CN205650187U

CN205650187U - Esterify and get together two cauldron devices

Info

Publication number: CN205650187U
Application number: CN201620343063.1U
Authority: CN
Inventors: 景辽宁; 严旭明; 陈文兴; 刘荣俊; 钟明
Original assignee: Yangzhou Huitong Chemical Polytron Technologies Inc
Current assignee: Yangzhou Huitong Chemical Polytron Technologies Inc
Priority date: 2016-04-22
Filing date: 2016-04-22
Publication date: 2016-10-19
Anticipated expiration: 2026-04-22

Abstract

The utility model relates to an esterify and get together two cauldron devices, including esterify in advance the condensation polymerization tower with do not have stirring polymerization ware, the preshrunk of condensation polymerization tower in advance of esterifying gathers the discharge gate and gathers the melt -conveying pump through preshrunk and link to each other with polymerization ware feed inlet. 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. The device compact structure, area is little, and production efficiency is high.

Description

A kind of fat polymerization two kettle device

Technical field

This utility model relates to a kind of fat polymerization two kettle device, 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 kettle device, compact conformation, and floor space is little, and production efficiency is high.

For solving above technical problem, a kind of fat polymerization two kettle device of the present utility model, including esterification prepolymerization reaction tower with without stirring polymer reactor, described esterification prepolymerization reaction tower is provided with esterification room slurry import and precondensation room discharging opening, described nothing stirring polymer reactor is provided with polymer reactor charging aperture and polymer discharge mouth, described precondensation room discharging opening is connected with described polymer reactor charging aperture with precondensation discharge nozzle by precondensation melt delivery pump, described esterification prepolymerization reaction tower includes the mixing chamber being sequentially stacked from top to bottom, esterification room and precondensation room, described mixing chamber is spaced from each other by the top of curved bottom with described esterification room, described esterification room is spaced from each other by the top of curved bottom with described precondensation room；The slurry import of described esterification room is connected to the top of described esterification room, and described precondensation room discharging opening is positioned at the bottom of described precondensation room；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: esterification room, mixing chamber and precondensation room are connected as a single entity by this esterification prepolymerization reaction tower, compact conformation, floor space is little, and heat loss is few, mixing chamber can be up to from esterification room without extra power material, flow to precondensation room, esterification room and precondensation room mechanical agitating device again, save energy consumption, reduce fault rate, improve production efficiency.nullPrecondensation melt is carried to polymer reactor charging aperture by precondensation melt delivery pump，Precondensation 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, the mixing chamber top of described esterification prepolymerization reaction tower is provided with additive inlet port and mixing chamber gaseous phase outlet, the top barrel of described mixing chamber connects mixing chamber carboxylate import, and the center of described mixing chamber curved bottom connects mixing chamber discharging opening；The top barrel of described esterification room connects esterification room gaseous phase outlet, and the cylinder inboard wall below the slurry import of described esterification room is provided with the esterification room discharging annular groove of upper end open, and the bottom of described esterification room discharging annular groove connects esterification room discharging opening；The top barrel of described precondensation room connects precondensation room charging aperture and precondensation room vacuum orifice；Described esterification room discharging opening is connected with described mixing chamber carboxylate import by esterification room fluid level control valve and carboxylate discharge nozzle, and described mixing chamber discharging opening is connected with described precondensation room charging aperture by mixing chamber fluid level control valve and mixture discharge nozzle.Esterification room is entered from esterification room slurry import after PTA powder and ethylene glycol mixing making beating, under the hot environment of esterification room, PTA powder and ethylene glycol generation esterification, the operating pressure of esterification room is 0.5～1.5bar(gauge pressure), the gaseous substance that esterification produces is discharged from esterification room gaseous phase outlet, and esterification material enters esterification room discharging annular groove, then discharges from esterification room discharging opening, the esterification yield of esterification material is more than 90%, and temperature controls at 250～260 DEG C；Then esterification material enters carboxylate discharge nozzle by esterification room fluid level control valve, under the effect of pressure reduction, esterification material is upwardly into mixing chamber carboxylate import, additive synchronizes to enter mixing chamber inner chamber from additive inlet port, esterification material and additive are discharged from mixing chamber discharging opening after uniformly mixing and heating, the gaseous substance that mixing chamber produces is discharged from mixing chamber gaseous phase outlet, the operating pressure of mixing chamber is normal pressure, temperature controls at 255～265 DEG C, esterification yield is more than 95%, mixed material enters mixture discharge nozzle by mixing chamber fluid level control valve, under the dual function of potential difference and pressure reduction, mixed material is downwardly into precondensation room charging aperture, partial esterification reaction is proceeded in precondensation room, simultaneously enter polycondensation process；The vacuum in precondensation room is kept in 1～10kpa(absolute pressure) by precondensation room vacuum orifice, material degree of polymerization during from bottom to top incrementally increases, finally discharge from precondensation room discharging opening, the esterification yield of precondensation room discharging opening is more than 99%, the degree of polymerization is more than 25, and temperature controls at 265～270 DEG C.

As further improvement of the utility model, the lower section of described esterification room discharging annular groove is provided with esterification room bringing-up section, the two ends up and down of described esterification room bringing-up section are provided with the esterification room tube sheet laterally separated by being esterified room, the central area of esterification room tube sheet connects up and down has and esterification room coaxial line and through esterification room guide shell, is also associated with many through esterification room tubulations up and down between the tube sheet of esterification room；The shell side bottom of described esterification room bringing-up section connects esterification room bringing-up section Heating medium, and the shell side top of described esterification room bringing-up section connects the bringing-up section heating agent outlet of esterification room；The inner chamber of described esterification room is provided with and extends downward center, the esterification room material pipe in the middle part of the guide shell of esterification room along axis, and the upper end of center, described esterification room material pipe is connected with the slurry import of described esterification room.PTA powder and ethylene glycol mixed slurry enter esterification room guide shell inner chamber from esterification center, room material pipe, after flowing downwardly into bottom esterification room, under the thermal convection current effect of esterification room bringing-up section up along each esterification room tubulation, flow up while being subject to be esterified the indirect heating of room bringing-up section thermal medium, material after heating arrives the top of esterification room bringing-up section, esterification room guide shell inner chamber is reentered under the dual function of thermal convection current and the jet of esterification center, room material pipe, jointly flow downward with fresh slurry, form stream circulation.

As further improvement of the utility model, the inner peripheral wall of described esterification room discharging annular groove is provided with the discharging annular groove flash mouth extended vertically downwards, the inner chamber of described esterification room discharging annular groove is provided with esterification room radially diaphragm, and described discharging annular groove flash mouth and described esterification room discharging opening lay respectively at the both sides of described esterification room radially diaphragm.Along with new slurry constantly enters, the material reacted enters esterification room discharging annular groove from discharging annular groove flash mouth, flow one week in the form that esterification room discharging annular groove is laminar flow and continue heated, extend the heat time heating time being esterified material in esterification room discharging annular groove, make esterification more thorough, esterification material is finally discharged from esterification room discharging opening, enters mixing chamber carboxylate import by esterification room fluid level control valve and carboxylate discharge nozzle.

As further improvement of the utility model, the lower section of described mixing chamber carboxylate import is provided with mixing chamber bringing-up section, the two ends up and down of described mixing chamber bringing-up section are provided with mixing chamber tube sheet laterally separated for mixing chamber, the central area of mixing chamber tube sheet connects up and down has and mixing chamber coaxial line and through mixing chamber guide shell, is also associated with many through mixing chamber tubulations between upper and lower mixing chamber tube sheet；The shell side bottom of described mixing chamber bringing-up section connects mixing chamber bringing-up section Heating medium, and the shell side top of described mixing chamber bringing-up section connects has mixing chamber bringing-up section heating agent to export；The inner chamber of described mixing chamber is provided with and extends downward the mixing chamber shaft in the middle part of mixing chamber guide shell along axis, the lower end of described mixing chamber shaft is provided with stirrer paddle, and the upper end of described mixing chamber shaft passes from mixing chamber top and is connected with the output shaft of stirring motor.After esterification material and additive enter mixing chamber, enter mixing chamber guide shell inner chamber, under the agitation of stirrer paddle, after flowing downwardly into bottom mixing chamber after esterification material and additive mix homogeneously, under the thermal convection current effect of mixing chamber bringing-up section up along each mixing chamber tubulation, flow up while being heated by the indirect of mixing chamber bringing-up section thermal medium, material after heating arrives the top of mixing chamber bringing-up section, mixing chamber guide shell inner chamber is reentered under the effect of thermal convection current, jointly flow downward with fresh material, form stream circulation.

As further improvement of the utility model, described precondensation room includes the precondensation room feed zone being sequentially connected with from top to bottom, precondensation room bringing-up section and precondensation room discharging section, the bottom of described precondensation room feed zone is provided with precondensation room diaphragm plate laterally separated for precondensation room, the inner chamber of described precondensation room feed zone is provided with along the precondensation room guide breather that axis downwardly extends, the lower nozzle of described precondensation room guide breather extends to the lower section of described precondensation room diaphragm plate, the lower section of described precondensation room guide breather is provided with the precondensation room deflection cone of umbrella shape, described precondensation room charging aperture is connected on the precondensation room barrel above the diaphragm plate of described precondensation room, the top of described precondensation room guide breather is provided with the precondensation room flash mouth extended vertically downwards；The two ends up and down of described precondensation room bringing-up section are provided with precondensation room tube sheet laterally separated for precondensation room, and connecting between the tube sheet of upper and lower precondensation room has many through precondensation room film supplying tubes；The shell side bottom of described precondensation room bringing-up section connects precondensation room bringing-up section Heating medium, and the shell side top of described precondensation room bringing-up section connects the bringing-up section heating agent outlet of precondensation room.Mixed material annulus above precondensation room charging aperture enters precondensation room diaphragm plate, 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；Mixed material enters the guide breather of precondensation room from precondensation room flash mouth, and the inwall along precondensation room guide breather flows downward, and gaseous substance flows up along precondensation room guide breather, and from precondensation room, vacuum orifice is drawn out of.Mixed material, after precondensation room guide breather flows out, falls on the deflection cone of precondensation room, and the normal cone along precondensation room deflection cone faces down and flows and uniform, enters precondensation room bringing-up section.Mixed material flows downward from precondensation room feed zone and enters each precondensation room film supplying tube, in precondensation room, film supplying tube inwall forms uniform falling liquid film, during flowing downward, under the heating and vacuum action of precondensation room bringing-up section heating agent, mixed material heats up and is able to polycondensation, then the lower port from precondensation room film supplying tube is discharged into precondensation room discharging section, and finally the precondensation room discharging opening from the outlet of precondensation room discharging section is discharged.

As further improvement of the utility model, the upper orifice of described precondensation room film supplying tube, middle part and lower nozzle are evenly distributed with multiple and precondensation room film supplying tube coaxial line precondensation room stock distributor, described precondensation room stock distributor includes cylinder pipeline section and the Taper Pipe section being connected as a single entity, described Taper Pipe section is up-small and down-big structure and the lower section being connected to described cylinder pipeline section, the upper port of described cylinder pipeline section is circumferentially uniformly provided with multiple upper material distribution tooth, the lower port of described Taper Pipe section is supported on the inwall of described precondensation room film supplying tube and is circumferentially uniformly provided with multiple lower material distribution tooth.A part of mixed material enters the ring cavity between cylinder pipeline section and the precondensation room film supplying tube inwall of precondensation room stock distributor, distribute tooth from the lower material of Taper Pipe section lower port downwards flow out and continue to flow downward, another part mixed material distributes tooth overflow from the upper material of cylinder pipeline section upper port and enters precondensation room stock distributor inner chamber, inwall along cylinder pipeline section and Taper Pipe section is membranaceous flowing downward, continue to flow downward after converging with the material flowed out from lower material distribution tooth, the falling liquid film that precondensation room stock distributor both can make material shape become is more uniform, falling liquid film can be flowed downward again and play retardation, increase the flowing time of falling liquid film, make polycondensation reaction more abundant.

As further improvement of the utility model, the annulus of guide breather periphery, described precondensation room is provided with precondensation room radially diaphragm, and described precondensation room flash mouth and described precondensation room charging aperture lay respectively at the both sides of described precondensation room radially diaphragm；The curved bottom of described mixing chamber is provided with mixing chamber thermometer boss and mixing chamber interface of the level gauge, and the aperture of described mixing chamber fluid level control valve is controlled by the liquid level of described mixing chamber；The curved bottom of described esterification room is provided with esterification room temperature meter interface and esterification room interface of the level gauge, and the aperture of described esterification room fluid level control valve is controlled by the liquid level of described esterification room；The lower sides of described precondensation room is provided with precondensation room temperature meter interface and precondensation room interface of the level gauge, and the flow rates controlled of described precondensation melt delivery pump is in the liquid level of described precondensation room.Mixed material enters the annulus of guide breather periphery, precondensation room from precondensation room charging aperture, form in laminar flow flows one week along this annulus and is heated, extend material heat time heating time at precondensation room feed zone, being conducive to the flash distillation removing of gaseous substance, material finally enters the guide breather of precondensation room from precondensation room flash mouth.

As further improvement of the utility model, the described cloth liquid dish without stirring polymer reactor is 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, the described cylinder inboard wall without stirring polymer reactor 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；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.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.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.

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 flow chart of this utility model fat polymerization two kettle device.

Fig. 2 is the structural representation being esterified prepolymerization reaction tower in this utility model.

Fig. 3 is the flow direction of material figure being esterified discharging annular groove in room in Fig. 2.

Fig. 4 is the flow direction of material figure of precondensation room feed zone in Fig. 2.

Fig. 5 is the partial schematic diagram of precondensation room film supplying tube in Fig. 2.

Fig. 6 is that this utility model is without stirring the structural representation of polymer reactor.

Fig. 7 is the enlarged drawing of aminoacyl site in Fig. 6.

In figure: 1. mixing chamber；1a. additive inlet port；1b. mixing chamber carboxylate import；1c. mixing chamber discharging opening；1d. mixing chamber guide shell；1e. mixing chamber tubulation；1f1. mixing chamber bringing-up section Heating medium；1f2. mixing chamber bringing-up section heating agent exports；1g1. mixing chamber chuck Heating medium；1g2. mixing chamber chuck heating agent exports；1h. stirring motor；1h1. mixing chamber shaft；1j. mixing chamber gaseous phase outlet；1k. mixing chamber thermometer boss；1m. mixing chamber interface of the level gauge.

2. esterification room；2a. is esterified room slurry import；2b. is esterified room discharging annular groove；2b1. discharging annular groove flash mouth；2b2. esterification room radially diaphragm；2c. esterification room discharging opening；2d. esterification room guide shell；2e. esterification room tubulation；2f1. esterification room bringing-up section Heating medium；The bringing-up section heating agent outlet of 2f2. esterification room；2g1. esterification room chuck Heating medium；The chuck heating agent outlet of 2g2. esterification room；2h. esterification center, room material pipe；2j. esterification room gaseous phase outlet；2k. is esterified room temperature meter interface；2m. esterification room interface of the level gauge.

3. precondensation room；3a. precondensation room charging aperture；3b. precondensation room guide breather；3b1. precondensation room flash mouth；3b2. precondensation room radially diaphragm；3c. precondensation room discharging opening；3d. precondensation room deflection cone；3e. precondensation room film supplying tube；3e1. precondensation room stock distributor；3e2. upper material distribution tooth；Material distribution tooth under 3e3.；3f1. precondensation room bringing-up section Heating medium；The bringing-up section heating agent outlet of 3f2. precondensation room；3g1. precondensation room feed zone chuck Heating medium；The feed zone chuck heating agent outlet of 3g2. precondensation room；3h1. precondensation room discharging section chuck Heating medium；The discharging section chuck heating agent outlet of 3h2. precondensation room；3j. precondensation room vacuum orifice；3k. precondensation room temperature meter interface；3m. precondensation room interface of the level gauge；3n. precondensation room diaphragm plate.

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.

V1. esterification room fluid level control valve；V2. mixing chamber fluid level control valve；G1. carboxylate discharge nozzle；G2. mixture discharge nozzle；G3. precondensation discharge nozzle；B1. precondensation melt delivery pump.

Detailed description of the invention

Shown in Fig. 1, fat polymerization two kettle device of the present utility model includes being esterified prepolymerization reaction tower and without stirring polymer reactor 4, esterification prepolymerization reaction tower is provided with esterification room slurry import 2a and precondensation room discharging opening 3c, being provided with polymer reactor charging aperture 401a and polymer discharge mouth 410a without stirring polymer reactor 4, precondensation room discharging opening 3c is connected with polymer reactor charging aperture 401a with precondensation discharge nozzle G3 by precondensation melt delivery pump B1.

As shown in Figure 2, esterification prepolymerization reaction tower includes mixing chamber 1, esterification room 2 and the precondensation room 3 being sequentially stacked from top to bottom, mixing chamber 1 is spaced from each other by the top of curved bottom with esterification room 2, and esterification room 2 is spaced from each other by the top of curved bottom with precondensation room 3.

The top of mixing chamber 1 is provided with additive inlet port 1a and mixing chamber gaseous phase outlet 1j, and the top barrel of mixing chamber connects mixing chamber carboxylate import 1b, and the center of mixing chamber curved bottom connects mixing chamber discharging opening 1c；The curved bottom of mixing chamber is provided with mixing chamber thermometer boss 1k and mixing chamber interface of the level gauge 1m.The lower section of mixing chamber carboxylate import 1b is provided with mixing chamber bringing-up section, barrel periphery above mixing chamber bringing-up section is provided with mixing chamber heating jacket, the bottom of mixing chamber heating jacket connects mixing chamber chuck Heating medium 1g1, and the top of mixing chamber heating jacket connects has mixing chamber chuck heating agent to export 1g2.

The top barrel of esterification room 2 connects esterification room slurry import 2a and esterification room gaseous phase outlet 2j, cylinder inboard wall below esterification room slurry import 2a is provided with the esterification room discharging annular groove 2b of upper end open, and the bottom of esterification room discharging annular groove 2b connects esterification room discharging opening 2c；The curved bottom of esterification room is provided with esterification room temperature meter interface 2k and esterification room interface of the level gauge 2m.The barrel periphery of esterification room discharging annular groove 2b is provided with esterification room heating jacket, and the bottom of esterification room heating jacket connects esterification room chuck Heating medium 2g1, and the top of esterification room heating jacket connects esterification room chuck heating agent outlet 2g2.

Precondensation room 3 includes precondensation room feed zone, precondensation room bringing-up section and the precondensation room discharging section being sequentially connected with from top to bottom.The top barrel of precondensation room feed zone connects precondensation room charging aperture 3a and precondensation room vacuum orifice 3j, and the bottom of precondensation room is provided with precondensation room discharging opening 3c；The lower sides of precondensation room discharging section is provided with precondensation room temperature meter interface 3k and precondensation room interface of the level gauge 3m, and the flow rates controlled of precondensation melt delivery pump B1 is in the liquid level of precondensation room 3.

The barrel periphery of precondensation room feed zone is provided with precondensation room feed zone heating jacket, the bottom of precondensation room feed zone heating jacket connects precondensation room feed zone chuck Heating medium 3g1, and the top of precondensation room feed zone heating jacket connects precondensation room feed zone chuck heating agent outlet 3g2.

The barrel periphery of precondensation room discharging section is provided with precondensation room discharging section heating jacket, the bottom of precondensation room discharging section heating jacket connects precondensation room discharging section chuck Heating medium 3h1, and the top of precondensation room discharging section heating jacket connects precondensation room discharging section chuck heating agent outlet 3h2.

Esterification room discharging opening 2c is connected with mixing chamber carboxylate import 1b by esterification room fluid level control valve V1 and carboxylate discharge nozzle G1, and the aperture of esterification room fluid level control valve V1 is controlled by the liquid level of esterification room.Mixing chamber discharging opening 1c is connected with precondensation room charging aperture 3a by mixing chamber fluid level control valve V2 and mixture discharge nozzle G2, and the aperture of mixing chamber fluid level control valve V2 is controlled by the liquid level of mixing chamber.

Esterification room is entered from esterification room slurry import 2a after PTA powder and ethylene glycol mixing making beating, under the hot environment of esterification room, PTA powder and ethylene glycol generation esterification, the operating pressure of esterification room is 0.5～1.5bar(gauge pressure), the gaseous substance that esterification produces is discharged from esterification room gaseous phase outlet 2j, and esterification material enters esterification room discharging annular groove 2b, then discharges from esterification room discharging opening 2c, the esterification yield of esterification material is more than 90%, and temperature controls at 250～260 DEG C.

Then esterification material enters carboxylate discharge nozzle G1 by esterification room fluid level control valve V1, under the effect of pressure reduction, esterification material is upwardly into mixing chamber carboxylate import 1b, additive (such as adding titanium dioxide as delustering agent) synchronizes to enter mixing chamber inner chamber from additive inlet port 1a, esterification material and additive are discharged from mixing chamber discharging opening 1c after uniformly mixing and heating, the gaseous substance that mixing chamber produces is discharged from mixing chamber gaseous phase outlet 1j, the operating pressure of mixing chamber is normal pressure, temperature controls at 255～265 DEG C, and esterification yield is more than 95%.

Mixed material enters mixture discharge nozzle G2 by mixing chamber fluid level control valve V2, and under the dual function of potential difference and pressure reduction, mixed material is downwardly into precondensation room charging aperture 3a, proceeds partial esterification reaction, simultaneously enter polycondensation process in precondensation room；The vacuum in precondensation room is kept in 1～10kpa(absolute pressure) by precondensation room vacuum orifice 3j, material degree of polymerization during from bottom to top incrementally increases, finally discharge from precondensation room discharging opening 3c, the esterification yield of precondensation room discharging opening 3c is more than 99%, the degree of polymerization is more than 25, and temperature controls at 265～270 DEG C.

The lower section of esterification room discharging annular groove 2b is provided with esterification room bringing-up section, the two ends up and down of esterification room bringing-up section are provided with the esterification room tube sheet laterally separated by being esterified room, the central area of esterification room tube sheet connects up and down has and esterification room coaxial line and through esterification room guide shell 2d, is also associated with many through esterification room tubulation 2e up and down between the tube sheet of esterification room；The shell side bottom of esterification room bringing-up section connects esterification room bringing-up section Heating medium 2f1, and the shell side top of esterification room bringing-up section connects esterification room bringing-up section heating agent outlet 2f2；The inner chamber of esterification room is provided with and extends downward center, the esterification room material pipe 2h in the middle part of esterification room guide shell 2d along axis, and the upper end of esterification center, room material pipe 2h is connected with esterification room slurry import 2a.

PTA powder and ethylene glycol mixed slurry enter esterification room guide shell 2d inner chamber from esterification center, room material pipe 2h, after flowing downwardly into bottom esterification room, under the thermal convection current effect of esterification room bringing-up section up along each esterification room tubulation 2e, flow up while being subject to be esterified the indirect heating of room bringing-up section thermal medium, material after heating arrives the top of esterification room bringing-up section, esterification room guide shell 2d inner chamber is reentered under the dual function of thermal convection current and the jet of esterification center, room material pipe 2h, jointly flow downward with fresh slurry, form stream circulation.

As shown in Figure 3, the inner peripheral wall of esterification room discharging annular groove 2b is provided with the discharging annular groove flash mouth 2b1 extended vertically downwards, the inner chamber of esterification room discharging annular groove 2b is provided with esterification room radial direction diaphragm 2b2, discharging annular groove flash mouth 2b1 and esterification room discharging opening 2c and lays respectively at the both sides of esterification room radially diaphragm 2b2.Along with new slurry constantly enters, the material reacted enters esterification room discharging annular groove 2b from discharging annular groove flash mouth 2b1, flow one week in the form that esterification room discharging annular groove 2b is laminar flow and continue heated, extend the heat time heating time being esterified material in esterification room discharging annular groove 2b, make esterification more thorough, esterification material is finally discharged from esterification room discharging opening 2c, enters mixing chamber carboxylate import 1b by esterification room fluid level control valve V1 and carboxylate discharge nozzle G1.

The two ends up and down of mixing chamber bringing-up section are provided with mixing chamber tube sheet laterally separated for mixing chamber, the central area of mixing chamber tube sheet connects up and down has and mixing chamber coaxial line and through mixing chamber guide shell 1d, is also associated with many through mixing chamber tubulation 1e between upper and lower mixing chamber tube sheet；The shell side bottom of mixing chamber bringing-up section connects mixing chamber bringing-up section Heating medium 1f1, and the shell side top of mixing chamber bringing-up section connects has mixing chamber bringing-up section heating agent to export 1f2；The inner chamber of mixing chamber is provided with and extends downward the mixing chamber shaft 1h1 in the middle part of mixing chamber guide shell 1d along axis, the lower end of mixing chamber shaft 1h1 is provided with stirrer paddle, and the upper end of mixing chamber shaft 1h1 passes from mixing chamber top and is connected with the output shaft of stirring motor 1h.

After esterification material and additive enter mixing chamber, enter mixing chamber guide shell 1d inner chamber, under the agitation of stirrer paddle, after flowing downwardly into bottom mixing chamber after esterification material and additive mix homogeneously, under the thermal convection current effect of mixing chamber bringing-up section up along each mixing chamber tubulation 1e, flow up while being heated by the indirect of mixing chamber bringing-up section thermal medium, material after heating arrives the top of mixing chamber bringing-up section, mixing chamber guide shell 1d inner chamber is reentered under the effect of thermal convection current, jointly flow downward with fresh material, form stream circulation.

The bottom of precondensation room feed zone is provided with precondensation room diaphragm plate 3n laterally separated for precondensation room, the inner chamber of precondensation room feed zone is provided with along the precondensation room guide breather 3b that axis downwardly extends, the lower nozzle of precondensation room guide breather 3b extends to the lower section of precondensation room diaphragm plate 3n, the lower section of precondensation room guide breather 3b is provided with the precondensation room deflection cone 3d of umbrella shape, precondensation room charging aperture 3a is connected on the precondensation room barrel above the diaphragm plate 3n of precondensation room, the top of precondensation room guide breather 3b is provided with the precondensation room flash mouth 3b1 extended vertically downwards.Mixed material annulus above precondensation room charging aperture 3a enters precondensation room diaphragm plate 3n, 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；Mixed material enters the guide breather 3b of precondensation room from precondensation room flash mouth 3b1, and the inwall along precondensation room guide breather 3b flows downward, and gaseous substance flows up along precondensation room guide breather 3b, and from precondensation room, vacuum orifice 3j is drawn out of.Mixed material, after precondensation room guide breather 3b flows out, falls on the deflection cone 3d of precondensation room, and the normal cone along precondensation room deflection cone 3d faces down and flows and uniform, enters precondensation room bringing-up section.

As shown in Figure 4, the annulus of guide breather 3b periphery, precondensation room is provided with precondensation room radially diaphragm 3b2, precondensation room flash mouth 3b1 and precondensation room charging aperture 3a and lays respectively at the both sides of precondensation room radially diaphragm 3b2.Mixed material enters the annulus of guide breather 3b periphery, precondensation room from precondensation room charging aperture 3a, form in laminar flow flows one week along this annulus and is heated, extend material heat time heating time at precondensation room feed zone, being conducive to the flash distillation removing of gaseous substance, material finally enters the guide breather 3b of precondensation room from precondensation room flash mouth 3b1.

The two ends up and down of precondensation room bringing-up section are provided with precondensation room tube sheet laterally separated for precondensation room, and connecting between the tube sheet of upper and lower precondensation room has many through precondensation room film supplying tube 3e；Upper orifice, middle part and the lower nozzle of precondensation room film supplying tube 3e is evenly distributed with multiple and precondensation room film supplying tube coaxial line precondensation room stock distributor 3e1.The shell side bottom of precondensation room bringing-up section connects precondensation room bringing-up section Heating medium 3f1, and the shell side top of precondensation room bringing-up section connects precondensation room bringing-up section heating agent outlet 3f2.

In precondensation room bringing-up section, mixed material flows downward from precondensation room feed zone and enters each precondensation room film supplying tube 3e, in precondensation room, film supplying tube 3e inwall forms uniform falling liquid film, during flowing downward, under the heating and vacuum action of precondensation room bringing-up section heating agent, mixed material heats up and is able to polycondensation, and then the lower port from precondensation room film supplying tube 3e is discharged into precondensation room discharging section, and finally the precondensation room discharging opening 3c from the outlet of precondensation room discharging section discharges.

As shown in Figure 5, precondensation room stock distributor 3e1 includes cylinder pipeline section and the Taper Pipe section being connected as a single entity, Taper Pipe section is up-small and down-big structure and the lower section being connected to cylinder pipeline section, the upper port of cylinder pipeline section is circumferentially uniformly provided with multiple upper material distribution tooth 3e2, and the lower port of Taper Pipe section is supported on the inwall of precondensation room film supplying tube 3e and is circumferentially uniformly provided with multiple lower material distribution tooth 3e3.In the film supplying tube 3e of precondensation room, a part of mixed material enters the ring cavity between cylinder pipeline section and the precondensation room film supplying tube 3e inwall of precondensation room stock distributor 3e1, distribute tooth 3e3 from the lower material of Taper Pipe section lower port downwards flow out and continue to flow downward, another part mixed material distributes tooth 3e2 overflow from the upper material of cylinder pipeline section upper port and enters precondensation room stock distributor 3e1 inner chamber, inwall along cylinder pipeline section and Taper Pipe section flows downward, continue to flow downward after converging with the material flowed out from lower material distribution tooth 3e3, the falling liquid film that precondensation room stock distributor 3e1 both can make material shape become is more uniform, falling liquid film can be flowed downward again and play retardation, increase the flowing time of falling liquid film, make polycondensation reaction more abundant.

As shown in Figure 6, Figure 7, 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.Vacuum in polymer reactor is less than 200Pa(absolute pressure), reaction temperature is between 280 ~ 295 DEG C, and final polymer poly is right is more than 100, and intrinsic viscosity is more than 0.6, can be used for direct pelletizing, spinning, membrane or polyester for bottle etc..

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.

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

1. fat polymerization two kettle device, including esterification prepolymerization reaction tower with without stirring polymer reactor, described esterification prepolymerization reaction tower is provided with esterification room slurry import and precondensation room discharging opening, described nothing stirring polymer reactor is provided with polymer reactor charging aperture and polymer discharge mouth, described precondensation room discharging opening is connected with described polymer reactor charging aperture with precondensation discharge nozzle by precondensation melt delivery pump, it is characterized in that: described esterification prepolymerization reaction tower includes the mixing chamber being sequentially stacked from top to bottom, esterification room and precondensation room, described mixing chamber is spaced from each other by the top of curved bottom with described esterification room, described esterification room is spaced from each other by the top of curved bottom with described precondensation room；The slurry import of described esterification room is connected to the top of described esterification room, and described precondensation room discharging opening is positioned at the bottom of described precondensation room；

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.

Fat polymerization two kettle device the most according to claim 1, it is characterized in that: the mixing chamber top of described esterification prepolymerization reaction tower is provided with additive inlet port and mixing chamber gaseous phase outlet, the top barrel of described mixing chamber connects mixing chamber carboxylate import, and the center of described mixing chamber curved bottom connects mixing chamber discharging opening；The top barrel of described esterification room connects esterification room gaseous phase outlet, and the cylinder inboard wall below the slurry import of described esterification room is provided with the esterification room discharging annular groove of upper end open, and the bottom of described esterification room discharging annular groove connects esterification room discharging opening；The top barrel of described precondensation room connects precondensation room charging aperture and precondensation room vacuum orifice；Described esterification room discharging opening is connected with described mixing chamber carboxylate import by esterification room fluid level control valve and carboxylate discharge nozzle, and described mixing chamber discharging opening is connected with described precondensation room charging aperture by mixing chamber fluid level control valve and mixture discharge nozzle.

Fat polymerization two kettle device the most according to claim 2, it is characterized in that: the lower section of described esterification room discharging annular groove is provided with esterification room bringing-up section, the two ends up and down of described esterification room bringing-up section are provided with the esterification room tube sheet laterally separated by being esterified room, the central area of esterification room tube sheet connects up and down has and esterification room coaxial line and through esterification room guide shell, is also associated with many through esterification room tubulations up and down between the tube sheet of esterification room；The shell side bottom of described esterification room bringing-up section connects esterification room bringing-up section Heating medium, and the shell side top of described esterification room bringing-up section connects the bringing-up section heating agent outlet of esterification room；The inner chamber of described esterification room is provided with and extends downward center, the esterification room material pipe in the middle part of the guide shell of esterification room along axis, and the upper end of center, described esterification room material pipe is connected with the slurry import of described esterification room.

Fat polymerization two kettle device the most according to claim 2, it is characterized in that: the inner peripheral wall of described esterification room discharging annular groove is provided with the discharging annular groove flash mouth extended vertically downwards, the inner chamber of described esterification room discharging annular groove is provided with esterification room radially diaphragm, and described discharging annular groove flash mouth and described esterification room discharging opening lay respectively at the both sides of described esterification room radially diaphragm.

Fat polymerization two kettle device the most according to claim 2, it is characterized in that: the lower section of described mixing chamber carboxylate import is provided with mixing chamber bringing-up section, the two ends up and down of described mixing chamber bringing-up section are provided with mixing chamber tube sheet laterally separated for mixing chamber, the central area of mixing chamber tube sheet connects up and down has and mixing chamber coaxial line and through mixing chamber guide shell, is also associated with many through mixing chamber tubulations between upper and lower mixing chamber tube sheet；The shell side bottom of described mixing chamber bringing-up section connects mixing chamber bringing-up section Heating medium, and the shell side top of described mixing chamber bringing-up section connects has mixing chamber bringing-up section heating agent to export；The inner chamber of described mixing chamber is provided with and extends downward the mixing chamber shaft in the middle part of mixing chamber guide shell along axis, the lower end of described mixing chamber shaft is provided with stirrer paddle, and the upper end of described mixing chamber shaft passes from mixing chamber top and is connected with the output shaft of stirring motor.

null6. according to fat polymerization two kettle device according to any one of claim 2 to 5，It is characterized in that: described precondensation room includes the precondensation room feed zone being sequentially connected with from top to bottom、Precondensation room bringing-up section and precondensation room discharging section，The bottom of described precondensation room feed zone is provided with precondensation room diaphragm plate laterally separated for precondensation room，The inner chamber of described precondensation room feed zone is provided with along the precondensation room guide breather that axis downwardly extends，The lower nozzle of described precondensation room guide breather extends to the lower section of described precondensation room diaphragm plate，The lower section of described precondensation room guide breather is provided with the precondensation room deflection cone of umbrella shape，Described precondensation room charging aperture is connected on the precondensation room barrel above the diaphragm plate of described precondensation room，The top of described precondensation room guide breather is provided with the precondensation room flash mouth extended vertically downwards；The two ends up and down of described precondensation room bringing-up section are provided with precondensation room tube sheet laterally separated for precondensation room, and connecting between the tube sheet of upper and lower precondensation room has many through precondensation room film supplying tubes；The shell side bottom of described precondensation room bringing-up section connects precondensation room bringing-up section Heating medium, and the shell side top of described precondensation room bringing-up section connects the bringing-up section heating agent outlet of precondensation room.

Fat polymerization two kettle device the most according to claim 6, it is characterized in that: the upper orifice of described precondensation room film supplying tube, middle part and lower nozzle are evenly distributed with multiple and precondensation room film supplying tube coaxial line precondensation room stock distributor, described precondensation room stock distributor includes cylinder pipeline section and the Taper Pipe section being connected as a single entity, described Taper Pipe section is up-small and down-big structure and the lower section being connected to described cylinder pipeline section, the upper port of described cylinder pipeline section is circumferentially uniformly provided with multiple upper material distribution tooth, the lower port of described Taper Pipe section is supported on the inwall of described precondensation room film supplying tube and is circumferentially uniformly provided with multiple lower material distribution tooth.

Fat polymerization two kettle device the most according to claim 6, it is characterized in that: the annulus of guide breather periphery, described precondensation room is provided with precondensation room radially diaphragm, described precondensation room flash mouth and described precondensation room charging aperture lay respectively at the both sides of described precondensation room radially diaphragm；The curved bottom of described mixing chamber is provided with mixing chamber thermometer boss and mixing chamber interface of the level gauge, and the aperture of described mixing chamber fluid level control valve is controlled by the liquid level of described mixing chamber；The curved bottom of described esterification room is provided with esterification room temperature meter interface and esterification room interface of the level gauge, and the aperture of described esterification room fluid level control valve is controlled by the liquid level of described esterification room；The lower sides of described precondensation room is provided with precondensation room temperature meter interface and precondensation room interface of the level gauge, and the flow rates controlled of described precondensation melt delivery pump is in the liquid level of described precondensation room.

Fat polymerization two kettle device the most according to claim 1, it is characterized in that: the described cloth liquid dish without stirring polymer reactor is 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.

Fat polymerization two kettle device the most according to claim 1, it is characterized in that: the described cylinder inboard wall without stirring polymer reactor 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；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.