CN202297440U - Continuous production system of polytrimethylene terephthalate - Google Patents
Continuous production system of polytrimethylene terephthalate Download PDFInfo
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- CN202297440U CN202297440U CN2011203366967U CN201120336696U CN202297440U CN 202297440 U CN202297440 U CN 202297440U CN 2011203366967 U CN2011203366967 U CN 2011203366967U CN 201120336696 U CN201120336696 U CN 201120336696U CN 202297440 U CN202297440 U CN 202297440U
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- 238000010924 continuous production Methods 0.000 title claims abstract description 28
- -1 polytrimethylene terephthalate Polymers 0.000 title claims abstract description 24
- 229920002215 polytrimethylene terephthalate Polymers 0.000 title abstract 4
- 238000007670 refining Methods 0.000 claims abstract description 65
- 239000007791 liquid phase Substances 0.000 claims abstract description 41
- 238000006068 polycondensation reaction Methods 0.000 claims abstract description 39
- 239000000203 mixture Substances 0.000 claims abstract description 35
- 238000005886 esterification reaction Methods 0.000 claims abstract description 31
- 230000032050 esterification Effects 0.000 claims abstract description 27
- 238000000034 method Methods 0.000 claims abstract description 24
- 230000008569 process Effects 0.000 claims abstract description 24
- 238000005453 pelletization Methods 0.000 claims abstract description 22
- 239000002994 raw material Substances 0.000 claims abstract description 17
- 239000000463 material Substances 0.000 claims abstract description 16
- 239000012071 phase Substances 0.000 claims abstract description 15
- 238000001035 drying Methods 0.000 claims abstract description 14
- 239000007789 gas Substances 0.000 claims description 55
- 239000007921 spray Substances 0.000 claims description 53
- KKEYFWRCBNTPAC-UHFFFAOYSA-N Terephthalic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)C=C1 KKEYFWRCBNTPAC-UHFFFAOYSA-N 0.000 claims description 44
- 230000008676 import Effects 0.000 claims description 43
- 239000007788 liquid Substances 0.000 claims description 40
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 17
- 238000012856 packing Methods 0.000 claims description 16
- 238000003860 storage Methods 0.000 claims description 14
- 239000000654 additive Substances 0.000 claims description 10
- 238000007599 discharging Methods 0.000 claims description 10
- 230000000996 additive effect Effects 0.000 claims description 8
- 239000007792 gaseous phase Substances 0.000 claims description 8
- 238000005406 washing Methods 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 5
- 238000013022 venting Methods 0.000 claims description 4
- 238000012216 screening Methods 0.000 claims description 3
- 238000000498 ball milling Methods 0.000 claims description 2
- 239000011552 falling film Substances 0.000 claims description 2
- 239000000945 filler Substances 0.000 claims description 2
- 239000002245 particle Substances 0.000 abstract description 11
- 238000002425 crystallisation Methods 0.000 abstract description 10
- 230000008025 crystallization Effects 0.000 abstract description 10
- ULWHHBHJGPPBCO-UHFFFAOYSA-N propane-1,1-diol Chemical compound CCC(O)O ULWHHBHJGPPBCO-UHFFFAOYSA-N 0.000 abstract 5
- 238000005507 spraying Methods 0.000 abstract 3
- 125000004122 cyclic group Chemical group 0.000 abstract 1
- 238000004821 distillation Methods 0.000 abstract 1
- 238000004519 manufacturing process Methods 0.000 description 8
- 150000007942 carboxylates Chemical class 0.000 description 6
- 239000000047 product Substances 0.000 description 5
- 238000000746 purification Methods 0.000 description 4
- HGINCPLSRVDWNT-UHFFFAOYSA-N Acrolein Chemical compound C=CC=O HGINCPLSRVDWNT-UHFFFAOYSA-N 0.000 description 2
- DNIAPMSPPWPWGF-UHFFFAOYSA-N Propylene glycol Chemical compound CC(O)CO DNIAPMSPPWPWGF-UHFFFAOYSA-N 0.000 description 2
- XXROGKLTLUQVRX-UHFFFAOYSA-N allyl alcohol Chemical compound OCC=C XXROGKLTLUQVRX-UHFFFAOYSA-N 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 230000001351 cycling effect Effects 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 238000005469 granulation Methods 0.000 description 2
- 230000003179 granulation Effects 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 229920000728 polyester Polymers 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000007704 transition Effects 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- UXFQFBNBSPQBJW-UHFFFAOYSA-N 2-amino-2-methylpropane-1,3-diol Chemical compound OCC(N)(C)CO UXFQFBNBSPQBJW-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- FFBHFFJDDLITSX-UHFFFAOYSA-N benzyl N-[2-hydroxy-4-(3-oxomorpholin-4-yl)phenyl]carbamate Chemical compound OC1=C(NC(=O)OCC2=CC=CC=C2)C=CC(=C1)N1CCOCC1=O FFBHFFJDDLITSX-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000000155 melt Substances 0.000 description 1
- 238000000465 moulding Methods 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000012798 spherical particle Substances 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 230000032258 transport Effects 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B9/00—Making granules
- B29B9/16—Auxiliary treatment of granules
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B9/00—Making granules
- B29B9/16—Auxiliary treatment of granules
- B29B2009/165—Crystallizing granules
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B9/00—Making granules
- B29B9/02—Making granules by dividing preformed material
- B29B9/06—Making granules by dividing preformed material in the form of filamentary material, e.g. combined with extrusion
- B29B9/065—Making granules by dividing preformed material in the form of filamentary material, e.g. combined with extrusion under-water, e.g. underwater pelletizers
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- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model relates to a continuous production system of polytrimethylene terephthalate. The system comprises a raw material feeding device, a polycondensation subsystem and a pelletizing crystallization drying subsystem which are connected in turn, wherein a gas phase outlet of an esterification subsystem is connected with an inlet of a process tower for preliminary distillation of a gas-phase discharged material at the esterification section; the liquid phase outlet of the process tower is connected with a to-be-refined PDO (propanediol) mixture input port of a refining device; a gas phase material outlet of a polycondensation reactor in the polycondensation subsystem is connected with a to-be-sprayed medium input port of a spraying device corresponding to the polycondensation reactor; the refined PDO liquid phase output port of the refining device is connected with the PDO raw material inlet of the raw material feeding device and/or the spraying medium inlet of the spraying device; and the non-condensable gas outlet of the process tower is connected with a to-be-treated tail gas inlet of a tail gas treatment subsystem. By adopting the system, PTT (polytrimethylene terephthalate) pelletized particles can be continuously and stably produced, the maximum cyclic utilization of PDO can also be realized, and cost is remarkably reduced.
Description
Technical field
The utility model relates to a kind of poly terephthalic acid 1, and ammediol ester continuous process system belongs to chemical production field.
Background technology
Poly terephthalic acid 1, ammediol ester (PTT) are the successful new polyester materials of 20th century the mid-90 commercial exploitation.Existing a lot of device or system that produces PTT; But do not see the production that comprised from polyester material itself as yet to the continuous process system of this kind material being carried out the full operation of crystallization, drying, pelletizing and packing; Do not have yet can with produce in the production process 1; Ammediol (PDO) is the production system of cyclically utilizing all, and production efficiency is not high, raw material availability is not high, has restricted the development of PTT moulding product.
The utility model content
In order to overcome above-mentioned defective; The utility model provides a kind of poly terephthalic acid 1; Ammediol ester continuous process system; This system can realize the whole process from the PTT material produce to PTT pelletizing, crystallization, drying, packing continuously and stably, can also realize that 1,3 Ucar 35 is in this intrasystem recycle to greatest extent.
The main technical scheme that the utility model adopted is:
A kind of poly terephthalic acid 1; Ammediol ester continuous process system; Comprise the raw material feed device, esterification subsystem, polycondensation subsystem and the pelletizing crystallizing and drying subsystem that connect successively; The gaseous phase outlet of said esterification subsystem connects one and is used for to esterification section gas phase discharging and carries out the import of the process tower of predistillation; The liquid phase outlet of said process tower connects the refining PDO mixture input aperture of treating of a refining plant; What the gas phase discharge port of the polycondensation reactor in the said polycondensation subsystem connected the spray equipment corresponding with it treats drip washing medium input aperture; The refining PDO liquid phase delivery port of said refining plant connects the spray medium inlet of the PDO material inlet and/or the said spray equipment of said raw material feed device, and the liquid phase outlet of said spray equipment connects the said refining PDO mixture input aperture of treating, the noncondensable gas outlet of said process tower connects the pending tail gas import of vent gas treatment subsystem.
Can comprise treating tower, reboiler and tower still recycle pump in the said refining plant; Said treating tower comprises the tower body that the tower still that is positioned at the bottom and its bottom opening directly are connected with the open top of said tower still; The liquid phase outlet of said tower still bottom connects said tower still inlet of circulating pump; Said tower still outlet of circulating pump connects the import of said reboiler, and the outlet at bottom of said reboiler directly is connected with another opening that is arranged on said tower body top.
Said esterification subsystem can comprise two esterifiers that connect successively; Wherein the kettle of second esterifier is the multi-cavity chamber horizontal reacting still of jacketed; The adjacent chamber of said second esterifier adopts dividing plate to separate; The bottom of dividing plate is provided with through hole or breach, and each chamber is provided with whisking appliance, heating coil, additive conduit and guide shell separately, and it is inner that each said additive conduit is inserted corresponding said guide shell.
Above-mentioned any poly terephthalic acid 1; In the ammediol ester continuous process system; Said pelletizing crystallizing and drying subsystem can comprise underwater pelletizer, prilling tower, bulk catcher and the chip dryer that connects successively; The tower body of said prilling tower mainly is made up of spiral pipe, and water temperature remains on 75-85 ℃ in the said prilling tower.
Said spray equipment can comprise that the trap and that connects successively is equipped with two liquid seal troughs of a usefulness; The outlet of said liquid seal trough is provided with impeller pump; The spray medium import of said trap is through the outlet of the said liquid seal trough of pipe connection; This pipeline is provided with the spray interchanger that is used for to the pipeline internal medium cooling; What the inlet of said trap constituted said spray equipment treats drip washing medium input aperture, and the outlet of said liquid seal trough also connects the refining PDO mixture input aperture of treating of said refining plant, constitutes the liquid phase outlet of said spray equipment.
Said poly terephthalic acid 1; Ammediol ester continuous process system can also comprise the treating tower vacuum sub-system and one to one overlap polycondensation section vacuum sub-system with said spray equipment more; Said refining vacuum sub-system comprises vacuum pump; The import of said vacuum pump is connected with the non-condensable gas outlet of said overhead vapours condensing surface or the return tank of top of the tower venting port that is attached thereto, and the liquid phase outlet connects the said refining PDO mixture input aperture of treating, said polycondensation section vacuum sub-system is provided with rotary pump with liquid ring; The inlet pipeline of said rotary pump with liquid ring is provided with or is not provided with vacuum jet pump; The import of the inlet pipeline of said rotary pump with liquid ring is the vacuum orifice of said polycondensation section vacuum sub-system, is connected with the gaseous phase outlet at said trap top, and the liquid phase outlet of said rotary pump with liquid ring is connected with the refining PDO mixture input aperture of treating of said refining plant.
The beneficial effect of the utility model:
Owing to adopt reboiler to the heating that circulates through the liquid phase substance that still contains PDO that comes together in tower still bottom after the tower body initial gross separation; Make PDO wherein constantly be heated evaporation with light component; Evaporating the PDO that directly gets into tower body once more with light component and purifies; Be equivalent to the PDO in the mixture that contains PDO is carried out repeatedly refining the purification; Therefore significantly improved the purity of PDO, but reached the specification of quality of reuse, for the recycle of PDO provides basic precondition as the esterification raw material.
Owing to adopt underwater cutpellet, granulation is even, slick and sly, dehydration is convenient, and environmental protection; Owing to adopt 75-85 ℃ crystallization processes under water; And the prilling tower that has adopted its tower body mainly to constitute by spiral pipe; Can guarantee fully that the PTT particle has enough residence time to carry out crystallization in tower; The second-order transition temperature of the PTT particle after the crystallization is improved, and corpuscular property can improve, though when temperature is higher also can not become thickness, caking of PTT particle; Convenient follow-up packing, storage and transportation are for providing important assurance from the PTT synthesis material up to the whole process continuous production of PTT particle.
Because the kettle of second esterifier is the multi-cavity chamber horizontal reacting still of jacketed; Can according to actual needs the length of each chamber be arranged to equate or do not wait; Be convenient to control the residence time of various materials (comprising carboxylate) at different chamber; Thereby control the Zhi Huadu of carboxylate, and, can multiple different additives be joined in the carboxylate of the different Zhi Huadus in the different chamber because each chamber is provided with separately independently whisking appliance, heating coil and additive conduit at each chamber; And each chamber carried out separately independently temperature control and stir; Help realizing accurate control, thereby improve the quality product after the esterification, for the PTT continuous production provides important quality-guarantee Zhi Huadu.
Because each liquid phase of overlapping the rotary pump with liquid ring of the liquid phase outlet of said spray equipment, said polycondensation section vacuum sub-system exports the refining PDO mixture input aperture of treating that all connects said refining plant; And the refining PDO liquid phase delivery port of said refining plant connects the spray medium inlet of the PDO material inlet and/or the said spray equipment of said esterification subsystem; Make the PDO in this system obtain maximized recovery, refining and recycle; Greatly improve raw material availability, significantly reduced the raw material consumption of PDO.
Description of drawings
Fig. 1 is the structural representation of the utility model;
Fig. 2 is the polycondensation section vacuum sub-system structural representation that is provided with vacuum jet pump.
Embodiment
The utility model provides a kind of poly terephthalic acid 1, ammediol ester continuous process system, and shown in Figure 1 is an one of which embodiment.This system comprises raw material feed device, esterification subsystem, polycondensation subsystem and the pelletizing crystallizing and drying subsystem that connects successively; The gaseous phase outlet of said esterification subsystem connects one and is used for to esterification section gas phase discharging and carries out the import of the process tower 26 of predistillation; The liquid phase outlet of said process tower connects the refining PDO mixture input aperture of treating of a refining plant; The mixture introducing refining plant that contains PDO that esterification section in the PTT continuous production is discharged is purified; The refining PDO liquid phase delivery port of said refining plant connects the spray medium inlet of the PDO material inlet and/or the said spray equipment of said raw material feed device; Make and obtain recycle as esterification raw material and/or spray medium once more through the high purity PDO after refining the purification; What the gas phase discharge port of the polycondensation reactor in the said polycondensation subsystem (preferably being provided with first Prepolycondensating reactor 23, second Prepolycondensating reactor 24 and final polycondensation reactor 25 in the said polycondensation subsystem) was connected the spray equipment corresponding with it treats drip washing medium input aperture; The liquid phase outlet of said spray equipment connects the said refining PDO mixture input aperture of treating, the noncondensable gas outlet of said process tower connects the pending tail gas import of vent gas treatment subsystem.
Comprise treating tower 3, reboiler 5 and tower still recycle pump 4 in the said refining plant; Said treating tower comprises the tower body that the tower still that is positioned at the bottom and its bottom opening directly are connected with the open top of said tower still; Said tower body is board-like or board-like/filler combination tower; The liquid phase outlet of said tower still bottom connects said tower still inlet of circulating pump; Said tower still outlet of circulating pump connects the import of said reboiler, and the outlet at bottom of said reboiler directly is connected with another opening that is arranged on said tower body top, and said reboiler is preferably the falling film type reboiler.
The liquid phase outlet of said process tower also connects the PDO phegma inlet of the esterifier (i.e. first esterifier 1 and second esterifier 2) of said esterification subsystem, the direct reuse of the PDO after the realization preliminary purification simultaneously.Guaranteeing that the direct reuse of PDO helps reducing PDO purified amount under the situation of esterification reaction section to the PDO purity requirement, reducing the consumption of system when simplifying technical process.The liquid phase outlet of said process tower and said treating can be provided with valve respectively between refining PDO mixture input aperture and the said PDO phegma inlet; The PDO that is used for regulating respectively direct reuse with introduce amount that refining plant carries out purified PDO to reach suitable ratio, help guaranteeing balance, the steady running of whole PTT continuous process system.
Said refining plant can also comprise overhead vapours condensing surface 9, return tank of top of the tower 8, PDO condensing surface 6, PDO storage tank 27, PDO rotary pump with liquid ring, PDO mixture holding tank 7 and fresh feed pump.The top of said tower body is provided with vapour outlet, is provided with phlegma import, PDO mixture intake and the outlet of PDO liquid phase on the sidewall from top to bottom successively.Connect said overhead vapours condensing surface and return tank of top of the tower between said vapour outlet and the phlegma import successively; It is the import that said vapour outlet connects said overhead vapours condensing surface; The outlet of said overhead vapours condensing surface connects the import of said return tank of top of the tower, and the outlet of said return tank of top of the tower connects said phlegma import.Said overhead vapours condensing surface will change into condensed water through the water vapor in the gaseous impurities of said vapour outlet discharge, be back to treating tower as phlegma then.Said return tank of top of the tower can be provided with a plurality of outlets; Wherein section port connects said phlegma import; Section port can connect the import of sewage treatment equipment; A plurality of outlets are set condensed water is introduced different equipment and independent respectively control flow velocity and flow, help guaranteeing the steady running of whole production system.
Said PDO liquid phase outlet connects the import of said PDO condensing surface; The outlet of said PDO condensing surface connects the import of said PDO storage tank; The outlet of said PDO storage tank connects the import of said PDO rotary pump with liquid ring, and the export mixes of said PDO rotary pump with liquid ring is the refining PDO liquid phase delivery port of said refining plant.The PDO with comparatively high temps, higher degree that makes with extra care back output is pooled in the said PDO storage tank earlier through said PDO condensing surface cooling then, is transported to the PDO material inlet realization cycling and reutilization of said esterification subsystem again through said PDO rotary pump with liquid ring.
Said PDO mixture holding tank is connected with fresh feed pump successively and said charging pump outlet connects said PDO mixture intake, and the import of said PDO mixture holding tank constitutes the refining PDO mixture input aperture of treating of said refining plant.
Said esterification subsystem comprises two esterification reaction section at least, the corresponding esterifier of each esterification reaction section.In the present embodiment; Said esterification subsystem comprises two esterifiers that connect successively; Wherein the kettle of second esterifier 2 is the multi-cavity chamber horizontal reacting still of jacketed; The adjacent chamber of said second esterifier adopts dividing plate to separate, and the bottom of dividing plate is provided with through hole or breach, and each chamber is provided with whisking appliance, heating coil, additive conduit and guide shell separately; It is inner that each said additive conduit and whisking appliance extend into corresponding said guide shell, and said heating coil is looped around the outside of said guide shell.Adopt this second esterifier; Can according to actual needs the length of each chamber be arranged to equate or do not wait; Therefore can control various materials (comprising carboxylate) flexibly in the residence time of different chamber, thereby the control carboxylate is at the Zhi Huadu of each chamber.Because each chamber is provided with separately independently whisking appliance, heating coil and additive conduit; Can multiple different additives be joined in the carboxylate of the different Zhi Huadus in the different chamber; And each chamber carried out separately independently temperature control and stir; Help realizing accurate control, help improving the quality of products Zhi Huadu.
Above-mentioned any said poly terephthalic acid 1; In the ammediol ester continuous process system; Said pelletizing crystallizing and drying subsystem can comprise underwater pelletizer 15, prilling tower 16, bulk catcher 17 and the chip dryer 18 that connects successively; The PTT pelletizing outlet of said pelletizing crystallizing and drying subsystem is connected to the material inlet of pelletizing packing subsystem successively through vibratory screening apparatus 19, shaker conveyer 20 and section storage hopper 21, for example, the delivery port of section storage hopper shown in Figure 1 is connected on the top of the inlet of packing machine 22; The PTT particle gets into packing machine by action of gravity from the section storage hopper, transports device by the packing machine packing.After excessive particle is rejected by the bulk catcher; Get into chip dryer and carry out drying; Get into vibratory screening apparatus then and sieve, in time reject substandard PTT pelletizing, dried qualified PTT particle is delivered to storage temporarily in the section storage hopper through said shaker conveyer again; Get into pelletizing packing subsystem then and directly packed, the packing manner of said pelletizing packing subsystem can be manual, semi or fully automatic mode.
Said underwater pelletizer is provided with the inlet that is used to import the melt that said polycondensation subsystem produces, and the PTT melt that PTT continuously produces directly gets into said underwater pelletizer and carries out pelletizing, has greatly shortened the whole production cycle of PTT particle.Adopt underwater cutpellet, granulation is even, slick and sly, dehydration is convenient, and environmental protection; Said underwater pelletizer is preferably ball milling dicing machine under water, forms spherical particle under water, is transported to prilling tower through pipeline together with water then; Crystallization in being full of the hot water of prilling tower; The tower body of said prilling tower mainly is made up of spiral pipe, its objective is that abundant assurance PTT particle has enough residence time to carry out crystallization in prilling tower, in addition; Water temperature preferably remains on 75-85 ℃ in the said prilling tower; The water and the section residence time of mixture in said prilling tower were controlled between 1-5 minute, and flow rate control is between 1-3m/s, and above prilling tower structure and crystallization processes parameter can be the second-order transition temperature that improves the PTT particle strong guarantee is provided.
Said spray equipment comprises the trap 11 and liquid seal trough 12 that connects successively; The outlet of said liquid seal trough is provided with impeller pump; The spray medium import of said trap is through the outlet of the said liquid seal trough of pipe connection; This pipeline is provided with the spray interchanger that is used for to the pipeline internal medium cooling; What the inlet of said trap constituted said spray equipment treats drip washing medium input aperture, and the outlet of said liquid seal trough also connects the refining PDO mixture input aperture of treating of said refining plant, constitutes the liquid phase outlet of said spray equipment.Utilize said trap spray to capture the gas phase discharging of polycondensation section reactor drum; Reclaim PDO wherein and the oligopolymer that is entrained with thereof; The PDO that the spray back obtains gets into liquid seal trough, is output as two-way then, and one the tunnel is pumped into the spray interchanger is cooled to the spray temperature; Use as the spray medium circulation then, the spray temperature can be adjusted according to processing requirement and spray effect; Another road is introduced into refining plant and makes with extra care purification, can be used as reaction raw materials then or spray medium to be back to said poly terephthalic acid 1, ammediol ester continuous process system.The PDO that said spray medium recycles after can purifying for fresh PDO or through said refining plant also can be the PDO that obtains through said spray equipment self spray back, can also be the mixture of above-mentioned several kinds of PDO.
In the said spray equipment trap can at least two liquid seal troughs of correspondence, at least two interchanger and at least two impeller pumps.Normal use of two liquid seal troughs, one subsequent use, can under normal operation, switch.Said spray interchanger can be plate-type heat exchanger, shell and tube heat exchanger or other kind interchanger.
Said poly terephthalic acid 1; Ammediol ester continuous process system also comprise the treating tower vacuum sub-system and with said spray equipment polycondensation section one to one vacuum sub-system; Be respectively said refining plant and the polycondensation subsystem provides vacuum environment; Said refining vacuum sub-system comprises vacuum pump 10; The import of said vacuum pump is connected with the non-condensable gas outlet of said overhead vapours condensing surface or the return tank of top of the tower venting port that is attached thereto, and aspirates the noncondensable gas in the said refining plant, and the liquid phase outlet connects the said refining PDO mixture input aperture of treating.Said polycondensation section vacuum sub-system is provided with rotary pump with liquid ring 14; The inlet pipeline of said rotary pump with liquid ring is provided with or is not provided with vacuum jet pump 13, and when said vacuum jet pump not being set, the import of said rotary pump with liquid ring is the vacuum orifice of said polycondensation section vacuum sub-system; When said vacuum jet pump is set; Referring to Fig. 2, the import of said vacuum jet pump is the vacuum orifice of said polycondensation section vacuum sub-system, and this vacuum orifice is connected with the gaseous phase outlet at said trap top; Aspirating the gas of collection at large in the said trap, is that said polycondensation subsystem is built subnormal ambient indirectly.When being provided with vacuum jet pump, preferably, utilize the PDO (PDO after preferably handling) that reclaims suction power to be provided for said vacuum jet pump through cooling, maximally utilised the PDO that reclaims.
The liquid phase outlet of said rotary pump with liquid ring is connected with the refining PDO mixture input aperture of treating of said refining plant; Preferably; The liquid phase outlet of said rotary pump with liquid ring is connected to a vacuum sub-system receiving tank earlier, the PDO that reclaims is pooled in this vacuum sub-system receiving tank, and then pumps in the said PDO mixture holding tank of said refining plant through the PDO that pump will compile; To reclaim the PDO in the spray equipment, enlarge scope and the degree that reclaims PDO as much as possible.
Preferably, the corresponding polycondensation section vacuum sub-system that vacuum jet pump is not set of using of said first Prepolycondensating reactor, the corresponding polycondensation section vacuum sub-system that is provided with vacuum jet pump of using of said second Prepolycondensating reactor and final polycondensation reactor.
Said vent gas treatment subsystem comprises eluting column 29 and the tail gas burning furnace that connects successively; The gaseous phase outlet of said vacuum pump outlet and said rotary pump with liquid ring and the equipment drain of other subsystems are connected with the tail gas import of said eluting column; The tail gas delivery port of said eluting column connects said tail gas burning furnace via exhaust ejector 28, and the tail gas import of said eluting column constitutes the pending tail gas import of said vent gas treatment subsystem.Said vent gas treatment subsystem all compiles the tail gas that produces in the relevant device to be sent in the said eluting column; After water coolant drip washing, form cleaning of off-gas; Send into the tail gas burning furnace burning disposal with said exhaust ejector again, the waste water that produces in the said eluting column can be sent into stripping tower and handle and to drain after qualified.
The groundwork process of the utility model is: terephthalic acid and 1,3 Ucar 35 are after a plurality of esterification reaction section esterifications of process under the catalyzer existence condition, and its liquid phase discharging gets into polycondensation section, and the gas phase discharging gets into process tower.The liquid phase discharging extent of polymerization that gets into the polycondensation section improves constantly; Finally obtain the product that final minification gathers; It is the PTT melt; The PTT melt directly is introduced into crystallization under water and the drying that pelletizing crystallizing and drying subsystem carries out underwater cutpellet, specified temp successively, directly gets into pelletizing packing subsystem then and accomplishes packing, thereby accomplished the continuous production from starting material to PTT pelletizing finished product.Contain a large amount of PDO in the gas phase discharging of esterification section; Also be entrained with impurity such as light constituents such as water vapour, vinyl carbinol, propenal and oligopolymer; This gas phase discharging at first gets into the process tower predistillation; PDO is converted into liquid phase and gets into refining plant, and the PDO entering esterification subsystem of the higher degree that meets PTT raw materials for production specification of quality after making with extra care serves as the PDO raw material and/or the entering spray equipment serves as the spray medium, realizes cycling and reutilization; The gas phase discharge port of each polycondensation reactor is also discharged and is contained the PDO mixed gas; These PDO mixed gass get into the spray equipment corresponding with corresponding polycondensation reactor to be separated; Sprayed by PDO; Reclaim PDO in the gas phase discharging and the oligopolymer that is entrained with, can avoid oligopolymer to stop up follow-up vacuum pipe (like the pipeline of vacuum jet pump), influence vacuumizes effect.The liquid phase substance that contains PDO that obtains in the spray equipment pumps into refining plant by impeller pump and purifies; And the gas of collection at large is aspirated into corresponding vacuum sub-system; For esterification section and polycondensation section provide vacuum environment; Wherein said rotary pump with liquid ring aspirates the tail gas of said vacuum jet pump, and the tail gas of said rotary pump with liquid ring is sent into the eluting column in the said vent gas treatment subsystem.
Native system is the fully-closed system; The tail gas of all devices all compiles the eluting column of sending in the vent gas treatment subsystem in the system; After water coolant drip washing; Send into tail gas burning furnace with exhaust ejector and burn, the waste water that produces during device is produced and the leacheate of eluting column are then sent into the stripping tower processing and are drained after qualified.
Aforesaid each subsystem all can be arranged to one or more sets according to needs of production, and relevant device wherein all can be arranged to one or more as required.Native system also comprises some assistant agent allotment and e Foerderanlages, gets final product by the routine setting.
Claims (10)
1. poly terephthalic acid 1; Ammediol ester continuous process system; It is characterized in that comprising raw material feed device, esterification subsystem, polycondensation subsystem and the pelletizing crystallizing and drying subsystem and the vent gas treatment subsystem that connect successively; The gaseous phase outlet of said esterification subsystem connects one and is used for to esterification section gas phase discharging and carries out the import of the process tower of predistillation; The liquid phase outlet of said process tower connects the refining PDO mixture input aperture of treating of a refining plant; What the gas phase discharge port of the polycondensation reactor in the said polycondensation subsystem connected the spray equipment corresponding with it treats drip washing medium input aperture; The refining PDO liquid phase delivery port of said refining plant connects the spray medium inlet of the PDO material inlet and/or the said spray equipment of said raw material feed device, and the liquid phase outlet of said spray equipment connects the said refining PDO mixture input aperture of treating, the noncondensable gas outlet of said process tower connects the pending tail gas import of vent gas treatment subsystem.
2. poly terephthalic acid 1 as claimed in claim 1; Ammediol ester continuous process system; It is characterized in that comprising in the said refining plant treating tower, reboiler and tower still recycle pump; Said treating tower comprises the tower body that the tower still that is positioned at the bottom and its bottom opening directly are connected with the open top of said tower still; The liquid phase outlet of said tower still bottom connects said tower still inlet of circulating pump, and said tower still outlet of circulating pump connects the import of said reboiler, and the outlet at bottom of said reboiler directly is connected with another opening that is arranged on said tower body top.
3. poly terephthalic acid 1 as claimed in claim 2, ammediol ester continuous process system is characterized in that the liquid phase outlet of said process tower also connects the PDO phegma inlet of the esterifier of said esterification subsystem simultaneously.
4. poly terephthalic acid 1 as claimed in claim 3; Ammediol ester continuous process system; It is characterized in that said refining plant also comprises overhead vapours condensing surface, return tank of top of the tower, PDO condensing surface, PDO storage tank, PDO rotary pump with liquid ring, PDO mixture holding tank and fresh feed pump; The top of said tower body is provided with vapour outlet; Be provided with phlegma import, PDO mixture intake and the outlet of PDO liquid phase on the sidewall from top to bottom successively; Connect said overhead vapours condensing surface and return tank of top of the tower between said vapour outlet and the phlegma import successively, said PDO liquid phase outlet connects the import of said PDO condensing surface, and the outlet of said PDO condensing surface connects the import of said PDO storage tank; The outlet of said PDO storage tank connects the import of said PDO rotary pump with liquid ring; The export mixes of said PDO rotary pump with liquid ring is the refining PDO liquid phase delivery port of said refining plant, and said PDO mixture holding tank is connected with fresh feed pump successively and said charging pump outlet connects said PDO mixture intake, and the import of said PDO mixture holding tank constitutes the refining PDO mixture input aperture of treating of said refining plant.
5. poly terephthalic acid 1 as claimed in claim 4; Ammediol ester continuous process system; It is characterized in that said esterification subsystem comprises two esterifiers that connect successively; Wherein the kettle of second esterifier is the multi-cavity chamber horizontal reacting still of jacketed, and the adjacent chamber of said second esterifier adopts dividing plate to separate, and the bottom of dividing plate is provided with through hole or breach; Each chamber is provided with whisking appliance, heating coil, additive conduit and guide shell separately, and it is inner that each said additive conduit is inserted corresponding said guide shell.
6. like the described poly terephthalic acid 1 of an arbitrary claim among the claim 1-5; Ammediol ester continuous process system; It is characterized in that said pelletizing crystallizing and drying subsystem comprises underwater pelletizer, prilling tower, bulk catcher and the chip dryer that connects successively; The tower body of said prilling tower mainly is made up of spiral pipe, and water temperature remains on 75-85 ℃ in the said prilling tower.
7. poly terephthalic acid 1 as claimed in claim 6; Ammediol ester continuous process system; It is characterized in that said spray equipment comprises that the trap and that connects successively is equipped with two liquid seal troughs of a usefulness, the outlet of said liquid seal trough is provided with impeller pump, and the spray medium import of said trap is through the outlet of the said liquid seal trough of pipe connection; This pipeline is provided with the spray interchanger that is used for to the pipeline internal medium cooling; What the inlet of said trap constituted said spray equipment treats drip washing medium input aperture, and the outlet of said liquid seal trough also connects the refining PDO mixture input aperture of treating of said refining plant, constitutes the liquid phase outlet of said spray equipment.
8. poly terephthalic acid 1 as claimed in claim 7; Ammediol ester continuous process system; It is characterized in that also comprising the treating tower vacuum sub-system and overlap polycondensation section vacuum sub-system one to one more with said spray equipment; Said refining vacuum sub-system comprises vacuum pump; The import of said vacuum pump is connected with the non-condensable gas outlet of said overhead vapours condensing air or the return tank of top of the tower venting port that is attached thereto, and the liquid phase outlet connects the said refining PDO mixture input aperture of treating, said polycondensation section vacuum sub-system is provided with rotary pump with liquid ring; The inlet pipeline of said rotary pump with liquid ring is provided with or is not provided with vacuum jet pump; The import of the inlet pipeline of said rotary pump with liquid ring is the vacuum orifice of said polycondensation section vacuum sub-system, is connected with the gaseous phase outlet at said trap top, and the liquid phase outlet of said rotary pump with liquid ring is connected with the refining PDO mixture input aperture of treating of said refining plant.
9. poly terephthalic acid 1 as claimed in claim 8; Ammediol ester continuous process system; It is characterized in that said vent gas treatment subsystem comprises eluting column and the tail gas burning furnace that connects successively; The gaseous phase outlet of said vacuum pump outlet and said rotary pump with liquid ring and all the other equipment venting ports are connected with the tail gas import of said eluting column; The tail gas delivery port of said eluting column connects said tail gas burning furnace via exhaust ejector, and the tail gas import of said eluting column constitutes the pending tail gas import of said vent gas treatment subsystem.
10. poly terephthalic acid 1 as claimed in claim 9; Ammediol ester continuous process system; It is characterized in that the PTT pelletizing outlet of said pelletizing crystallizing and drying subsystem is connected to the material inlet of pelletizing packing subsystem successively through vibratory screening apparatus, shaker conveyer and section storage hopper; Said tower body is board-like or board-like/filler combination tower, and said reboiler is the falling film type reboiler, and said spray interchanger is plate-type heat exchanger or shell and tube heat exchanger; Said underwater pelletizer is ball milling dicing machine under water, and the packing manner of said section packing subsystem is full-automatic, semi-automatic or manual.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011203366967U CN202297440U (en) | 2011-09-08 | 2011-09-08 | Continuous production system of polytrimethylene terephthalate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011203366967U CN202297440U (en) | 2011-09-08 | 2011-09-08 | Continuous production system of polytrimethylene terephthalate |
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| Publication Number | Publication Date |
|---|---|
| CN202297440U true CN202297440U (en) | 2012-07-04 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011203366967U Expired - Lifetime CN202297440U (en) | 2011-09-08 | 2011-09-08 | Continuous production system of polytrimethylene terephthalate |
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| CN (1) | CN202297440U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103360211A (en) * | 2013-07-17 | 2013-10-23 | 浙江万凯新材料有限公司 | Improved ethylene glycol production system |
| CN104558573A (en) * | 2013-10-12 | 2015-04-29 | 中国石油化工股份有限公司 | Polyester production device |
-
2011
- 2011-09-08 CN CN2011203366967U patent/CN202297440U/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103360211A (en) * | 2013-07-17 | 2013-10-23 | 浙江万凯新材料有限公司 | Improved ethylene glycol production system |
| CN103360211B (en) * | 2013-07-17 | 2014-10-15 | 浙江万凯新材料有限公司 | Improved ethylene glycol production system |
| CN104558573A (en) * | 2013-10-12 | 2015-04-29 | 中国石油化工股份有限公司 | Polyester production device |
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Address after: 100007 Beijing, Dongzhimen, North Street, No. 9, No. Patentee after: China National Petroleum Corporation Patentee after: China Kunlun Engineering Co., Ltd. Address before: 100007 Beijing, Dongzhimen, North Street, No. 9, No. Patentee before: China National Petroleum Corporation Patentee before: China Kunlun Contracting & Engineering Corporation |
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Granted publication date: 20120704 |
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