2b under precondensation, the aperture of precondensation fluid level control valve V2 or flow rates controlled liquid level of room discharging annular groove 2b under precondensation of precondensation melt delivery pump B1.

The bottom of esterification heating jacket is provided with the upper room Heating medium 1m of esterification, and the top of esterification heating jacket is provided with esterification upper room heating agent outlet 1n；The bottom of precondensation heating jacket is provided with Heating medium 2h in room under precondensation, and the top of precondensation heating jacket is provided with room heating agent outlet 2j under precondensation；The shell side bottom of esterification material preheater 3 is provided with preheater Heating medium 3c, and the shell side top of esterification material preheater 3 is provided with preheater heating agent outlet 3d.

The job step of this utility model esterification Prepolycondensating reactor is as follows: (1) PTA powder and ethylene glycol mixing making beating Hou Jing center material pipe enter the inner draft tube 1g of the upper room 1 of esterification, nitrogen sprays from each nitrogen jet mouth 1h1 of cyclone agitator disk 1h, horizontal vortex is formed through water conservancy diversion bottom of room 1 in esterification of nitrogen water conservancy diversion arc 1h2, nitrogen moves upward and material is formed secondary stirring, material moves upward along the annulus between inner draft tube 1g and external flow guiding cylinder 1d under the thermal convection current dual function of nitrogen and heating coil, material within inner draft tube 1g flows downward, form inside and outside stream circulation.

The most at high temperature room 1 there is esterification with ethylene glycol in PTA powder in esterification, and in esterification, the gauge pressure of room 1 is 0.5～2bar, and the gaseous substance that esterification produces room gaseous phase outlet 1b from esterification discharges；Along with new material constantly enters, the material reacted enters esterification discharging annular groove 1e from external flow guiding cylinder material outlet 1d1, flowing one week in esterification discharging annular groove 1e and continuing to be heated makes reaction thorough, finally discharge from esterification material outlet 1f, carboxylate discharge nozzle G1 is entered by esterifying liquid level control valve V1, the aperture of esterifying liquid level control valve V1 is controlled by the liquid level of esterification discharging annular groove 1e, and auxiliary agent is added to carboxylate discharge nozzle G1 from auxiliary agent import G1a.

(3) under the effect of potential difference and pressure reduction, esterification material and auxiliary agent entrance preheater also pass material distribution plate 3e, and in auxiliary agent, the ethylene glycol gasification of excess produces bubble, and bubble moves upward and promotes material and stir；It is upwardly into room 2 under precondensation after esterification material is heated.

(4) under precondensation, in room 2, material upwards sequentially passes through each floor tower tray and proceeds partial esterification reaction, and enters polycondensation process；When through tower tray 2a, material is advanced into the inner chamber of material deflector cup 2a2 from material tedge 2a1, and then the baffling deflector cup discharging opening 2a3 from material deflector cup lower circumference downwards flows out, and forms air cavity at the top of material deflector cup 2a2；Under precondensation, the absolute pressure in ceiling portion is 1～10kpa, vacuum in last layer material deflector cup air cavity is the highest, more the most progressively successively decrease, material degree of polymerization during from bottom to top incrementally increases, enter discharging annular groove 2b in room under precondensation, under precondensation, discharging annular groove 2b in room flow one week and continue heated, finally discharging from precondensation discharging opening 2c, entering precondensation discharge nozzle G2 by precondensation fluid level control valve V2 or precondensation melt delivery pump B1.The material esterification yield of precondensation discharging opening 2c is more than 96%, and the degree of polymerization is more than 15.

The foregoing is only the preferable possible embodiments of this utility model, non-therefore limit to scope of patent protection of the present utility model.In addition to the implementation, this utility model can also have other embodiments, such as heating agent can be conduction oil, it is also possible to for other heat carrier etc..The technical scheme that all employing equivalents or equivalent transformation are formed, all falls within the protection domain of this utility model requirement.This utility model can pass through or use prior art to realize without the technical characteristic described, and does not repeats them here.

Claims (10)

1. null1. a fat polymerization two still system，Including esterification Prepolycondensating reactor with without stirring polymer reactor，Described esterification Prepolycondensating reactor is provided with material inlet and precondensation discharging opening，Described nothing stirring polymer reactor is provided with polymer reactor charging aperture and polymer discharge mouth，Described precondensation discharging opening is connected with precondensation discharge nozzle by precondensation fluid level control valve or precondensation melt delivery pump，Described precondensation discharge nozzle is connected with described polymer reactor charging aperture，It is characterized in that: the described cylinder including vertical setting and closed at both ends without stirring polymer reactor，The top of cylinder lumen is provided with cloth liquid dish that is horizontal and that laterally cut off by cylinder，Described cloth liquid dish is provided with up big and down small liquid distributing hole，Described liquid distributing hole is provided with film supplying tube and both coaxial lines，Described film supplying tube extends straight down，The inner chamber of described film supplying tube is plugged with polymer reactor heating medium for heating pipe，The external wall of upper portion of described cylinder is provided with polymer reactor vacuum orifice and described polymer reactor charging aperture，The lower end of described cylinder is provided with conical head，The lower end of described conical head is provided with discharging spiral，Described polymer discharge mouth is positioned at the lower end of described discharging spiral；The periphery of described cylinder is provided with polymer reactor chuck, the periphery of described conical head is provided with conical head chuck, described polymer reactor charging aperture is positioned at the lower section of described cloth liquid dish, the inwall of described cylinder is provided with ring-type cloth liquid bath with the described corresponding position of polymer reactor charging aperture, leaves uniform annular slot between lower end and the cylinder inboard wall of described cloth liquid bath；The lower inner wall of described cylinder is provided with ring-type collecting tank, the upper end open of described collecting tank and lower end closed；The outer wall of described cylinder is provided with the middle melt outlet communicated with the bottom of described collecting tank, described middle melt outlet is connected with the entrance of middle melt delivery pump, described middle melt conveying delivery side of pump is connected with middle melt inlet, and described middle melt inlet is positioned on cylinder body outer wall and is positioned at the top of described cloth liquid dish.
2. Fat polymerization two still system the most according to claim 1, it is characterized in that: described cloth liquid dish be arranged over film supplying tube dividing plate, described film supplying tube dividing plate be arranged over polymer reactor heating medium for heating pipe dividing plate, cylinder is laterally cut off by described film supplying tube dividing plate and described polymer reactor heating medium for heating pipe dividing plate respectively, described polymer reactor heating medium for heating pipe dividing plate be arranged over polymer reactor upper cover；The upper port of described film supplying tube is connected on the pore of described film supplying tube dividing plate, and the upper port of described polymer reactor heating medium for heating pipe is connected on the pore of described polymer reactor heating medium for heating pipe dividing plate；Connecting on described polymer reactor upper cover and have film supplying tube Heating medium, the barrel wall between described film supplying tube dividing plate with polymer reactor heating medium for heating pipe dividing plate is connected has film supplying tube heating agent to export.
3. Fat polymerization two still system the most according to claim 1, it is characterized in that: described cylinder inboard wall is provided with the barrel material distribution ring that downward spiral extends, the upper end of described barrel material distribution ring is positioned at below the outlet of described cloth liquid bath, the lower end of described barrel material distribution ring is positioned at above the upper port of described collecting tank, and described barrel material distribution ring is semi-circular cross-section and plane is connected on described cylinder inboard wall.
4. Fat polymerization two still system the most according to claim 1, it is characterised in that: the film supplying tube outer wall below described liquid distributing hole is uniformly provided with at least one film supplying tube material distribution ring, and the cross section of described film supplying tube material distribution ring is the little cydariform broad in the middle in two.
5. Fat polymerization two still system the most according to claim 1, it is characterized in that: described esterification Prepolycondensating reactor includes the vertical tower body closed, it is separated into room under the upper room of esterification and precondensation by arc-shaped partition in described vertical column body, in described esterification, the barrel of room is externally provided with esterification heating jacket, and under described precondensation, the barrel of room is externally provided with precondensation heating jacket；In described esterification, the top of room is provided with the upper room gaseous phase outlet of esterification and described material inlet, and the bottom centre of described arc-shaped partition is provided with nitrogen inlet, and in described esterification, the sidewall of room is provided with esterification material outlet；Under described precondensation, the bottom of room connects esterification material preheater, it is provided with preheater charging aperture bottom the low head of described esterification material preheater, described esterification material outlet is connected with described preheater charging aperture with carboxylate discharge nozzle by esterifying liquid level control valve, connecting on described carboxylate discharge nozzle has auxiliary agent import, the preheater discharging opening of described esterification material preheater upper end to be connected with the bottom inlet of room under described precondensation；Under described precondensation, the inner chamber of room is provided with multilamellar tower tray from bottom to top, and described precondensation discharging opening is positioned on the top barrel of room under described precondensation, described precondensation discharging opening be arranged over room vacuum orifice under precondensation.
6. Fat polymerization two still system the most according to claim 5, it is characterized in that: in described esterification, the bottom centre of room is provided with the cyclone agitator disk being horizontally disposed with and being centrosymmetric, described cyclone agitator disk is hollow cylinder plate, the bottom centre of described cyclone agitator disk is connected with described nitrogen inlet, multiple nitrogen jet mouth it is evenly distributed with in the circumferential wall of described cyclone agitator disk, the outside of each described nitrogen jet mouth is respectively equipped with the nitrogen water conservancy diversion arc making nitrogen tangentially penetrate, the root of each described nitrogen water conservancy diversion arc is connected in the circumferential wall of described cyclone agitator disk.
7. Fat polymerization two still system the most according to claim 6, it is characterized in that: in described esterification, the inner wall lower of room is provided with circumferentially and the external flow guiding cylinder of upper end open, esterification discharging annular groove is formed between described external flow guiding cylinder and the upper chamber interior walls of esterification, described external flow guiding cylinder is provided with external flow guiding cylinder material outlet and communicates with described esterification discharging annular groove, and described esterification material outlet communicates with the bottom of described esterification discharging annular groove；The inner chamber of described external flow guiding cylinder is provided with the inner draft tube of line coaxially therewith, and the annular section between described inner draft tube and described external flow guiding cylinder is positioned at above the excircle of described cyclone agitator disk, and the upper port of described inner draft tube is less than the upper port of external flow guiding cylinder；In described esterification, the inner chamber of room is provided with and extends downward the center material pipe in the middle part of inner draft tube along axis, and the upper end of described center material pipe is connected with described material inlet；Between described external flow guiding cylinder and inner draft tube, annulus is provided with many group esterification heating coils, and often group heating medium for heating coil pipe is respectively equipped with esterification heating coil Heating medium and esterification heating coil heating agent outlet.
8. Fat polymerization two still system the most according to claim 7, it is characterized in that: described external flow guiding cylinder material outlet extends vertically downwards along the short transverse of described external flow guiding cylinder, the inner chamber room of being provided with of described esterification discharging annular groove radially diaphragm, described external flow guiding cylinder material outlet and described esterification material outlet lay respectively at the both sides of described upper room radially diaphragm；Top tray be arranged over discharging annular groove in room under precondensation, under described precondensation, the bottom of room discharging annular groove is connected under described precondensation on the barrel of room, under described precondensation, room discharging annular groove is provided with flash mouth in room under vertically extending precondensation, described precondensation discharging opening communicates with the bottom of room discharging annular groove under described precondensation, under described precondensation, the inner chamber of room discharging annular groove is provided with room radially diaphragm under precondensation, and under described precondensation, room flash mouth and described precondensation discharging opening lay respectively at the both sides of room radially diaphragm under described precondensation.
9. Fat polymerization two still system the most according to claim 5, it is characterized in that: on the described tower tray of each layer, be respectively uniformly distributed the material tedge of multiple through tower tray, the top of each described material tedge is covered each by the material deflector cup of line coaxially therewith, each described material deflector cup is fornix shape and lower port is connected on described tower tray, and the lower circumference of each described material deflector cup is uniformly provided with deflector cup discharging opening.
10. Fat polymerization two still system the most according to claim 8, it is characterized in that: under described precondensation room discharging annular groove be arranged over foam trapping dish, described foam trapping dish is horizontally set under described precondensation on the cross section of room and is positioned at the lower section of room vacuum orifice under described precondensation；The low head inner chamber of described esterification material preheater is respectively equipped with horizontally disposed material distribution plate, and described material distribution plate is evenly distributed with multiple material dispensing orifice.