CN203295414U - Polyamide polymerization production equipment - Google Patents
Polyamide polymerization production equipment Download PDFInfo
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- CN203295414U CN203295414U CN2013203171046U CN201320317104U CN203295414U CN 203295414 U CN203295414 U CN 203295414U CN 2013203171046 U CN2013203171046 U CN 2013203171046U CN 201320317104 U CN201320317104 U CN 201320317104U CN 203295414 U CN203295414 U CN 203295414U
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Abstract
The utility model relates to polyamide polymerization production equipment which is composed of a caprolactam melting system, titanium dioxide, benzoic acid, additive, a material feeding system, a high-temperature pre-aggregator, a front polymerization tower, a rear polymerization tower, a dicing and pre-extraction tower, an extraction tower, a pre-drying tower, a drying tower and an extraction water recovery and transportation packaging system. The whole system is automatically controlled by DCS; the equipment and systems are connected through pipelines. According to the polyamide polymerization production equipment provided by the utility model, the high-temperature pre-aggregator and the pre-drying tower are additionally arranged, and a static guide screw mixer assembly is additionally arranged on the lower section of each pipe of the front and rear polymerization towers and the extraction tower, so that polyamide hydrolysis loop open and dehydration are more uniform and more sufficient, and dehydration is more fast and convenient; pre-polymerization addition reaction is more sufficient and stable; molecular distribution in post polymerization condensation polymerization phase is more uniform and stable; extraction of caprolactam monomer from extraction tower is more sufficient and stable; the pre-drying tower removes surface moisture of the section, and the drying tower dries bound water; the recovery system recycles oligomer and caprolactam monomer in extraction water.
Description
Technical field
The utility model relates to a kind of polymerizing polyamide production unit.
Background technology
China is mainly to quote import equipment and technique for the continuous synthetic fibre 6 section polymerization techniques of polymeric amide and equipment at present, and it mainly contains Ji Ma, Yi Wenda, A Jiafei, PE, noy etc.And the equipment and process of introducing is one section or two sections polymerizations substantially, except a large amount of foreign exchange investments of needs cost, also there are a lot of unreasonable designs in its processing unit, as the civilian high-speed spinning section for high-end, will be more obvious in particular for high-end thin dawn spinning chips problem, section poor stability, the molecular distribution of producing is irregular, the viscose glue particle is serious, controllability is difficult, and product specification is in low and middle-grade levels all the time, thereby caused, domesticly for high-end civilian section, mainly still relies on import.
Existing Introduced From Abroad processing unit partly is comprised of caprolactam fusing system, titanium dioxide compounding system, phenylformic acid compounding system, caprolactam charging stock tank, pre-polymerization tower, post polymerization tower, dicing machine, extraction tower, drying tower and conveying and packaging, and whole system adopts the DCS automatization to control.The polymerizing polyamide production technique is hexanolactam charging together with titanium dioxide, phenylformic acid of melting, through pre-polymerization, post polymerization, pelletizing, extraction, the dry product that obtains.
At present domesticly for the polymerizing polyamide production technology and equipments, caprolactam fusing system, titanium dioxide compounding system, phenylformic acid compounding system, caprolactam feed system, pre-polymerization tower, post polymerization tower, dicing machine, extraction tower, drying tower and conveying and packaging, partly consist of, whole system adopts DCS to control; Polymerization process is hexanolactam charging together with titanium dioxide, phenylformic acid of melting, through pre-polymerization, post polymerization, pelletizing, extraction, the dry product that obtains.
Following four subject matters that above Processes and apparatus exists:
1, the equipment workshop section function design of polyamide reaction stage is unreasonable, and conversion zone is indefinite, causes reaction, starting time to obscure;
2, polyreaction molecular distribution out is too wide, and the change of molecular weight is large, poor stability;
3, extracting system exists vapour locking boiling, section motion to have dead angle and oxidized phenomenon, the extraction of oligomers of having no idea;
4, drying temperature is too high, and chip drying adopts high temperature drying, and the section solid-phase tack producing is serious.
Spinning property and the spinning intensity of its impact section, easily produce the spinning broken end, causes the unstable of filament spinning component; Spinning property and the spinning intensity of impact section, easily cause spinning brute force, plucked, and component pressure is unstable; There is a large amount of dead angles in extracting system, and the section motion is inhomogeneous, and top high temperature contacts easy oxidation with air and produces a large amount of yellow sections, causes spinning powerful descend, waft silk and broken end; The high section viscose glue particle that easily forms of drying temperature, make spinning produce a large amount of waft silk and broken end, the directly spinning property of impact section.
for addressing the above problem, it is by the caprolactam melting that the applicant has " polymerizing polyamide production technology and equipments " (China Patent No. 200710052102.8) patent, the hexanolactam of melting and titanium dioxide, phenylformic acid, charging together, through pre-polymerization, post polymerization, pelletizing, extraction, the dry product that obtains, nitrogen-sealed is adopted in the caprolactam melting, the de-salted water preparation, the hexanolactam of melting and titanium dioxide, phenylformic acid is charging together, with the standard fine filter, filter, enter the caprolactam feed system, through pre-polymerization, post polymerization, pelletizing, extraction, drying is carried out under Full-closed system and nitrogen protection.
Above-mentioned patent extraction increases header tank, has solved vapour lock boiling and problem of oxidation; The large flow of dry employing, played certain mitigation to viscose glue, and chipping qualities increases, but do not solve oligomer extraction problem and the inherent molecular distribution problem of cutting into slices in section.The applicant has applied for again " polymerizing polyamide production technology and equipments " (Chinese patent application number 201210271816.9) for this reason, and production technology and equipments is comprised of fusing system, titanium dioxide system, phenylformic acid system, additive system, feed system, the dynamic mixing system of high temperature, pre-polymerization tower, post polymerization tower, pre-extraction tower, extraction tower, drying tower, recovery system.It sets up the dynamic mixing tank of high temperature and pre-extraction tower, set up additive system, on the extraction tower header tank, increase section, water separator, drying tower is set up the section water cooler, the polymeric amide hydrolysis, the dehydration under the dynamic admixture of high temperature, carry out, make the pre-polymerization polyaddition reaction more fully, more stable; Post polymerization polycondensation phase molecular distribution more evenly, more stable.After pre-extraction water and slice separation are left in section on the extraction tower header tank, water separator, pre-extraction water returns pre-extraction tower, make the aqueous solution in pre-extraction tower and extraction tower independently regulate and control not interfere with each other, be conducive to pre-extraction tower emphasis extraction of oligomers, extraction tower only extracts caprolactam monomer, and each concentration stabilize.The drying tower bottom is provided with the section water cooler, can quick cooling section, it is moisture that it should remove slice surface, again except in section in conjunction with water, drying tower inner drying temperature is 125-150 ℃, 30 hours time.
Though above-mentioned patented technology is greatly improved quality product, but do not solve the most basic problem in polymerizing polyamide reaction, namely can full and uniform mixing in high temperature, high pressure, high sticky main equipment, stable, without dead angle and cryodrying.
Summary of the invention
The purpose of this utility model is for above-mentioned present situation, aims to provide that a kind of molecule that can effectively control in dry sliced is uniformly distributed and stable, the up-to-date polymerizing polyamide production unit that drying temperature is low, the time is short.
The implementation of the utility model purpose is, the polymerizing polyamide production unit, caprolactam fusing system, titanium dioxide compounding system, phenylformic acid compounding system, additive compounding system, caprolactam feed system, High Temperature Pre polymerizer, pre-polymerization tower, post polymerization tower, pelletizing system, pre-extraction tower, extraction tower, drying tower, extraction water recovery system and conveying and packaging system are arranged, and whole system equipment adopts the DCS automatization to control;
On the upper and lower connected of High Temperature Pre polymerizer heating tubulation one, honeybee shape orifice plate one, lower honeybee shape orifice plate one are fixed on the High Temperature Pre polymerizer on inwall, High Temperature Pre polymerizer hypomere is provided with static water conservancy diversion mixing screw subassembly one, two, three, four, bubble-cap interface one, the feed-pipe one that is communicated with front poly-tower arranged at top, material outlet one is arranged at bottom, and heating semicanal or chuck are arranged outward;
Between extraction tower and drying tower, be provided with predrying tower, predrying top of tower has section charging interface five, air outlet five, and discharge port five is arranged at bottom; Predrying inner wall of tower hypomere connects back taper air blast ring five, and back taper air blast ring five will form dry air blast distributing ring five with predrying tower back taper hypomere, and dry air blast distributing ring five connects air blast distributing ring blast inlet five;
On heating tubulation two upper and lower connected, honeybee shape orifice plate two, lower honeybee shape orifice plate two are fixed on the pre-polymerization tower on inwall, pre-polymerization tower hypomere is provided with static water conservancy diversion mixing screw subassembly A, B, C, D, the pre-polymerization top of tower is provided with bubble-cap interface two, the feed-pipe two that is communicated with the High Temperature Pre polymerizer, and bottom is provided with material outlet two, and tower has heating semicanal or chuck outward;
On heating tubulation three upper and lower connected, honeybee shape orifice plate three, lower honeybee shape orifice plate three are fixed on the post polymerization tower on inwall, post polymerization tower hypomere is provided with static water conservancy diversion mixing screw subassembly E, F, G, H, on post polymerization top of tower bubble-cap interface three, film forming water trap, connect feed-pipe three, the lower biphenyl heating tube three that connects, under material outlet three is arranged, heating semicanal or chuck are arranged outward;
Header tank charging interface four is arranged at the extraction tower top, the extraction tower bottom is provided with material outlet four, the heat tracing pipe is arranged outward, in extraction tower, be provided with static water conservancy diversion mixing screw subassembly I, J, K, L, M, N from top to bottom, static water conservancy diversion mixing screw subassembly is fixed on the extraction tower inwall.
The utility model has increased predrying tower process and predrying tower on former patent High Temperature Pre polymerization technique and High Temperature Pre polymerizer Equipment Foundations.Polymeric amide hydrolysis, dehydration, carry out in the High Temperature Pre polymerizer.In High Temperature Pre polymerizer, pre-polymerization tower, each tubulation hypomere of post polymerization tower and extraction tower, all have additional static water conservancy diversion mixing screw subassembly, in high temperature, high pressure, high adhesive aggregation close, can fully mix and can avoid dead angle; Addition reaction and part polycondensation are carried out in the pre-polymerization tower, polycondensation is carried out in the post polymerization tower, make the hydrolysis of its High Temperature Pre polymerizer, ring-opening reaction more fully, dehydration is faster; Make the pre-polymerization polyaddition reaction more fully, more stable; Make post polymerization polycondensation phase molecular distribution more evenly, more stable.In extraction tower, set up static water conservancy diversion mixing screw subassembly, make extraction water and section motion more evenly, the monomer washing controls more stable; The predrying tower of newly establishing is only except slice surface moisture (being down to below 1% from 10%), drying temperature can reduce greatly, time of drying is also very short, the temperature that is conducive to the later stage drying tower reduces and time shorten, prevent that section from forming the viscose glue particle when drying is in conjunction with water in drying tower, affects quality product.
The accompanying drawing explanation
Fig. 1 is High Temperature Pre polymerizer structural representation,
Fig. 2 is pre-polymerization tower structure schematic diagram,
Fig. 3 is post polymerization tower structure schematic diagram,
Fig. 4 is the extraction tower structural representation,
Fig. 5 is predrying tower structure schematic diagram.
Embodiment
The utility model consists of caprolactam fusing system, titanium dioxide compounding system, phenylformic acid compounding system, additive compounding system, caprolactam feed system, High Temperature Pre polymerizer, pre-polymerization tower, post polymerization tower, pelletizing system, pre-extraction, extraction tower, predrying tower, drying tower, extraction water recovery system and conveying and packaging system.Whole system adopts the DCS automatization to control; Each tower, system connect by pipeline.
Wherein titanium dioxide compounding system, phenylformic acid compounding system, additive compounding system, caprolactam feed system, pre-polymerization tower, post polymerization tower, pelletizing system, pre-extraction, extraction tower, drying tower, extraction water recovery system and conveying and packaging system adopt the Processes and apparatus of the original patent of the applicant or patent applied for.
The utility model is described in detail in detail with reference to the accompanying drawings.
With reference to honeybee shape orifice plate 1, lower honeybee shape orifice plate 1 on Fig. 1, heating tubulation 1 upper and lower connected, be fixed on the High Temperature Pre polymerizer on inwall, High Temperature Pre polymerizer hypomere is provided with static water conservancy diversion mixing screw subassembly one, two, three, 45,6,7,8, interface 1, the feed-pipe 1 that is communicated with bubble-cap with the pre-polymerization tower arranged at top, material outlet 1 is arranged at bottom, and heating semicanal or chuck 9 are arranged outward.The hexanolactam of melting mixes with titanium dioxide, phenylformic acid, additive, in the High Temperature Pre polymerizer, carries out polymeric amide hydrolysis, dehydration, under high temperature static water conservancy diversion thread mixing, carries out, make its reaction more evenly, more fully, dehydration is faster.Be conducive to the pre-polymerization addition reaction more fully, more stable, also be conducive to simultaneously post polymerization polycondensation phase molecular distribution more evenly, more stable.
With reference to Fig. 2, on heating tubulation 2 16 upper and lower connected, honeybee shape orifice plate 2 17, lower honeybee shape orifice plate 2 18 are fixed on the pre-polymerization tower on inwall, pre-polymerization tower hypomere is provided with static water conservancy diversion mixing screw subassembly A, B, C, D20,21,22,23, pre-polymerization top of tower are provided with interface 2 15, the feed-pipe 2 14 that is communicated with bubble-cap with the High Temperature Pre polymerizer, bottom is provided with material outlet 2 19, and tower has heating semicanal or chuck 24 outward.The hexanolactam of melting mixes with titanium dioxide, phenylformic acid, additive, after the High Temperature Pre polymerizer, enter the pre-polymerization tower, carry out polymeric amide open loop, dehydration, addition polycondensation reaction, whole process is carried out under the static water conservancy diversion thread mixing of pre-polymerization tower, make reaction more evenly, more fully, more stable.Also be conducive to simultaneously post polymerization polycondensation phase molecular distribution more evenly, more stable.
With reference to Fig. 3, on heating tubulation 3 26 upper and lower connected, honeybee shape orifice plate 3 27, lower honeybee shape orifice plate 3 28 are fixed on the post polymerization tower on inwall, post polymerization tower hypomere is provided with static water conservancy diversion mixing screw subassembly E, F, G, H33,34,35,25, the feed-pipe 3 30 that the post polymerization top of tower has bubble-cap interface 29, is communicated with the pre-polymerization tower, material outlet 3 13 is arranged at bottom, on film forming water trap 31, connect feed-pipe 3 30, the lower biphenyl heating tube 50 that connects, biphenyl is sent in the film forming water trap, the film forming water trap is heated.Heating semicanal or chuck 32 are arranged outward.The hexanolactam of melting mixes with titanium dioxide, phenylformic acid, additive, after High Temperature Pre polymerizer, pre-polymerization tower, enters polymerization tower, under the static water conservancy diversion thread mixing of post polymerization tower, carries out polycondensation, reaction effect more evenly, more fully, more stable.
With reference to Fig. 4, header tank charging interface 41 is arranged at the extraction tower top, and bottom is provided with material outlet 4 42, and heat tracing pipe 4 43 is arranged outward.In extraction tower, be provided with static water conservancy diversion mixing screw subassembly I, J, K, L, M, N36,37,38,39,40,41 from top to bottom, static water conservancy diversion mixing screw subassembly is fixed on the extraction tower inwall, and static water conservancy diversion mixing screw subassembly can increase or reduce according to processing requirement and device structure size.The hexanolactam of melting mixes with titanium dioxide, phenylformic acid, additive, through High Temperature Pre polymerizer, pre-polymerization tower post polymerization tower, pelletizing system, pre-extraction, enter extraction tower, by the static water conservancy diversion mixing screw of extraction tower, repeatedly mix, its extraction caprolactam monomer effect more fully, more evenly, more stable.
With reference to Fig. 5, predrying top of tower has section charging interface 5 44, air outlet 5 49, and predrying inner wall of tower hypomere back taper air blast ring 5 45, dry air blast distributing ring 5 46, air blast distributing ring blast inlet 5 47, section discharging interface 5 48 is arranged at predrying tower bottom.through pelletizing system, pre-extraction, extraction tower enters predrying tower, predrying tower plays regional function in drying process and divides, because section contains two kinds of water in process of production: a kind of is surface water approximately 10%, another kind is in conjunction with the about 0.01%-1% of water, the characteristics that easily are removed according to surface water, this increases predrying tower, can surface water be down to below 1% by 10% in lower temperature and shorter time, be conducive to later stage dry impact that is not subjected to the surface water drying during in conjunction with water in drying tower, drying temperature is 105-125 ℃, time 12-14 hour, the drying tower temperature reduces greatly, time also shortens greatly, can prevent effectively that section from forming the viscose glue particle during in conjunction with water and affecting quality product in drying, namely guaranteed quality product, energy-conserving and environment-protective again.
Claims (1)
1. polymerization process is produced the equipment of polymeric amide, caprolactam fusing system, titanium dioxide compounding system, phenylformic acid compounding system, additive compounding system, caprolactam feed system, High Temperature Pre polymerizer, pre-polymerization tower, post polymerization tower, pelletizing system, pre-extraction tower, extraction tower, drying tower, extraction water recovery system and conveying and packaging system are arranged, and whole system equipment adopts the DCS automatization to control;
It is characterized in that on the upper and lower connected of High Temperature Pre polymerizer heating tubulation one that honeybee shape orifice plate one, lower honeybee shape orifice plate one are fixed on the High Temperature Pre polymerizer on inwall, High Temperature Pre polymerizer hypomere is provided with static water conservancy diversion mixing screw subassembly one, two, three, four, bubble-cap interface one, the feed-pipe one that is communicated with front poly-tower arranged at top, material outlet one is arranged at bottom, and heating semicanal or chuck are arranged outward;
Between extraction tower and drying tower, be provided with predrying tower, predrying top of tower has section charging interface five, air outlet five, and discharge port five is arranged at bottom; Predrying inner wall of tower hypomere connects back taper air blast ring five, and back taper air blast ring five will form dry air blast distributing ring five with predrying tower back taper hypomere, and dry air blast distributing ring five connects air blast distributing ring blast inlet five;
On heating tubulation two upper and lower connected, honeybee shape orifice plate two, lower honeybee shape orifice plate two are fixed on the pre-polymerization tower on inwall, pre-polymerization tower hypomere is provided with static water conservancy diversion mixing screw subassembly A, B, C, D, the pre-polymerization top of tower is provided with bubble-cap interface two, the feed-pipe two that is communicated with the High Temperature Pre polymerizer, and bottom is provided with material outlet two, and tower has heating semicanal or chuck outward;
On heating tubulation three upper and lower connected, honeybee shape orifice plate three, lower honeybee shape orifice plate three are fixed on the post polymerization tower on inwall, post polymerization tower hypomere is provided with static water conservancy diversion mixing screw subassembly E, F, G, H, on post polymerization top of tower bubble-cap interface three, film forming water trap, connect feed-pipe three, the lower biphenyl heating tube three that connects, under material outlet three is arranged, heating semicanal or chuck are arranged outward;
Header tank charging interface four is arranged at the extraction tower top, the extraction tower bottom is provided with material outlet four, the heat tracing pipe is arranged outward, in extraction tower, be provided with static water conservancy diversion mixing screw subassembly I, J, K, L, M, N from top to bottom, static water conservancy diversion mixing screw subassembly is fixed on the extraction tower inwall.
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| Application Number | Priority Date | Filing Date | Title |
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| CN2013203171046U CN203295414U (en) | 2013-06-04 | 2013-06-04 | Polyamide polymerization production equipment |
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| CN2013203171046U CN203295414U (en) | 2013-06-04 | 2013-06-04 | Polyamide polymerization production equipment |
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| CN203295414U true CN203295414U (en) | 2013-11-20 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114196009A (en) * | 2020-08-31 | 2022-03-18 | 中国石油化工股份有限公司 | Method for continuously preparing poly (m-xylylene adipamide) |
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- 2013-06-04 CN CN2013203171046U patent/CN203295414U/en not_active Withdrawn - After Issue
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114196009A (en) * | 2020-08-31 | 2022-03-18 | 中国石油化工股份有限公司 | Method for continuously preparing poly (m-xylylene adipamide) |
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Legal Events
| Date | Code | Title | Description |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20131120 Effective date of abandoning: 20151021 |
|
| C25 | Abandonment of patent right or utility model to avoid double patenting |