CN106268591A - A kind of polymerization reaction kettle and method for making polyester - Google Patents
A kind of polymerization reaction kettle and method for making polyester Download PDFInfo
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- CN106268591A CN106268591A CN201610848575.8A CN201610848575A CN106268591A CN 106268591 A CN106268591 A CN 106268591A CN 201610848575 A CN201610848575 A CN 201610848575A CN 106268591 A CN106268591 A CN 106268591A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/18—Stationary reactors having moving elements inside
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0053—Details of the reactor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0053—Details of the reactor
- B01J19/0066—Stirrers
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
- C08G63/78—Preparation processes
- C08G63/785—Preparation processes characterised by the apparatus used
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
- B01J2219/00092—Tubes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
- B01J2219/00094—Jackets
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- Chemical Kinetics & Catalysis (AREA)
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- Health & Medical Sciences (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Other Resins Obtained By Reactions Not Involving Carbon-To-Carbon Unsaturated Bonds (AREA)
- Polyesters Or Polycarbonates (AREA)
Abstract
The invention discloses a kind of polymerization reaction kettle and method for making polyester.Polymerization reaction kettle includes the horizontal cylinder sealed, and in cylinder, material inlet is provided with front end rotating shaft, and one end of front end rotating shaft is stretched out from cylinder and is connected with power set one；In cylinder, material outlet being provided with rear end rotating shaft, one end of rear end rotating shaft is stretched out from cylinder and is connected with power set two；Supporting front end rotating shaft and the supporting construction of rear end rotating shaft it is provided with in cylinder；Cage gate stirrer it is provided with in the rotating shaft of front end；At the rotating shaft of front end, it is provided with one section of spiral disk in the rotating shaft of rear end；Rear end rotating shaft remainder is provided with the annulus that many groups are coaxial, is often provided with the some scrapers parallel with anchor ring between group annulus.Method is to utilize above-mentioned polymerization reaction kettle to carry out production of polyester to obtain high-viscosity polyester melt.Cage gate stirrer is arranged on front end by the present invention, is arranged on rear end by organizing annulus more, it is possible to be effectively improved the devolatilization efficiency of equipment.
Description
Technical field
The invention belongs to polyester producing process field, relate to the visual plant of a kind of production of polyester, use particularly to one
Polymerization reaction kettle and method for making polyester in production of polyester.
Background technology
Polymerization reaction kettle is the visual plant of production of polyester.The Chinese patent of Publication No. CN201684605U
(CN201020175319.5) disclosing the combination type polymerization reaction kettle in a kind of polyester production device field, it includes sealing
Horizontal cylinder, described cylinder one end is provided with material inlet, and the other end is provided with material outlet, and described cylinder is arranged over gas phase and goes out
Mouthful, it being provided with rotating shaft one in cylinder, rotating shaft one is provided with organizes disk more, and the end of rotating shaft one is stretched out from one end of cylinder；Described turn
Axle one is arranged on material inlet one end；Being additionally provided with rotating shaft two near material outlet one end in cylinder, described rotating shaft two is from cylinder
The other end stretches out, and is additionally provided with supporting rotating shaft one and the supporting device of rotating shaft two in cylinder；Rotating shaft two is provided with squirrel-cage agitator.
Arranging of disk can make material stirring abundant, reaches the effect of laminar flow reaction, and material is had well by squirrel-cage agitator
Stir into membrane interaction, the evaporation surface of material is significantly greatly increased, the further polycondensation of material can be promoted.
There is the inefficient defect of devolatilization in above-mentioned CN201020175319.5 patent during actual production uses, former
Because of as follows: according to material distribution in polymerization reaction kettle, front equipment end material viscosity is less, good fluidity, the closer to rear end,
Material viscosity is the biggest, and mobility is the poorest；Due in the rotating shaft one of front end for organize disk more, the rotating shaft two of rear end is stirred for squirrel-cage
Mix device；In polymerization reaction kettle, the low viscosity material of front end has flowing velocity faster on disk, and film forming area is little, time
Between short, simultaneously because the mobility of material own is preferable, by action of gravity, is difficult to the top half at disk and dividing plate and is formed effectively
Film, causes devolatilization efficiency low；And due to the internal complicated component of squirrel-cage agitator, the high-viscosity material of rear end is the most very
Difficulty only relies on deadweight and flows down and film forming.
Summary of the invention
It is an object of the invention to, overcome the deficiencies in the prior art, it is provided that a kind of devolatilization effect that can be effectively improved equipment
The polymerization reaction kettle of rate and method for making polyester.
It is an object of the invention to be achieved through the following technical solutions:
A kind of polymerization reaction kettle, it includes the horizontal cylinder sealed, and described cylinder one end is provided with material inlet, and the other end sets
There is material outlet；Described cylinder is provided with gaseous phase outlet and is connected with vacuum system；In cylinder, material inlet is provided with front end
Rotating shaft, one end of front end rotating shaft is stretched out from cylinder and is connected with power set one；In cylinder, material outlet is provided with rear end
Rotating shaft, one end of rear end rotating shaft is stretched out from cylinder and is connected with power set two；Front end rotating shaft, rear end rotating shaft are respectively by machinery
Seal and be connected with cylinder；Supporting front end rotating shaft and the supporting construction of rear end rotating shaft it is provided with in cylinder；It is provided with cage in the rotating shaft of front end
Gate stirrer；At the rotating shaft of front end, it is provided with one section of spiral disk in the rotating shaft of rear end；Rotating shaft remainder in rear end is arranged
There is the annulus that many groups are coaxial.
Further, it is provided with the some scrapers parallel with anchor ring between annulus often organizing in described cylinder, described
Scraper is fixing with cylinder to be connected.The effect of scraper is to make high-viscosity material film forming on annulus.
Further, described scraper radially has certain angle with cylinder, and this angle is between 30 degree to 60 degree.
Further, described often group annulus is made up of the annulus of several different-diameters, the annulus of several different-diameters
In the same plane, and all connect by intermediate support is fixing；During intermediate support includes that a center ring and one end are fixed on
Many support bars on thimble, center ring is fixed in the rotating shaft of rear end, and the annulus of several different-diameters is fixed on many supports
On bar.The number of annulus can be determined: the less (cylinder of equipment size according to the size (size of barrel diameter) of concrete equipment
Diameter is little) time, it is possible to use single annulus；During equipment size big (barrel diameter is big), as used single annulus, then material is at list
It is difficult to film forming, it is necessary to increase number of rings, use the annulus of multiple different-diameter, to reduce single shaping above individual annulus
The area of film, beneficially material film forming devolatilization.
Further, being provided with scraper plate outside described cage gate stirrer, scraper plate and cylinder axially have certain angle,
This angle is between 0 degree to 5 degree.
Further, described cage gate stirrer is slightly larger than other end diameter near material inlet one end diameter.
Further, described cylinder is Double-layer clamp shell type heat tracing cylinder, cylinder be provided with heating agent entrance and heating agent outlet with
Jacket space connects.
Further, outside described cylinder, it is provided with heating coil, heating coil is provided with heating agent entrance, heating agent outlet
And air vent；Heating coil cross section can be random geometry.
Further, part cylinder is Double-layer clamp shell type heat tracing cylinder, and this part cylinder is provided with heating agent entrance and heating agent
Outlet connects with jacket space；It is provided with heating coil outside another part cylinder, heating coil is provided with heating agent entrance, heat
Matchmaker's outlet and air vent.
The material feedstock characteristic viscosity that described polymerization reaction kettle is suitable for is 0.15dL/g～0.40dL/g；The temperature being suitable for is
260 DEG C～295 DEG C；The pressure being suitable for is absolute pressure 0Pa～2000Pa；Feedstock characteristic viscosity is 0.15dL/g～0.40dL/g
Material, in this polymerization reaction kettle reaction stop 50min～150min, discharging intrinsic viscosity can reach 0.6dL/g～
1.0dL/g。
A kind of method utilizing above-mentioned polymerization reaction kettle to carry out production of polyester is as follows: be 0.15dL/g by material characteristic viscosity
～the polyester fondant of 0.40dL/g, be continuously introduced into above-mentioned polymerization reaction kettle, temperature 260 DEG C～295 DEG C, absolute pressure 0Pa～
React 50min～150min under conditions of 2000Pa, prepare the polyester fondant that intrinsic viscosity is 0.6dL/g～1.0dL/g.
Further, by the polyester fondant that material characteristic viscosity is 0.15dL/g～0.40dL/g, it is continuously introduced into above-mentioned poly-
Close reactor, temperature 270 DEG C～280 DEG C, under conditions of absolute pressure 100Pa～1000Pa, react 50min～150min, system
For obtaining the polyester fondant that intrinsic viscosity is 0.6dL/g～1.0dL/g.
Beneficial effects of the present invention:
The polymerization reaction kettle of the present invention, is arranged on front end by cage gate stirrer, and low viscosity material can be made to be sufficiently stirred for
And reach film-formation result, increase material devolatilization area, improve rate of polymerization, increase material viscosity；After cage gate stirrer
One section of spiral disk is set, it is possible to effectively promote material to move to discharge end；It is arranged on rear end, energy by organizing several annulus more
The further polycondensation of high-viscosity material is enough promoted (to make high-viscosity material can form effective film, and film forming area on each annulus
Greatly, thus it is effectively increased devolatilization area, has reached Efficient Adhesive Promotion).This device devolatilization efficiency is high, it is possible to ensure polyreaction
Speed is fast, and the material viscosity scope being suitable for is wide, can be used for the production of various polyester.
The present invention, compared with prior art (CN201020175319.5 patent), has the advantage that
(1) cage gate stirrer is arranged on front end, has bigger benefit than being arranged on rear end.
Cage gate stirrer be utilize material to be brought in cage frame after, material rely on deadweight along cage frame dirty naturally one-tenth
Film, thus increase material devolatilization area.Carry out film forming owing to it only relies on material deadweight, it requires that material viscosity can not be too big,
Otherwise relying on material deadweight dirty too slow, film forming difficulty, efficiency is low.According to material distribution in polymerization reaction kettle, poly-
Closing in reactor, the closer to material inlet section (front equipment end), material viscosity is the lowest, the closer to material outlet section (after equipment
End), material viscosity is the highest.
Cage gate stirrer is arranged on front end by the present invention, then the low viscosity material of front end is easier in cage frame rely on certainly
Under density current and film forming, thus it is effectively improved devolatilization area, reaches Efficient Adhesive Promotion.Therefore, cage gate stirrer is arranged by the present invention
In front end, it is possible to be effectively improved the devolatilization efficiency of equipment.
And in CN201020175319.5 patent, squirrel-cage agitator is arranged on rear end, due to squirrel-cage agitator
Internal complicated component, the high-viscosity material of rear end is difficult to only rely on deadweight in the above and flows down and film forming.
(2) it is arranged on rear end by organizing annulus more, has bigger benefit than being arranged on front end.
In CN201020175319.5 patent, for organize disk in the rotating shaft one of front end, due in polymerization reaction kettle more,
The low viscosity material of front end has flowing velocity faster on disk, and film forming area is little, and the time is short, simultaneously because material itself
Mobility is preferable, by action of gravity, is difficult to the top half at disk and dividing plate and forms effective film, cause devolatilization efficiency low.
And in the present invention, be arranged on rear end by organizing annulus more, due in polymerization reaction kettle, the high-viscosity material of rear end by
Big in viscosity, it has slower flowing velocity on annulus, and film forming area is big, and the time is long, adds the effect of upper blade, makes material
On each annulus and often can form effective film between the multiple annulus on group annulus, thus be effectively increased devolatilization face
Long-pending, reach Efficient Adhesive Promotion.Therefore, the present invention is arranged on rear end by organizing annulus more, it is possible to be effectively improved the devolatilization efficiency of equipment,
Improve discharging viscosity.
(3) become to organize annulus by reactor back end design, the benefit bigger than being designed to many groups disk more.
Reactor back end design is become the many groups of annulus being made up of the annulus of several different-diameters by the present invention, makes material
Film forming between the annulus of multiple different-diameters, two faces of the surfaces externally and internally of the film of formation can devolatilization, which increases
Devolatilization area；And in CN201020175319.5 patent, film forming on many group disks, then the film formed only has inner surface one
Face can be with devolatilization, and devolatilization area is relatively small.Therefore, reactor back end design is become to organize annulus by the present invention more, it is possible to effectively carry
High devolatilization area, thus it is effectively improved the devolatilization efficiency of equipment, improve discharging viscosity.
Accompanying drawing explanation
Fig. 1 is the main TV structure schematic diagram of a kind of polymerization reaction kettle of the present invention；
Fig. 2 is the side-looking structural representation often organizing annulus 6 in the present invention；
Fig. 3 is the distribution schematic diagram (side-looking) of the scraper 7 in the present invention in approximately the same plane.
In figure: 1 material inlet, 2 cage gate stirrers, 3 scraper plates, 4 front end rotating shafts, 5 spiral disks, 6 annulus, 61 great circles
Ring, 62 small circle rings, 7 scrapers, 8 rear end rotating shafts, 9 supporting constructions, 10 material outlets, 11 heating agent entrances, 12 heating agent outlets, 13 gas phases
Outlet, 14 support bars, 15 center rings.
Detailed description of the invention
Below in conjunction with drawings and Examples, the present invention is further illustrated.
Embodiment 1
As it is shown in figure 1, one polymerization reaction kettle of the present invention, it includes the horizontal cylinder sealed, and described cylinder one end is provided with
Material inlet 1, the other end is provided with material outlet 10；Described cylinder is provided with gaseous phase outlet 13 and is connected with vacuum system；In cylinder
Material inlet is provided with front end rotating shaft 4, and one end of front end rotating shaft is stretched out from cylinder and is connected with power set one；In cylinder
Material outlet is provided with rear end rotating shaft 8, and one end of rear end rotating shaft is stretched out from cylinder and is connected with power set two；Front end turns
Axle, rear end rotating shaft are connected with cylinder by mechanical seal respectively；Supporting front end rotating shaft and the support of rear end rotating shaft it is provided with in cylinder
Structure 9；Cage gate stirrer 2 it is provided with in the rotating shaft of front end；At the rotating shaft of front end, one section it is provided with spirally in the rotating shaft of rear end
Disk 5；Rear end rotating shaft remainder is provided with the annulus 6 that many groups are coaxial.
As it is shown on figure 3, be provided with three scrapers 7 parallel with anchor ring between annulus often organizing in described cylinder, three
Scraper 7 is fixing with cylinder to be connected.Article three, scraper 7 radially has certain angle with cylinder, and this angle is between 30 degree to 60 degree.
As in figure 2 it is shown, described often group annulus 6 is by annulus (i.e. large circle 61 and the small circle ring 62) group of two different-diameters
Becoming, the annulus of two different-diameters is in the same plane, and all by the fixing connection of intermediate support, (intermediate support includes one
Three support bars 14 that center ring 15 and one end are fixed on center ring 15, center ring 15 is fastened in rear end rotating shaft 8, large circle
61 and small circle ring 62 be fixed on three support bars 14).It is empty between large circle 61 and small circle ring 62.High-viscosity material is two
Thin film, beneficially material devolatilization is formed on individual annulus and between two annulus.High-viscosity material is from large circle 61 and small circle ring 62
Between by time, owing to material viscosity is big, material has slower flowing velocity on annulus, adds the effect of upper blade, makes thing
Material can form effective film on each annulus and between two annulus, and film forming area is big, and the time is long, the most effectively carries
High devolatilization area, has reached Efficient Adhesive Promotion.
As it is shown in figure 1, be provided with scraper plate 3 outside described cage gate stirrer, scraper plate and cylinder axially have certain folder
Angle, this angle is between 0 degree to 5 degree.Described cage gate stirrer is slightly larger than other end diameter near material inlet one end diameter.
Described cylinder leading portion (being i.e. provided with the part cylinder of cage gate stirrer) outside is provided with heating coil, adds hot plate
Tube section can be random geometry, and heating coil is provided with heating agent entrance 11, heating agent outlet 12 and air vent.Described cylinder
Back segment (being i.e. provided with the part cylinder organizing annulus) is Double-layer clamp shell type heat tracing cylinder more, and cylinder is provided with heating agent entrance 11 and heat
Matchmaker exports 12 and connects with jacket space.
Barrel front end and rear end are equipped with temperature sensor and pressure transducer (in Fig. 1 the upper left corner and the upper right corner shown in).
The material feedstock characteristic viscosity that described polymerization reaction kettle is suitable for is 0.15dL/g～0.40dL/g；The temperature being suitable for is
260 DEG C～295 DEG C；The pressure being suitable for is absolute pressure 0Pa～2000Pa；Be suitable for the time of staying be: 50min～150min；
This polymerization reaction kettle discharging intrinsic viscosity reaches 0.6dL/g～1.0dL/g.
Embodiment 2
A kind of method utilizing polymerization reaction kettle described in embodiment 1 to carry out production of polyester is as follows:
It is the polyester fondant of 0.25dL/g by material characteristic viscosity, is continuously introduced into above-mentioned polymerization reaction kettle, in temperature 275
DEG C, react 150min under conditions of absolute pressure 400Pa, prepare the polyester fondant that intrinsic viscosity is 0.87dL/g.
Embodiment 3
A kind of method utilizing polymerization reaction kettle described in embodiment 1 to carry out production of polyester is as follows:
It is the polyester fondant of 0.40dL/g by material characteristic viscosity, is continuously introduced into above-mentioned polymerization reaction kettle, in temperature 270
DEG C, react 150min under conditions of absolute pressure 250Pa, prepare the polyester fondant that intrinsic viscosity is 1.0dL/g.
Embodiment 4
A kind of method utilizing polymerization reaction kettle described in embodiment 1 to carry out production of polyester is as follows:
It is the polyester fondant of 0.21dL/g by material characteristic viscosity, is continuously introduced into above-mentioned polymerization reaction kettle, in temperature 265
DEG C, react 60min under conditions of absolute pressure 100Pa, prepare the polyester fondant that intrinsic viscosity is 0.67dL/g.
Embodiment 5
A kind of method utilizing polymerization reaction kettle described in embodiment 1 to carry out production of polyester is as follows:
It is the polyester fondant of 0.15dL/g by material characteristic viscosity, is continuously introduced into above-mentioned polymerization reaction kettle, in temperature 260
DEG C, react 50min under conditions of absolute pressure 0Pa, prepare the polyester fondant that intrinsic viscosity is 0.6dL/g.
Embodiment 6
A kind of method utilizing polymerization reaction kettle described in embodiment 1 to carry out production of polyester is as follows:
It is the polyester fondant of 0.32dL/g by material characteristic viscosity, is continuously introduced into above-mentioned polymerization reaction kettle, in temperature 280
DEG C, react 120min under conditions of absolute pressure 1000Pa, prepare the polyester fondant that intrinsic viscosity is 0.91dL/g.
Embodiment 7
A kind of method utilizing polymerization reaction kettle described in embodiment 1 to carry out production of polyester is as follows:
It is the polyester fondant of 0.25dL/g by material characteristic viscosity, is continuously introduced into above-mentioned polymerization reaction kettle, in temperature 295
DEG C, react 90min under conditions of absolute pressure 2000Pa, prepare the polyester fondant that intrinsic viscosity is 0.78dL/g.
Claims (10)
1. a polymerization reaction kettle, it include seal horizontal cylinder, described cylinder one end is provided with material inlet, and the other end is provided with
Material outlet；Described cylinder is provided with gaseous phase outlet and is connected with vacuum system；It is characterized in that: set near material inlet in cylinder
Being equipped with front end rotating shaft, one end of front end rotating shaft is stretched out from cylinder and is connected with power set one；Set near material outlet in cylinder
Being equipped with rear end rotating shaft, one end of rear end rotating shaft is stretched out from cylinder and is connected with power set two；Front end rotating shaft, rear end rotating shaft are respectively
It is connected with cylinder by mechanical seal；Supporting front end rotating shaft and the supporting construction of rear end rotating shaft it is provided with in cylinder；In the rotating shaft of front end
It is provided with cage gate stirrer；At the rotating shaft of front end, it is provided with one section of spiral disk in the rotating shaft of rear end；Rear end rotating shaft remaining
Part is provided with the annulus that many groups are coaxial.
2. polymerization reaction kettle as claimed in claim 1, it is characterised in that if being provided with between annulus often organizing in described cylinder
The scraper that dry bar is parallel with anchor ring, described scraper is fixing with cylinder to be connected；Described scraper radially has certain angle with cylinder,
This angle is between 30 degree to 60 degree.
3. polymerization reaction kettle as claimed in claim 1 or 2, it is characterised in that described often group annulus is by several different-diameters
Annulus composition, the annulus of several different-diameters is in the same plane, and all by the fixing connection of intermediate support；Middle
Frame includes the many support bars that a center ring and one end are fixed on center ring, and center ring is fixed in the rotating shaft of rear end, some
The annulus of individual different-diameter is fixed on many support bars.
4. polymerization reaction kettle as claimed in claim 1 or 2, it is characterised in that be provided with outside described cage gate stirrer and scrape
Plate, scraper plate and cylinder axially have certain angle, and this angle is between 0 degree to 5 degree.
5. polymerization reaction kettle as claimed in claim 1 or 2, it is characterised in that described cage gate stirrer is near material inlet
One end diameter is slightly larger than other end diameter.
6. polymerization reaction kettle as claimed in claim 1 or 2, it is characterised in that described cylinder is Double-layer clamp shell type heat tracing cylinder,
Cylinder is provided with heating agent entrance and connects with jacket space with heating agent outlet.
7. polymerization reaction kettle as claimed in claim 1 or 2, it is characterised in that be provided with heating coil outside described cylinder, add
Heating agent entrance, heating agent outlet and air vent it is provided with on hot coil；Heating coil cross section is random geometry.
8. polymerization reaction kettle as claimed in claim 1 or 2, it is characterised in that part cylinder is Double-layer clamp shell type heat tracing cylinder,
This part cylinder is provided with heating agent entrance and connects with jacket space with heating agent outlet；It is provided with outside another part cylinder and adds hot plate
Pipe, heating coil is provided with heating agent entrance, heating agent outlet and air vent.
9. polymerization reaction kettle as claimed in claim 1 or 2, it is characterised in that the material charging that described polymerization reaction kettle is suitable for
Intrinsic viscosity is 0.15dL/g～0.40dL/g；The temperature being suitable for is 260 DEG C～295 DEG C；The pressure being suitable for is absolute pressure 0Pa
～2000Pa；Feedstock characteristic viscosity is the material of 0.15dL/g～0.40dL/g, and in this polymerization reaction kettle, reaction stops 50min
～150min, discharging intrinsic viscosity can reach 0.6dL/g～1.0dL/g.
10. utilizing the method that the polymerization reaction kettle as described in claim 1-9 is arbitrary carries out production of polyester, its feature exists
In, by the polyester fondant that material characteristic viscosity is 0.15dL/g～0.40dL/g, it is continuously introduced into above-mentioned polymerization reaction kettle, in temperature
260 DEG C～295 DEG C, reacting 50min～150min under conditions of absolute pressure 0Pa～2000Pa, preparing intrinsic viscosity is
The polyester fondant of 0.6dL/g～1.0dL/g.
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| CN201610848575.8A CN106268591B (en) | 2016-09-23 | 2016-09-23 | A kind of polymerization reaction kettle and method for making polyester |
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| CN201610848575.8A CN106268591B (en) | 2016-09-23 | 2016-09-23 | A kind of polymerization reaction kettle and method for making polyester |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107051355A (en) * | 2017-03-30 | 2017-08-18 | 山东里德工程技术有限公司 | A kind of single shaft self-cleaning reactor |
| CN110270289A (en) * | 2019-07-02 | 2019-09-24 | 中国科学院过程工程研究所 | A kind of superelevation sealing polycarbonate reaction unit |
| CN110280202A (en) * | 2019-06-18 | 2019-09-27 | 中国科学院过程工程研究所 | A kind of final polycondensation reactor preparing polycarbonate |
| CN111545152A (en) * | 2020-04-24 | 2020-08-18 | 浙江恒澜科技有限公司 | Disc reactor with scraper device |
| CN111701553A (en) * | 2020-05-19 | 2020-09-25 | 浙江恒澜科技有限公司 | Polymerization reactor suitable for high-viscosity PTT production |
| CN113797872A (en) * | 2020-06-11 | 2021-12-17 | 中国石油化工股份有限公司 | Final polycondensation reactor and method for producing polyester |
| CN113797850A (en) * | 2020-06-11 | 2021-12-17 | 中国石油化工股份有限公司 | Cage frame type final polycondensation reactor and method for producing polyester |
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| CN110270289A (en) * | 2019-07-02 | 2019-09-24 | 中国科学院过程工程研究所 | A kind of superelevation sealing polycarbonate reaction unit |
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| CN111701553A (en) * | 2020-05-19 | 2020-09-25 | 浙江恒澜科技有限公司 | Polymerization reactor suitable for high-viscosity PTT production |
| CN113797872A (en) * | 2020-06-11 | 2021-12-17 | 中国石油化工股份有限公司 | Final polycondensation reactor and method for producing polyester |
| CN113797850A (en) * | 2020-06-11 | 2021-12-17 | 中国石油化工股份有限公司 | Cage frame type final polycondensation reactor and method for producing polyester |
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