CN2767447Y - Highly efficient simplified apparatus for producing polyethylene terephthalate - Google Patents
Highly efficient simplified apparatus for producing polyethylene terephthalate Download PDFInfo
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- CN2767447Y CN2767447Y CN 200520002231 CN200520002231U CN2767447Y CN 2767447 Y CN2767447 Y CN 2767447Y CN 200520002231 CN200520002231 CN 200520002231 CN 200520002231 U CN200520002231 U CN 200520002231U CN 2767447 Y CN2767447 Y CN 2767447Y
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Abstract
The utility model discloses a high efficiency simplified apparatus for producing polyethylene terephthalate, which comprises a first esterification reactor, a second esterification reactor, a pre-polycondensation reactor and a post-polycondensation reactor, wherein a material outlet under the first esterification reactor is communicated with an outer chamber of the second esterification reactor, a material outlet of the second esterification reactor is communicated with an upper cavity body of the pre-polycondensation reactor, and a prepolymer outlet of the pre-polycondensation reactor is communicated with a material inlet of the post-polycondensation reactor. The high efficiency simplified apparatus for producing polyethylene terephthalate of the utility model adopting two stages of esterification processes and two stages of polycondensation reaction processes causes the whole process to have the advantages of simple and direct processes, high production efficiency and cost reduction; every technical index of the utility model is superior to that of a device in the same kind.
Description
Technical field
The utility model relates to the efficient simplification device of a kind of production polyethylene terephthalate (PET).
Background technology
Along with being extensive use of of polyethylene terephthalate (PET), its production equipment and technology have also been proposed corresponding requirement, though it is more to produce the industrialized unit and the technology of polyethylene terephthalate at present, as disclosed " production method of polyester " in No. the 97122449.8th, disclosed " continuous condensed method and apparatus " in No. the 97197662.7th, the Chinese patent and the Chinese patent, but problem such as production equipment in these patents and technology all yield poorly because of the unreasonable structure of each reactor has in actual use, production cost height.
For this reason, creator in the utility model relies on it to be engaged in the experience and the practice of relevant industries for many years, and, create a kind of efficient simplification device of the production polyethylene terephthalate that can effectively enhance productivity and reduce cost finally through concentrating on studies and developing.
Summary of the invention
Main purpose of the present utility model is to provide a kind of efficient simplification device of producing polyethylene terephthalate, and this device has improved the unreasonable structure of existing production equipment, effectively enhances productivity and reduces cost.
Produce the efficient simplification device of polyethylene terephthalate in the utility model, include first, second esterifier, Prepolycondensating reactor and final polycondensation reactor, the material outlet of the described first esterifier bottom is connected with the mistress of described second esterifier, the material outlet of described second esterifier is communicated with the upper cavity of described Prepolycondensating reactor, the prepolymer outlet of described Prepolycondensating reactor is connected with the material inlet of final polycondensation reactor, described second esterifier part within it wherein is provided with heating agent coil pipe and the whipping appts that is driven by external force every mistress and inner room that formation communicates in inner room;
Described first esterifier is a hybrid power outer circulation type esterifier, include inhomogeneous reaction device, evaporation reaction device and Power Drive Unit, described inhomogeneous reaction device includes the reactor of setting up formula tubulation heat-exchanger rig in one, the outlet of this reactor is connected with described evaporation reaction device, and inlet is connected with the opening for feed of reaction mass and the bottom of evaporation reaction device; Described evaporation reaction device includes an airtight housing, on the top of enclosure interior is evaporating area, the bottom is a reaction zone, be provided with gaseous phase outlet at its top, the bottom is extended with a diversion section, be provided with at least one flow deflector in this diversion section, this evaporation reaction device and described reactor constitute the loop of a sealing; Described Power Drive Unit includes the driving mechanism that is located at described evaporation reaction device outside, the axial-flow type whipping appts that is hubbed on described diversion section inside, and this axial-flow type whipping appts connects with described driving mechanism by axle;
Described Prepolycondensating reactor includes a upper cavity and a lower chamber, be provided with the whipping appts that drives by external force in lower chamber inside, upper cavity and lower chamber are isolated cylindrical shell by one and are combined in the airtight housing, described upper cavity is provided with a material inlet, and is provided with heating coil in this upper cavity inside; The top of described lower chamber is provided with exhaust-duct, the bottom of extending outside the described housing and is provided with pipeline and the prepolymer outlet that is communicated with described upper cavity bottom, and the inner bottom part at this lower chamber is provided with heating coil simultaneously; On described isolation cylindrical shell, offer a slit, and this slit place is provided with arc plate toward inner extension of described lower chamber, this arc plate forms one with described isolating cylinder body and is used to be communicated with the crooked swirling flow passage of described upper cavity and lower chamber, and is provided with one at described slit place and is used to regulate the variable valve of slit size;
Described final polycondensation reactor includes the rounded or oblong pressure-bearing type cylindrical shell of cross section of a sealing, and this cylindrical shell is provided with material inlet and material outlet, and is provided with the agitator that can form vertical film and parallel membrane in inner barrel.
Be five flow aprons that positive pentagon distributes by being welded with in the described first esterifier diversion section, and left the space that is used to put described axial-flow type whipping appts middle the blocking of every flow deflector.
The side that the upper cavity inside of described Prepolycondensating reactor is positioned at slit is provided with one and is used for the flow deflector that pilot-gas flows to.
The agitator of described final polycondensation reactor inside includes two drive shafts and many group disk rings, the center of circle that is centered close to cylindrical shell of described drive shaft or down round center, described disk ring is separately fixed on two drive shafts, and described ring dish is installed with the parallel axial membrane steel plate of polylith at its sidepiece.
Drive shaft in the described final polycondensation reactor is a tubular shaft.
Described disk ring is by being welded be that regular hexagon distributes six radially membrane plate back up pads, and every radially membrane plate and adjacent ring dish are integrally welded.
The efficient simplification device of producing polyethylene terephthalate in the utility model adopts two sections esterifications and two sections polycondensation processes, make whole technology have the advantage that simple and direct, the every technical indicator of flow process all is better than same device, can effectively enhance productivity and reduce cost.
Description of drawings
Fig. 1 is a rough schematic view of producing the efficient simplification device of polyethylene terephthalate in the utility model;
Fig. 2 is the structural representation of first esterifier in the utility model;
Fig. 3 is the structural representation of Prepolycondensating reactor in the utility model;
Fig. 4 is the horizontal cross-sectional schematic of Prepolycondensating reactor in the utility model;
Fig. 5 is the structural representation of final polycondensation reactor in the utility model;
Fig. 6 is the horizontal cross-sectional schematic of final polycondensation reactor in the utility model.
Embodiment
The specific embodiment of the utility model is described in further detail below in conjunction with accompanying drawing.
As shown in Figure 1, the efficient simplification device of production polyethylene terephthalate includes the first esterifier A, the second esterifier B, Prepolycondensating reactor C and final polycondensation reactor D in the utility model.
As shown in Figure 2, the first esterifier A is a hybrid power outer circulation type polyester esterification reactor, includes inhomogeneous reaction device 1, evaporation reaction device 2 and Power Drive Unit 3, wherein:
Evaporation reaction device 2 includes an airtight housing 20, outside housing 20, be provided with a liquid phase heating agent chuck 26 with heat insulation function, these housing 20 inside can be divided into the evaporating area 21 on top and the reaction zone 22 of bottom in reaction process, be provided with gaseous phase outlet 23 at its top, the bottom is extended with a diversion section 24 in integrally formed mode, be provided with five by welding or other fixedly connected mode on the inwall of this diversion section 24 and be the baffle plate 25 that positive pentagon distributes, and each baffle plate 25 is all by the space of blocking and being formed for putting axial-flow type whipping appts 30, utilize this baffle plate 25 can destroy liquid formed whirlpool under 30 effects of axial-flow type whipping appts, thereby guarantee that liquid is toward current downflow.
Inhomogeneous reaction device 1 includes the reactor 10 that an inside is provided with vertical tubulation heat-exchanger rig 16, the outlet of this reactor 10 is connected with the evaporating area 21 on evaporation reaction device 2 tops by water conservancy diversion top cover 11, inhomogeneous reaction thing outlet pipe 12, inlet 17 is a guiding cone of standing upside down, and has the function of homogeneous mixture of material.This inlet 17 is connected by the diversion section 24 of a U-shaped pipe 14 with evaporation reaction device 2 bottoms, thereby constitute the loop of a sealing by inhomogeneous reaction device 1 and evaporation reaction device 2, end at U-shaped pipe 14 close reactor 10 inlets 17 is provided with a material inlet 13, is provided with a material outlet 15 at the end near evaporation reaction device 2.The entry and exit 18,19 of vertical tubulation heat-exchanger rig 16 are connected with extraneous liquid phase heating agent heating tube (not shown), utilize the liquid phase heating agent can the material that enter reactor 10 inside be heated.In order to prevent the loss of heat, also be arranged with liquid phase heating agent chuck with the outside of inhomogeneous reaction thing outlet pipe 12 with heat insulation function at reactor 10, U-shaped pipe 14, top cover 11.
Power Drive Unit 3 includes the driving mechanism 31 that is located at evaporation reaction device 2 tops, parallel two the axial-flow type whipping apptss 30 (also can be one or more) that are hubbed on evaporation reaction device diversion section 24 inside by same axle 32 drivings, this axial-flow type whipping appts 30 connects with driving mechanism 31 by axle 32, and in the junction of axle 32 and housing 20 for being tightly connected.
As shown in Figure 1, the second esterifier B includes a housing 4, these housing 4 inside are divided into mistress 41 and inner room 42 by an inner core 40, wherein mistress 41 is connected with the material outlet 15 of the first esterifier A, in inner room 42, be provided with heating agent heating coil 43 and the whipping appts 44 that drives by external force, heating coil 43 is connected with extraneous liquid phase heating agent, and can carry out heat exchange to material.Inner room 41 bottoms of this second esterifier B are connected with the material inlet 510 of Prepolycondensating reactor C upper cavity.Therefore this second esterifier B describes in detail its concrete structure and principle of work no longer separately owing to adopt the esterifier that has now in the production equipment.
As shown in Figure 3 and Figure 4, Prepolycondensating reactor C includes an airtight housing 5, this housing 5 portion within it is separated into upper cavity 51 that is atmospheric pressure state and the lower chamber 52 that is vacuum state by an isolation cylindrical shell 50, wherein upper cavity 51 is around in the top in lower chamber 52 outsides, and being provided with a whipping appts 53 in lower chamber 52 inside, this whipping appts 53 is driven by axle 54 and the drive unit 55 that is located at housing 5 tops.
As shown in Figure 4, a side that is positioned at slit 500 in upper cavity 51 inside is provided with a flow deflector 504, utilize this flow deflector 504 that upper cavity 51 gas inside are flowed along assigned direction, and enter in the crooked swirling flow passage 502, utilize the setting of this flow deflector 504 and crooked swirling flow passage 502, can effectively strengthen separating of gas phase and liquid phase, make gas phase enter exhaust gas processing device by exhaust-duct 59, liquid phase then falls into lower chamber 52 and carries out polycondensation.
As shown in Figure 5 and Figure 6, final polycondensation reactor D includes an airtight rounded or oblong cylindrical shell 6 of cross section, this cylindrical shell 6 is horizontal setting, and be provided with a material inlet 60 and a material outlet 61 respectively at both ends, this reactor also includes one makes air communication cross the air feeder (not shown) of inside reactor, to utilize air-flow to take away ethylene glycol and water molecules fast,, no longer describe in detail at this because this part-structure is a prior art.Between the end cap at cylindrical shell 6 both ends, be pivoted with two hollow drive shafts 62,68, this two drive shaft 62,68 all is positioned at the center of circle or the following circle centre position of cylindrical shell 6, wherein an end of each drive shaft 62,68 extends the both ends of cylindrical shell 6 respectively and connects with transmission mechanism, motor, and by electric motor driving.At drive shaft 62,68 parallel being installed with in position that are positioned at cylindrical shell 6 inside are organized ring dishes 63 more, constitute the agitator that is located at cylindrical shell 6 inside by this two drive shaft and many group disk rings, as shown in Figure 6, ring dish 63 is six radially membrane plate 65 supports that regular hexagon distributes by being welded with, every radially membrane plate 65 is integrally welded with adjacent ring dish 63, in addition radially be welded with the axial membrane steel plate 66 of polylith on membrane plate 65 and the disk ring 63 at each, on the inwall of cylindrical shell 6, adopt slot to be connected with the scraper plate (not shown) simultaneously, by adjusting scraper plate and axial membrane steel plate 66, the thickness of liquid film 67 is controlled in gap between the ring dish 63, final polycondensation reactor in the utility model is owing to adopt tubular shaft and separable ring dish structure, and many disadvantages of solid shaft disc type agitator and cage agitator have been overcome, and use the film (abbreviation vertical film) that can form behind this agitator perpendicular to air flow line in the reactor, and be parallel to the film (abbreviation parallel membrane) of air flow line in the reactor, increased the amount of unit agitator action space belongings feed liquid film, increase the mass transfer area of reactor, effectively raised stirring efficiency.In addition, the rigidity of this final polycondensation reactor is strengthened, and can obviously reduce the metal consumption of agitator, has improved the reliability of agitator.
The production process of the device of production polyethylene terephthalate is as follows in the utility model:
Raw material EG and PTA are mixed with fresh oar material by certain mol proportion at 1.7: 1, material inlet 13 by reactor 10 bottoms adds, after circulation oar material mixes, enter reactor 10, carry out heat exchange with the vertical tubulation heat-exchanger rig 16 of reactor 10 inside, the oar material is heated, temperature raises, esterification takes place, part ethylene glycol vaporization in esterification, therefore form the lower gas-liquid mixed phase of density on reactor 10 tops, under the promotion of density difference, material is via the water conservancy diversion top cover 11 on top, inhomogeneous reaction thing outlet pipe 12 enters the evaporating area 21 of evaporation reaction device 2, produces gas-liquid separation, oar material and the ethylene glycol generation esterification of not vaporizing generate carboxylate and water.Water and unnecessary ethylene glycol part vaporization at high temperature, the gas phase of ethylene glycol and water is discharged by the gaseous phase outlet 23 at evaporation reaction device 2 tops, enters tail gas treatment process tower 7.And liquid phase enters the reaction zone 22 of evaporation reaction device 2 bottoms, proceeds reaction and gas-liquid separation.The material that part has been finished esterification imports the second esterifier B through reaction zone 22 bottom material outlets 15, and the material of part enters circulation next time again with after fresh oar material mixes.
The material of having finished esterification imports the mistress 41 of the second esterifier B from material outlet 15, behind inner core 40 1 circles, enter inner room 42 through slit, in inner room 42, carry out heat exchange with heating coil 43, and stir by 44 pairs of materials of whipping appts, carry out esterification, the oligopolymer of finishing after the esterification is discharged by the bottom, and water that generates in reaction process and excessive ethylene glycol are discharged from the top with gas phase state and sent into process tower and handle.
Water of being discharged by first and second esterifier A, B top and ethylene glycol steam enter process tower 7 and carry out separating treatment, and the ethylene glycol of separating at the bottom of the tower is introduced first and second esterifier A, B recycling.Water and the noncondensable gas separated from cat head enter reflux exchanger 70, and noncondensable gas is sent into tail gas tower and handled, and a water of condensation part refluxes, and another part send waste disposal plant 71 to handle.
Material after the second esterifier B esterification enters in the upper cavity 51 of Prepolycondensating reactor C, flow and carry out heat exchange along phase with heating coil 56 in the upper cavity 51, wherein liquid phase from upper cavity 51 via pipeline 56, under the control of variable valve 58, flow into lower chamber 52, in lower chamber 52, continue to carry out heat exchange, and under the effect of whipping appts 53, carry out polycondensation with heating coil 520.Gas phase in the material is ethylene glycol and other volatiles that devolatilization is come out in the reaction, they are entering lower chamber 52 from upper cavity 51 by crooked swirling flow passage 502 under the effect of pressure difference 2000-4000pa under the control of variable valve 503, separate the removal entrained drip through rotation, the gas that junction lower chamber 52 is evaporated together enters vacuum system from gaseous phase outlet 59.
Liquid phase material in the Prepolycondensating reactor C is discharged by pre-polymerization material outlet 520, sends into final polycondensation reactor D with pump 9, material from enter the mouth 60 enter reactor after, under the effect of separable ring dish whipping appts, carry out polycondensation.It is membranaceous that material is formed, help the ethylene glycol liquid polymer of from the continuous replacement process of film, overflowing, polycondensation is carried out to the deeper degree direction, owing in reactor, form a kind of film (abbreviation vertical film) perpendicular to air flow line in the reactor, be parallel to the film (abbreviation parallel membrane) of air flow line in the reactor with another kind, thereby increased the amount of unit whipping appts action space belongings feed liquid film, make the reactor mass transfer area increase, the probability that ethylene glycol is deviate from improves, and effectively raises stirring efficiency.The ethylene glycol of deviating from from liquid phase enters spray condenser 8 through gaseous phase outlet, and after cold liquid glycol direct heat exchange condensation, ethylene glycol enters the ethylene glycol receiving tank, and noncondensable gas enters vacuum system.
In above-mentioned reaction process, the heating coil in each reactor is connected with liquid phase heating agent house steward E10, E11, E20, the E21 in the external world respectively, and sufficient amount of heat is provided.
In sum, the efficient simplification device of production polyethylene terephthalate has the following advantages in the utility model:
1. the esterification part makes the esterification yield of second esterifier outlet reach more than 96% owing to adopt first and second esterifiers, the esterification smooth operation, and content of carboxyl end group is easy to control.
2. because first esterification reaction process has adopted a kind of hybrid power outer circulation type esterifier, and because this reactor has rationally solved the heat power circulation and external force promotes the round-robin fit scale, reduced the internal circulating load of ethylene glycol, rationally use the energy, make device both save the energy, reduce equipment volume again, reduce under the situation of cost, reach the purpose that polyester device maximizes.
3. because the esterification yield height, make precondensation section lactonization reaction ratio descend greatly, the water yield that reaction generates seldom, so can adopt with ethylene glycol is the airless injection system of power steam, this injection system has advantages such as energy consumption is low, the EG reuse convenient, and quantity of wastewater effluent is few.
In polycondensation part owing to adopt Prepolycondensating reactor and final polycondensation reactor, make precondensation outlet limiting viscosity reach 0.22～0.28, satisfy the requirement that directly enters final polycondensation reactor.
5. owing to adopted Prepolycondensating reactor, make and produce steadily that control is simple with special construction.
6. because the use of final polycondensation reactor, can form film (abbreviation vertical film) perpendicular to air flow line in the reactor, with the film that is parallel to air flow line in the reactor (abbreviation parallel membrane), increased the amount of unit whipping appts action space belongings feed liquid film, increase the reactor mass transfer area, effectively raised stirring efficiency.
Claims (6)
1. efficient simplification device of producing polyethylene terephthalate, include first, second esterifier, Prepolycondensating reactor and final polycondensation reactor, the material outlet of the described first esterifier bottom is connected with the mistress of described second esterifier, the material outlet of described second esterifier is communicated with the upper cavity of described Prepolycondensating reactor, the prepolymer outlet of described Prepolycondensating reactor is connected with the material inlet of final polycondensation reactor, described second esterifier part within it wherein is provided with heating agent coil pipe and the whipping appts that is driven by external force every mistress and inner room that formation communicates in inner room; It is characterized in that:
Described first esterifier is a hybrid power outer circulation type esterifier, include inhomogeneous reaction device, evaporation reaction device and Power Drive Unit, described inhomogeneous reaction device includes the reactor of setting up formula tubulation heat-exchanger rig in one, the outlet of this reactor is connected with described evaporation reaction device, and inlet is connected with the opening for feed of reaction mass and the bottom of evaporation reaction device; Described evaporation reaction device includes an airtight housing, on the top of enclosure interior is evaporating area, the bottom is a reaction zone, be provided with gaseous phase outlet at its top, the bottom is extended with a diversion section, be provided with at least one flow deflector in this diversion section, this evaporation reaction device and described reactor constitute the loop of a sealing; Described Power Drive Unit includes the driving mechanism that is located at described evaporation reaction device outside, the axial-flow type whipping appts that is hubbed on described diversion section inside, and this axial-flow type whipping appts connects with described driving mechanism by axle;
Described Prepolycondensating reactor includes a upper cavity and a lower chamber, be provided with the whipping appts that drives by external force in lower chamber inside, upper cavity and lower chamber are isolated cylindrical shell by one and are combined in the airtight housing, described upper cavity is provided with a material inlet, and is provided with heating coil in this upper cavity inside; The top of described lower chamber is provided with exhaust-duct, the bottom of extending outside the described housing and is provided with pipeline and the prepolymer outlet that is communicated with described upper cavity bottom, and the inner bottom part at this lower chamber is provided with heating coil simultaneously; On described isolation cylindrical shell, offer a slit, and this slit place is provided with arc plate toward inner extension of described lower chamber, this arc plate forms one with described isolating cylinder body and is used to be communicated with the crooked swirling flow passage of described upper cavity and lower chamber, and is provided with one at described slit place and is used to regulate the variable valve of slit size;
Described final polycondensation reactor includes the rounded or oblong pressure-bearing type cylindrical shell of cross section of a sealing, and this cylindrical shell is provided with material inlet and material outlet, and is provided with the agitator that can form vertical film and parallel membrane in inner barrel.
2. according to the efficient simplification device of the production polyethylene terephthalate described in the claim 1, it is characterized in that: be five flow aprons that positive pentagon distributes by being welded with in the described first esterifier diversion section, and left the space that is used to put described axial-flow type whipping appts middle the blocking of every flow deflector.
3. according to the efficient simplification device of the production polyethylene terephthalate described in the claim 1, it is characterized in that: the side that the upper cavity inside of described Prepolycondensating reactor is positioned at slit is provided with one and is used for the flow deflector that pilot-gas flows to.
4. according to the efficient simplification device of the production polyethylene terephthalate described in the claim 1, it is characterized in that: the agitator of described final polycondensation reactor inside includes two drive shafts and many group disk rings, the center of circle that is centered close to cylindrical shell of described drive shaft or down round center, described disk ring is separately fixed on two drive shafts, and described ring dish is installed with the parallel axial membrane steel plate of polylith at its sidepiece.
5. according to the efficient simplification device of the production polyethylene terephthalate described in the claim 4, it is characterized in that: the drive shaft in the described final polycondensation reactor is a tubular shaft.
6. according to the efficient simplification device of the production polyethylene terephthalate described in the claim 4, it is characterized in that: described disk ring is by being welded be that regular hexagon distributes six radially membrane plate back up pads, and every radially membrane plate and adjacent ring dish are integrally welded.
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| Application Number | Priority Date | Filing Date | Title |
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| CN 200520002231 CN2767447Y (en) | 2005-02-05 | 2005-02-05 | Highly efficient simplified apparatus for producing polyethylene terephthalate |
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| Application Number | Priority Date | Filing Date | Title |
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| CN 200520002231 CN2767447Y (en) | 2005-02-05 | 2005-02-05 | Highly efficient simplified apparatus for producing polyethylene terephthalate |
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| CN2767447Y true CN2767447Y (en) | 2006-03-29 |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102190784A (en) * | 2011-04-01 | 2011-09-21 | 浙江万凯新材料有限公司 | Production equipment for PET (poly(ethylene terephthalate)) chip |
| CN101580974B (en) * | 2009-05-31 | 2011-12-21 | 中国纺织工业设计院 | Continuous cation modified polyester preparation method and system for continuously preparing modified polyester melt and directly spinning polyester fiber |
| CN101612544B (en) * | 2009-05-27 | 2012-01-25 | 中国纺织工业设计院 | Prepolycondensating reactor device |
| CN102775584A (en) * | 2012-08-30 | 2012-11-14 | 中国昆仑工程公司 | Pre-polycondensation reactor |
| CN103717299A (en) * | 2011-06-10 | 2014-04-09 | 英威达技术有限公司 | Variable pressure drop up flow-pre-polymerizer (UFPP) systems and methods |
| CN104098762A (en) * | 2014-07-16 | 2014-10-15 | 珠海华润包装材料有限公司 | Bottle-grade PET (polyethylene glycol terephthalate) device and production technology thereof |
| CN109621867A (en) * | 2018-12-13 | 2019-04-16 | 中国石油天然气集团有限公司 | The polycondensation reactor of Novel air phase space structure |
-
2005
- 2005-02-05 CN CN 200520002231 patent/CN2767447Y/en not_active Expired - Lifetime
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101612544B (en) * | 2009-05-27 | 2012-01-25 | 中国纺织工业设计院 | Prepolycondensating reactor device |
| CN101580974B (en) * | 2009-05-31 | 2011-12-21 | 中国纺织工业设计院 | Continuous cation modified polyester preparation method and system for continuously preparing modified polyester melt and directly spinning polyester fiber |
| CN102190784A (en) * | 2011-04-01 | 2011-09-21 | 浙江万凯新材料有限公司 | Production equipment for PET (poly(ethylene terephthalate)) chip |
| CN102190784B (en) * | 2011-04-01 | 2012-11-14 | 浙江万凯新材料有限公司 | Production equipment for PET (poly(ethylene terephthalate)) chip |
| CN103717299A (en) * | 2011-06-10 | 2014-04-09 | 英威达技术有限公司 | Variable pressure drop up flow-pre-polymerizer (UFPP) systems and methods |
| CN103717299B (en) * | 2011-06-10 | 2015-12-23 | 英威达技术有限公司 | Variable-pressure drop upper reaches pre-polymerizer (UFPP) system and method |
| CN102775584A (en) * | 2012-08-30 | 2012-11-14 | 中国昆仑工程公司 | Pre-polycondensation reactor |
| CN104098762A (en) * | 2014-07-16 | 2014-10-15 | 珠海华润包装材料有限公司 | Bottle-grade PET (polyethylene glycol terephthalate) device and production technology thereof |
| CN109621867A (en) * | 2018-12-13 | 2019-04-16 | 中国石油天然气集团有限公司 | The polycondensation reactor of Novel air phase space structure |
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| GR01 | Patent grant | ||
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Expiration termination date: 20150205 Granted publication date: 20060329 |