CN101302285A - Production process of polyethylene glycol terephthalate - Google Patents
Production process of polyethylene glycol terephthalate Download PDFInfo
- Publication number
- CN101302285A CN101302285A CNA2008101229224A CN200810122922A CN101302285A CN 101302285 A CN101302285 A CN 101302285A CN A2008101229224 A CNA2008101229224 A CN A2008101229224A CN 200810122922 A CN200810122922 A CN 200810122922A CN 101302285 A CN101302285 A CN 101302285A
- Authority
- CN
- China
- Prior art keywords
- unit
- dehydration
- esterification
- ethylene glycol
- slurry
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Landscapes
- Polyesters Or Polycarbonates (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a process for making polyethylene glycol terephthalate, in particular to a process for making polyester by taking aromatic carboxylic acid as materials, belonging to the chemical production technical field. The process comprises the steps of material preparation unit - pulping unit - pulp dehydration unit - evaporation dehydration unit - esterification unit - polycondensation reaction unit - end polycondensation reaction unit, and finally qualified PET products are obtained; a terephthalic acid with impurities is used as the material, and the material undergoes hydrogen refining, crystallization and solid-liquid separation, and the terephthalic acid with the water content of approximately 10 percent is obtained, and the terephthalic acid obtained is mixed with the glycol and made into pulp, and the pulp has water contained in the pulp removed in the evaporation dehydration unit and enters the esterification, and the esterification steam enters an esterification dehydrating tower for dehydration, and the tower top steam in the esterification dehydrating tower is led to the pulp dehydration unit and used as the energy needed for dehydration; glycols discharged from the bottom parts of the esterification dehydrating tower and an evaporation dehydrating tower are returned to the pulping unit. The novel process has the advantages of simple process and great reduction of energy consumption, etc.
Description
Technical field
The present invention relates to the production technique of polyethylene terephthalate, specifically a kind of is the technology of raw material production polyester with the aromatic carboxylic acid, belongs to chemical production technical field.
Background technology
Polyethylene terephthalate (being called for short PET) is a kind of important thermoplastic macromolecule material, extensively applies to aspects such as fiber, polyester bottles, engineering plastics.The main technique method of producing is to be raw material with pure terephthalic acid and ethylene glycol, makes through the esterifying polycondensation reaction.Terephthalic acid in its raw material, be to obtain impure crude terephthalic acid with p-Xylol air liquid phase oxidation reaction, crude terephthalic acid obtains pure terephthalic acid's (being called for short PTA) again and makes after operations such as hydrofining, crystallization, separation, drying, dried PTA is air conveying to polyester device through solid, be made into slurry with ethylene glycol and carry out esterification, wherein, need a plurality of feed bins of configuration and gas-solid handling equipment.Not only exist technical process long, also there is dust explosion risk in shortcomings such as energy consumption height.The PTA industrial scale is increasing at present, the single series production capacity has reached more than 1,000,000 tons, PTA after the hydrofining of the process aqueous solution is after solid-liquid separation, generally contain the water about 10%, all adopt the desiccating method dehydration at present, rotary drier commonly used carries out drying, and this is the energy consumption height not only, and still do not have sophisticated megaton PTA drying machine production technology at present in the world, existing processes can not adapt to the needs of scale operation.Existing polyester production process is: after terephthalic acid and ethylene glycol are made into slurry, in esterifier, carry out esterification, product after the esterification is again through appending esterification, operation such as precondensation and aftercondensated obtains required polyester product, in esterification, the water that esterifier produces evaporates with part ethylene glycol, in the normal pressure dehydration tower, dewater, ethylene glycol at the bottom of the tower returns reaction member, the steam of cat head adopts water cooling, and the steam of cat head not only is not fully utilized like this, has also consumed a large amount of water coolants, the whole production technical process is long, the energy consumption height, cost height, the needs of incompatibility scale operation.
Summary of the invention
The objective of the invention is the defective at the production technique of existing polyethylene terephthalate, propose a kind of new process of production of polyethylene terephthalate, shortened process reduces production energy consumption.
The objective of the invention is to be achieved through the following technical solutions: a kind of production technique of polyethylene terephthalate, its step comprises the poly-reaction member of feed preparation unit-join slurry unit-de-watering of slurries unit-esterification unit-polycondensation unit-final minification, and the operation steps of described feed preparation unit is crude terephthalic acid and water to be made into slurry hydrofining post crystallization carry out solid-liquid separation and obtain the pure terephthalic acid; In the de-watering of slurries unit, also contain the dehydration by evaporation unit; The catalyzer that uses in the hydrogenation step of described feed preparation unit is a heavy metal catalyst, comprises palladium-carbon catalyst and rhodium C catalyst, and its range of reaction temperature is 260-300 ℃, pressure range 47-86bar; The described slurry unit of joining adopts ethylene glycol to mix with the pure terephthalic acid, and its mol ratio is 1-3; Unitary ethylene glycol of described de-watering of slurries and pure terephthalic acid's mol ratio is 1.0-2.5; Described dehydration by evaporation unit is a vacuum operating, and the scope of vacuum pressure is 50-200mmHg, comprises dehydration by evaporation step, esterification dehydrating step and steam spray step, wherein, in the dehydration by evaporation step, the slurry unit is joined in the ethylene glycol introducing of dehydration by evaporation tower bottom; The pressure condition of the esterification dehydration tower in the esterification dehydrating step is more than the 1bar, and the steam of a cat head part is introduced described de-watering of slurries unit, and another part is set up vacuum, and the ethylene glycol at the bottom of the tower is introduced and joined the slurry unit; Contain first esterifier and second esterifier in the described esterification unit, the pressure range of described esterifier is 1-4bar, and the steam of described first esterifier enters described esterification dehydration tower dehydration; Described ethylene glycol is made up of the ethylene glycol of ethylene glycol, the recovery of dehydration by evaporation tower and the ethylene glycol that the esterification dehydration tower reclaims.
The objective of the invention is further to realize by the following technical programs:
(1) will contain the slurry of 20-40% crude terephthalic acid, under 280 ℃, carry out carrying out solid-liquid separation with filter again by the crystallizer crystallization behind the catalytic hydrogenation reaction in hydrogenator with palladium carbon catalyst, waste liquid is discharged, and obtains moisture 10% pure terephthalic acid;
(2) be 2 in making beating jar, to be made into slurry in molar ratio with ethylene glycol and above-mentioned pure terephthalic acid;
(3) above-mentioned slurry is dewatered, and control ethylene glycol and pure terephthalic acid's mol ratio is 2 that wherein the vacuum tightness of dehydration by evaporation step is 100mmHg, and the ethylene glycol of dehydration by evaporation tower bottom is introduced in the described making beating jar in evaporating pot; The pressure of esterification dehydration tower is 1.5bar, and the steam part of cat head is introduced described de-watering of slurries unit, and another part is set up vacuum, and the ethylene glycol at the bottom of the tower is introduced and joined the slurry unit;
(4) slurry after the above-mentioned dehydration enters first esterifier and carries out esterification, reaction pressure is 2bar, reaction back moisture vapor enters esterification dehydration tower dehydration in the step (3), after material enters follow-up second esterifier reaction, through polycondensation, final polycondensation reactor, obtain the polyester finished product; In described step (1), carry out solid-liquid separation with filter after, slurry enters making beating jar making beating once more again, and by after filter after the row solid-liquid separation, obtain moisture 10% pure terephthalic acid, wherein filtrate cycle is used.
To be raw material with the p-Xylol obtain crude terephthalic acid or directly be raw material with the crude terephthalic acid through oxidizing reaction in the present invention, earlier crude terephthalic acid and water are made into slurry, under High Temperature High Pressure, hydrofining becomes easily water-soluble material with impurity conversion wherein, removes in the Crystallization Separation unit in road, back.The slurry of crystallization gained or through solid-liquid separation, the slurry that obtains after the washing once more obtains moisture terephthalic acid about 10% through solid-liquid separation.This moisture PTA and ethylene glycol are made into slurry, and slurry removes the moisture in the slurry through the dehydration by evaporation unit, enter esterifier and carry out esterification, and what the ethylene glycol discharging of dehydration by evaporation tower bottom turned back to moisture PTA joins the slurry unit.The dehydration by evaporation unit adopts vacuum operating, and the steam that adopts a part of esterification dehydration tower is thermal source, and other parts steam is used for vapor jet pump and sets up vacuum or the outer steam that supplies of part employing.Esterification reaction pressure is controlled in the 1.2-3.5bar scope, and the moisture vapor of esterifier enters the dehydration of esterification dehydration tower, and the pressure-controlling of esterification dehydration tower is operated under identical with esterifier or low slightly pressure, and control pressure is more than 1bar.Esterification dehydration column overhead steam is incorporated into the de-watering of slurries unit, is used to the required energy that dewaters.The ethylene glycol of esterification dehydration tower bottom is incorporated into the slurrying unit of moisture PTA.The material that esterifier comes out enters into the follow-up poly-reaction member of esterification, precondensation and final minification that appends and reacts, and obtains the PET product of required specification.The invention has the beneficial effects as follows: in feed preparation unit, cancelled drying, PTA conveying, intermediate bunker in the existing technology, PTA weighs and pull an oar the unit, saved drier unit, technology is simple, dexterously the steam at esterification dehydration tower top is introduced the de-watering of slurries unit, for de-watering of slurries provides the energy, reduced of the consumption of esterification dehydration tower overhead vapor with water of condensation, saved the steam consumption of drying machine, thus the purpose that reaches shortened process, significantly cuts down the consumption of energy, reduces cost.
Description of drawings
Fig. 1 is one embodiment of the present of invention process flow sheet;
Fig. 2 is an alternative embodiment of the invention process flow sheet;
Wherein the corresponding relation of label and equipment is: 1. the making beating jar, 2. evaporating pot, 3. first esterifier, 4. second esterifier, 5. polycondensation reactor, 6. final polycondensation reactor, 7. the dehydration by evaporation tower, 8. the esterification dehydration tower, 9. vapor jet pump, 10. knockout drum, 11. filters, 12. crystallizers, 13. hydrogenators, 14. crude terephthalic acid slurry, 15. ethylene glycol, 16 polyester products, 17. waste liquids, 18. are played oar jar, 19. again after filter, 20. filtrates.
Embodiment
The present invention has developed a kind of production of polyester novel process, preparation material unit: will contain 0-5000ppm the crude terephthalic acid and the de-salted water of carboxyl benzaldehyde and other foreign pigment is made into the slurry that contains terephthalic acid 20-40%, slurry is heated between 260-300 ℃, at heavy metal catalyst, as palladium carbon catalyst, under the effect of catalyzer such as rhodium Pd/carbon catalyst, hydrogenation reaction takes place in hydrogenator, to become easily water-soluble material to impurity conversion such as carboxyl benzaldehydes, Crystallization Separation is removed in follow-up crystallizer.Crystallizer can be one or more polyphone.Terephthalic acid slurries after the crystallization are after solid-liquid separation, or through after washing solid-liquid separation once more, obtaining raw material is moisture wet PTA at 7-15%; Join the slurry unit: should moisture PTA and ethylene glycol in making beating jar, be made into slurry, wherein the mol ratio of ethylene glycol and PTA is controlled between the 1-3, joins the used ethylene glycol of slurry and is made up of three parts: the ethylene glycol that the ethylene glycol that fresh ethylene glycol, dehydration by evaporation tower reclaim, esterification dehydration tower reclaim; The de-watering of slurries unit: this slurry enters in the evaporating pot, and it is thermal source that evaporating pot adopts the part steam at esterification dehydration tower top; The dehydration by evaporation unit: dewater in the dehydration tower that enters the top of water that is evaporated and ethylene glycol, the ethylene glycol of dehydration tower bottom turns back to joins the slurry unit.This vapo(u)rization system is the reduction vaporization system, and adopting the steam of esterification dehydration tower is power, and esterification dehydration column overhead steam is incorporated into the de-watering of slurries unit, and required energy and set up vacuum is used to dewater.The slurrying unit that the ethylene glycol of esterification dehydration tower bottom is incorporated into moisture PTA is used for slurrying, adopt two-stage or multistage steam squirt pump or adopt the outer steam that supplies to set up vacuum, vacuum pressure is at the 50-150mm mercury column, slurry is after the dehydration by evaporation unit removes moisture in the slurry, and the mol ratio of ethylene glycol and PTA is controlled in the 1.0-2.5 scope; Esterification unit: enter and carry out esterification in first esterifier, reaction pressure is controlled in the 1.2-3.5bar scope, the moisture vapor of esterifier enters the dehydration of esterification dehydration tower, the pressure-controlling of esterification dehydration tower is operated under identical with esterifier or low slightly pressure, make its pressure at 1-3.5bar, the material that first esterifier comes out enters into the second follow-up esterifier and reacts to polycondensation and the poly-reaction member of final minification, obtains the PET product of required specification.
Below in conjunction with accompanying drawing technical scheme of the present invention is further specified:
Embodiment one
The technical process of present embodiment as shown in Figure 1, with crude terephthalic acid 37649kg/hr and de-salted water 76074kg/hr, be mixed with slurry 14, be warmed up to 290 ℃, enter into the hydrogenator 13 that palladium carbon catalyst is housed, feed the hydrogen of 8.9kg/hr, the slurry that comes out enters into the crystallizer 12 of 5 polyphones, decrease temperature and pressure progressively, the temperature of last crystallizer is 150 ℃.After slurry process filter 11 solid-liquid separation that crystallizer comes out, filtrate is discharged as waste liquid 17, and solid enters in the making beating jar 1, adds fresh ethylene glycol 11480kg/hr, adds simultaneously from the ethylene glycol of dehydration by evaporation tower 7 and the backflow of esterification dehydration tower 8 bottoms; The material that comes out in the making beating jar 1 enters into evaporating pot 2, the top of evaporating pot connects the dehydration by evaporation tower, after connect two vapor jet pumps 9, adopting the steam of esterification dehydration tower 8 cats head is power, set up the vacuum of 150mmHg, glycol content is less than 0.5% in the water at the top of dehydration by evaporation tower, and ethylene glycol content is greater than 90% in the tower bottom discharging, and bottom discharge turns back in the making beating jar 1; The ethylene glycol slurry that evaporating pot 2 comes out enters in first esterifier 3 esterification takes place, esterification reaction temperature is 272 ℃, 20.bar, the water that esterification generates enters in the esterification dehydration tower 8 with ethylene glycol, the concentration of ethylene glycol is less than 0.5% in the water vapour of cat head, the concentration of ethylene glycol is greater than 90% in the discharging at the bottom of the tower, and discharging turns back in the making beating jar 1 at the bottom of the tower; The material that esterifier comes out enters into second esterifier 4, polycondensation reactor 5 and final polycondensation reactor 6, and esterifying polycondensation obtains required PET16.
Embodiment two
The technical process of present embodiment as shown in Figure 2, with crude terephthalic acid 28819kg/hr and de-salted water 67244kg/hr, be mixed with slurry 14, be warmed up to 280 ℃, enter into the hydrogenator 13 that palladium carbon catalyst is housed, feed the hydrogen of 8.6kg/hr, the slurry that comes out enters into the crystallizer 12 of 5 polyphones, decrease temperature and pressure progressively, the temperature of last crystallizer is 148 ℃.After slurry process filter 11 solid-liquid separation that crystallizer comes out, filtrate is discharged as waste liquid 17, solid enters making beating jar 18 again, with fresh de-salted water making beating washing, the de-salted water consumption is 67244kg/hr, enter into after filter 19 from jar 18 slurries that come out of pulling an oar again, filtrate 20 recycles, and is used for making beating jar 1 making beating; Solid enters in the making beating jar 1, adds fresh ethylene glycol 10850kg/hr, adds simultaneously from the ethylene glycol of dehydration by evaporation tower 7 and the backflow of esterification dehydration tower 8 bottoms; The material that comes out in the making beating jar 1 enters into evaporating pot 2, the top of evaporating pot connects the dehydration by evaporation tower, after connect two vapor jet pumps 9, adopting the steam of esterification dehydration tower 8 cats head is power, set up the vacuum of 100mmHg, glycol content is less than 0.5% in the water at the top of dehydration by evaporation tower, and ethylene glycol content is greater than 90% in the tower bottom discharging, and bottom discharge turns back in the making beating jar 1; The ethylene glycol slurry that evaporating pot 2 comes out enters in first esterifier 3 esterification takes place, esterification reaction temperature is 269 ℃, 1.5bar, the water that esterification generates enters in the esterification dehydration tower 8 with ethylene glycol, the concentration of ethylene glycol is less than 0.5% in the water vapour of cat head, the concentration of ethylene glycol is greater than 90% in the discharging at the bottom of the tower, and discharging turns back in the making beating jar 1 at the bottom of the tower; The material that esterifier comes out enters into second esterifier 4, polycondensation reactor 5 and final polycondensation reactor 6, and esterifying polycondensation obtains required PET16.
In addition to the implementation, the present invention can also have other embodiments.All employings are equal to the technical scheme of replacement or equivalent transformation formation, all drop on the protection domain of requirement of the present invention.
Claims (9)
1. the production technique of a polyethylene terephthalate, its step comprises the poly-reaction member of feed preparation unit-join slurry unit-de-watering of slurries unit-esterification unit-polycondensation unit-final minification, it is characterized in that: the operation steps of described feed preparation unit is crude terephthalic acid and water to be made into slurry hydrofining post crystallization carry out solid-liquid separation and obtain the pure terephthalic acid; In the de-watering of slurries unit, also contain the dehydration by evaporation unit.
2. the production technique of a kind of polyethylene terephthalate according to claim 1, it is characterized in that: the catalyzer that uses in the hydrogenation step of described feed preparation unit is a heavy metal catalyst, comprise palladium carbon catalyst and rhodium Pd/carbon catalyst, its range of reaction temperature is 260-300 ℃, and pressure range is 47-86bar.
3. the production technique of a kind of polyethylene terephthalate according to claim 1 is characterized in that: the described slurry unit of joining adopts ethylene glycol to mix with the pure terephthalic acid, and its mol ratio is 1-3.
4. the production technique of a kind of polyethylene terephthalate according to claim 1, it is characterized in that: unitary ethylene glycol of described de-watering of slurries and pure terephthalic acid's mol ratio is 1.0-2.5.
5. the production technique of a kind of polyethylene terephthalate according to claim 1, it is characterized in that: described dehydration by evaporation unit is a vacuum operating, the scope of vacuum pressure is 50-200mmHg, comprise dehydration by evaporation step, esterification dehydrating step and steam spray step, wherein, in the dehydration by evaporation step, the slurry unit is joined in the ethylene glycol introducing of dehydration by evaporation tower bottom; The pressure condition of the esterification dehydration tower in the esterification dehydrating step is more than the 1bar, and the steam of a cat head part is introduced described de-watering of slurries unit, and another part is set up vacuum, and the ethylene glycol at the bottom of the tower is introduced and joined the slurry unit.
6. the production technique of a kind of polyethylene terephthalate according to claim 1, it is characterized in that: contain first esterifier and second esterifier in the described esterification unit, the pressure range of described esterifier is 1-4bar, and the steam of described first esterifier enters described esterification dehydration tower dehydration.
7. the production technique of a kind of polyethylene terephthalate according to claim 2 is characterized in that: the ethylene glycol that ethylene glycol that described ethylene glycol is reclaimed by ethylene glycol, dehydration by evaporation tower and esterification dehydration tower reclaim is formed.
8. the production technique of a kind of polyethylene terephthalate according to claim 1 is characterized in that:
(1) will contain the slurry of 20-40% crude terephthalic acid, under 280 ℃, carry out carrying out solid-liquid separation with filter again by the crystallizer crystallization behind the catalytic hydrogenation reaction in hydrogenator with palladium carbon catalyst, waste liquid is discharged, and obtains moisture 10% pure terephthalic acid;
(2) be 2 in making beating jar, to be made into slurry in molar ratio with ethylene glycol and above-mentioned pure terephthalic acid;
(3) above-mentioned slurry is dewatered, and control ethylene glycol and pure terephthalic acid's mol ratio is 2 that wherein the vacuum tightness of dehydration by evaporation step is 100mmHg, and the ethylene glycol of dehydration by evaporation tower bottom is introduced in the described making beating jar in evaporating pot; The pressure of esterification dehydration tower is 1.5bar, and the steam part of cat head is introduced described de-watering of slurries unit, and another part is set up vacuum, and the ethylene glycol at the bottom of the tower is introduced and joined the slurry unit;
(4) slurry after the above-mentioned dehydration enters first esterifier and carries out esterification, reaction pressure is 2bar, reaction back moisture vapor enters esterification dehydration tower dehydration in the step (3), after material enters follow-up second esterifier reaction, through polycondensation, final polycondensation reactor, obtain the polyester finished product.
9. the production technique of a kind of polyethylene terephthalate according to claim 8, it is characterized in that: in the described step (1), after carrying out solid-liquid separation with filter, slurry enters making beating jar making beating once more again, and pass through after filter after the row solid-liquid separation, obtain moisture 10% pure terephthalic acid, wherein filtrate cycle is used.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008101229224A CN101302285B (en) | 2008-06-20 | 2008-06-20 | production process of polyethylene glycol terephthalate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008101229224A CN101302285B (en) | 2008-06-20 | 2008-06-20 | production process of polyethylene glycol terephthalate |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101302285A true CN101302285A (en) | 2008-11-12 |
| CN101302285B CN101302285B (en) | 2011-11-30 |
Family
ID=40112398
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2008101229224A Active CN101302285B (en) | 2008-06-20 | 2008-06-20 | production process of polyethylene glycol terephthalate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101302285B (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN104109230A (en) * | 2013-04-17 | 2014-10-22 | 中国石油化工股份有限公司 | Continuous production method of PBT-PET copolyester |
| CN104558563A (en) * | 2015-01-13 | 2015-04-29 | 浙江万凯新材料有限公司 | Device for synthesizing uniaxially stretching film-grade PET polyester chip and synthesis method using device |
| CN110354788A (en) * | 2019-08-09 | 2019-10-22 | 江苏恒科新材料有限公司 | A kind of esterification device of polyester |
| CN113396003A (en) * | 2019-02-01 | 2021-09-14 | Ifp 新能源公司 | Process for producing terephthalic acid esters incorporating depolymerization process |
| CN114516793A (en) * | 2022-02-23 | 2022-05-20 | 中国科学院大连化学物理研究所 | Method for producing terephthalic acid ester by continuous esterification |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3300613B2 (en) * | 1996-09-12 | 2002-07-08 | 三井化学株式会社 | Method for producing polyethylene terephthalate |
| CN1100749C (en) * | 2000-09-20 | 2003-02-05 | 中国石化集团扬子石油化工有限责任公司 | Palladium-carbon catalyst on-line regeneration method for terephthalic acid production apparatus |
| CN100415710C (en) * | 2002-10-24 | 2008-09-03 | 中国石油化工股份有限公司 | Process for preparing glycol terephthalate from terephthalic acid and glycol |
| CN2592645Y (en) * | 2002-12-17 | 2003-12-17 | 中国石化仪征化纤股份有限公司 | Apparatus for continuous production from crude terephthalic acid to polythylene glycol terephthalate |
-
2008
- 2008-06-20 CN CN2008101229224A patent/CN101302285B/en active Active
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104109230A (en) * | 2013-04-17 | 2014-10-22 | 中国石油化工股份有限公司 | Continuous production method of PBT-PET copolyester |
| CN104109230B (en) * | 2013-04-17 | 2016-10-05 | 中国石化仪征化纤有限责任公司 | The continuous production method of PBT-PET copolyesters |
| 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 |
| CN104558563A (en) * | 2015-01-13 | 2015-04-29 | 浙江万凯新材料有限公司 | Device for synthesizing uniaxially stretching film-grade PET polyester chip and synthesis method using device |
| CN104558563B (en) * | 2015-01-13 | 2016-07-20 | 浙江万凯新材料有限公司 | The synthesizer of simple tension film level PET polyester slice and apply the synthetic method of this device |
| CN113396003A (en) * | 2019-02-01 | 2021-09-14 | Ifp 新能源公司 | Process for producing terephthalic acid esters incorporating depolymerization process |
| CN110354788A (en) * | 2019-08-09 | 2019-10-22 | 江苏恒科新材料有限公司 | A kind of esterification device of polyester |
| CN114516793A (en) * | 2022-02-23 | 2022-05-20 | 中国科学院大连化学物理研究所 | Method for producing terephthalic acid ester by continuous esterification |
| CN114516793B (en) * | 2022-02-23 | 2024-05-07 | 中国科学院大连化学物理研究所 | Method for producing terephthalic acid ester by continuous esterification |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101302285B (en) | 2011-11-30 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101302285B (en) | production process of polyethylene glycol terephthalate | |
| CN1258512C (en) | Process for production of purified terephthalic acid | |
| CN105001073A (en) | PTA production method with low energy consumption, low material consumption andlow refuse discharge | |
| CN101531588A (en) | Method for preparing new purified terephthalic acid | |
| CN110078284B (en) | Water-rich solvent grading utilization emission reduction system for preparing terephthalic acid | |
| CN103183607B (en) | A kind of production method mixing fragrant dioctyl phthalate | |
| KR101532157B1 (en) | Optimized production of aromatic dicarboxylic acids | |
| CN103025700A (en) | Production of aromatic carboxylic acids | |
| CN110573486B (en) | Energy and environment integrated process for producing aromatic dicarboxylic acids by oxidation | |
| CN204874349U (en) | PTA production system that low energy consumption material consumption, few wastes material discharged | |
| CN1951900A (en) | Low-energy consumption preparation method of terephthalic acid | |
| CN104119225A (en) | New technology for producing ethyl acetate through reactive distillation by taking mixed ionic liquid as catalyst | |
| CN101434539B (en) | Preparation of benzyl acetate | |
| CN114984866B (en) | System and method for preparing dimethyl maleate | |
| CN1307109C (en) | Method for recovering aromatic carboxylic acid in waste water | |
| CN102775538A (en) | Production method of polyvinyl alcohol | |
| CN106220489B (en) | The method for producing M-phthalic acid as raw material using paraxylene raffinate | |
| CN100460400C (en) | Continuous production process of high purity trimellitic anhydride with trimellitic acid | |
| CN111943918A (en) | Five-tower continuous rectification process for furfural | |
| KR100539285B1 (en) | Recovery system of waste polyester oligomer using hybrid process of methanolysis reactor and distillation | |
| CN101747177A (en) | Device and method for preparing butane diacid by continuously hydrolyzing dialkyl succinate ester | |
| CN100391929C (en) | Method of drying terephthalic acid | |
| CN101508638A (en) | Method for preparing mixed benzol dioctyl phthalate and benzene acetic acid | |
| CN100447124C (en) | Method for producing meta benzene tricarbonic acid through sequential oxidation by using intermittent multiple cascaded Bubbling oxidation towers | |
| KR101392543B1 (en) | Optimized production of aromatic dicarboxylic acids |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20160122 Address after: 211900 Yizheng Changjiang Road, Jiangsu, China, No. 1, No. Patentee after: CHINA SINOPEC YIZHENG CHEMICAL FIBER CO., LTD. Address before: 211900 Xu Town, Jiangsu City, Yizheng Province Patentee before: Yizheng Chemical Fiber Co., Ltd., China Petrochemical Group Corp. |