CN1743305A

CN1743305A - Processes for the purification of bis(2-hydroxyethyl)terephthalate

Info

Publication number: CN1743305A
Application number: CN 200510097626
Authority: CN
Inventors: 稻田修司; 佐藤菊智
Original assignee: AIES Co Ltd
Current assignee: AIES Co Ltd
Priority date: 2002-06-04
Filing date: 2003-05-30
Publication date: 2006-03-08
Anticipated expiration: 2023-05-30
Also published as: CN100344604C

Abstract

An object of the present invention is to provide a method of obtaining BHET of high purity efficiently from an EG (ethylene glycol) solution containing crude BHET (bis(2-hydroxyethyl)terephthalate), especially a decomposition product solution obtained by decomposing a polyester containing PET (polyethylene terephthalate) as a main component, by use of EG, while minimizing by-production of impurity components such as DEG (diethylene glycol), DEG ester and oligomers. The present invention is a method of purifying BHET by subjecting the decomposition product solution to crystallization and solid-liquid separation under specific temperature conditions. Further, the present invention is a method of purifying BHET which comprises evaporation steps of evaporating low-boiling-point components from the decomposition product solution under specific conditions so as to obtain a melt solution and a molecular distillation step of distilling the obtained melt solution under specific conditions so as to obtain a specific fraction.

Description

The process for purification of terephthalic acid two (2-hydroxyethyl) ester

Technical field

The present invention relates to the process for purification of terephthalic acid two (2-hydroxyethyl) ester.In more detail, relate to by being that the ethylene glycol solution of crude terephthalic acid two (2-hydroxyethyl) ester of impurity implements down in specified conditions that partial crystallization is handled and/or distillation handles the process for purification that obtains high-quality terephthalic acid two (2-hydroxyethyl) ester with good efficiency containing with terephthalic acid 2-hydroxyethyl [2-(2-hydroxyl-oxethyl) ethyl] ester and oligopolymer.

Background technology

Polyester, particularly polyethylene terephthalate (hereinafter to be referred as PET) are widely used in various goods fields such as fiber, film, resin.Although PET is normally by making with the method for dimethyl terephthalate (DMT) or terephthalic acid and ethylene glycol (hereinafter to be referred as EG) reaction in the presence of catalyzer, but, for it is satisfied with the needed characteristic of purposes, in reaction, also added such as characteristic imparting agents such as stablizer, tinting material, static inhibitor, UV light absorber.Particularly PET is being used under the situation of beverage-container recently, kind according to institute's storage product in the container, in order to keep its quality, just require it to have the so-called performance that intercepts ultraviolet ray and trapping, for this countermeasure of taking has, for example, with UV light absorber or gas barrier properties mixed with polymers, perhaps use thus polymkeric substance with the laminated vessel of thin layer mode lamination.

On the other hand, polyethylene terephthalate goods, the particularly bottle made from polyethylene terephthalate (PET bottle) with the discarded social concern that can cause environmental degradation in back, have therefore carried out the work that it is reclaimed, utilizes.

One of method is so-called material regeneration method, that is, the used PET bottle of retrieving is pulverized, and after the smear metal or the thin slice that obtain are cleaned, made with extra care, provides the shaping raw material as other molded article.The problem of the shaping raw material PET that obtains of method is thus, it is extremely difficult to prevent sneaking into of impurity such as metal, glass, other resin, in other words, the utmost point is difficult to low cost and removes such impurity, the production efficiency that the existence of this type of impurity has caused other molded article to be made is low, reduce the quality of goods, also improved manufacturing cost.Also have, if the PET bottle that in the PET bottle that reclaims, is mixed with painted, very high the cost that they separate, this has just improved the cost of resulting shaping raw material, therefore be to stop using painted PET bottle as avoiding the means of this situation, and so that be used in the method that the body of clear PET bottle partly sticks coloured labels and replace.Yet this means not only impair attractive in appearance, have improved cost, but also the problem that has the coloured labels effect to lack perfection.Furtherly, dissimilar polymer or lamination are sneaked in employing give functional PET bottle, it also is extremely difficult distinguishing them.

To the regeneration of PET bottle, also inquired into some other method, one of them is exactly the chemical regeneration method.Employing this method such as the inventor are carried out manipulation of regeneration to the PET bottle, smear metal of the PET bottle that reclaims being pulverized and obtaining or thin slice are with excessive ethylene glycol depolymerization, (depolymerization reaction generates solution: EG solution) carry out refinement treatment then resulting decomposition to be generated solution, to make highly purified terephthalic acid two (2-hydroxyethyl) ester (hereinafter to be referred as BHET), discover, above-mentioned reaction generates solution just can obtain high-purity BHET after the refinement treatment through combining decolouring, disengaging, partial crystallization, distillation etc., the scheme that has proposed please refer to patent documentation 1～16.

Patent documentation 1: the spy opens the 2000-53802 communique

Patent documentation 2: the spy opens the 2000-169623 communique

Patent documentation 3: the spy opens the 2000-239233 communique

Patent documentation 4: the spy opens the 2001-18224 communique

Patent documentation 5: the spy opens the 2001-48834 communique

Patent documentation 6: the spy opens the 2001-48835 communique

Patent documentation 7: the spy opens the 2001-48836 communique

Patent documentation 8: the spy opens the 2001-48837 communique

Patent documentation 9: the spy opens the 2001-322967 communique

Patent documentation 10: the spy opens the 2001-335539 communique

Patent documentation 11: the spy opens the 2002-121173 communique

Patent documentation 12: the international reprint that discloses No. 01/10812

Patent documentation 13: the international reprint that discloses No. 01/19775

Patent documentation 14: the international reprint that discloses No. 01/29110

Patent documentation 15: the international reprint that discloses No. 01/56970

Patent documentation 16: the international reprint that discloses No. 02/10117

The inventor etc. find in for the purification efficiency that further improves the method, research that quality is carried out, because the impurity component beyond the BHET, diethylene glycol (hereinafter to be referred as DEG) composition and functional as the employed composition of purpose to give particularly, therefore reduced the quality of BHET, the concentration problems of doing one's utmost to suppress these compositions in goods BHET has been inquired into.

Owing to contain the DEG composition and give functional composition at the raw material (PET bottle) that is used for chemical regeneration, therefore must the limit suppress the side reaction limit of these compositions they are removed effectively.

Also have, the DEG composition produces as the accessory substance in the depolymerization operation on one side, Yi Bian be again in decomposing the refinement treatment process that generates solution, when for example breaking away from sub the processing, is generated by the EG dehydrating condensation. Also have, terephthalic acid (TPA) 2-ethoxy [2-(2-hydroxyl-oxethyl) ethyl] ester (hereinafter to be referred as the DEG ester) that is generated by the ester exchange reaction of DEG and BHET also causes the decline of BHET quality. And the characteristic of DEG composition and EG or BHET are very close sometimes, extremely remove difficult the separation from goods BHET.

Summary of the invention

The inventor etc. are to have found by decomposing the concentration that the partial crystallization condition that generates solution can reduce the DEG composition in the precipitate and give functional ingredient the result of the discussion of effective process for purification of BHET.

Also find, the BHETs many with giving functional ingredient the DEG composition carry out molecular distillation, then or be to allow the DEG composition among the goods BHET and give functional ingredient to become many, be to have to reduce the goods yield, in order to prevent this situation, effectively to remove the DEG composition as far as possible and give functional ingredient and prevent that it from producing as by product in the operation in front.

Also discovery, when partial crystallization BHET from decomposition generation solution, because the partial crystallization of BHET is decomposed the influence of the specific conductivity that generates solution, thereby therefore for the greatly easy solid-liquid separation of the crystal size that makes its precipitate, it is effective that described specific conductivity is diminished.

The inventor etc. find that also when further distillation was refining BHET, this BHET is further polycondensation at high temperature, and by-product bears the oligopolymer of the polymerization degree 2～20.

So, the objective of the invention is to, the process for purification of BHET is provided: use EG contain the EG solution of thick BHET, particularly with PET decompose as the polyester of main component obtain, to contain with BHET be that main solute, EG generate in the treating process of solution as the decomposition of primary solvent, do one's utmost to suppress particularly production of by-products such as DEG, DEG ester and oligopolymer of impurity component, and separate these impurity with good efficiencies, thereby obtain highly purified BHET.

Another object of the present invention is, the method of partial crystallization separation BHET is provided: with EG the polyester that with PET is main component being decomposed resulting decomposition generation solution, particularly with EG the polyester that with recovery PET is main component decomposed resulting containing with BHET is that main solute, EG are in the solution of primary solvent, under the occasion that contains Diethylene Glycol composition and the composition (gas blocking agent composition) that comes from the gas barrier properties polymkeric substance, the partial crystallization separation obtains described gas blocking agent component content BHET still less.

Another purpose of the present invention is, provide effective partial crystallization to separate the method for BHET: by generating solution to the polyester that with PET is main component being decomposed resulting decomposition with EG, be that main solute, EG are the solution of primary solvent promptly with BHET, break away from son processing, partial crystallization processing, make that under the occasion that contains Diethylene Glycol composition and gas blocking agent composition the partial crystallization separation obtains described gas blocking agent component content BHET still less.

A further object of the present invention is, effective separation method is provided: to EG containing the EG solution of thick BHET, particularly being that the polyester of main component decomposes resulting decomposition and generates solution with PET, be that main solute, EG are the solution of primary solvent promptly with BHET, carry out that solvent is removed, molecular distillation, obtain Diethylene Glycol component content BHET still less.

Of the present invention also have a purpose to be, provide the process for purification of BHET: contain the EG solution of thick BHET, particularly the polyester that with PET is main component decomposed resulting decomposition generation solution with the EG handle, be that main solute, EG are the solution of primary solvent promptly with BHET, remove processing, molecular distillation through specific partial crystallization processing, solvent, to obtain high-quality BHET effectively.

Can further understand other purpose of the present invention and advantage in the following description.

According to the present invention, above-mentioned purpose of the present invention be by, the first, the ethylene glycol solution that contains crude terephthalic acid two (2-hydroxyethyl) ester adopted comprise

(1) this solution from the temperature more than the saturation solubility be cooled to the temperature of 15～30 ℃ of scopes and under the temperature of this scope, keep 1h at least the partial crystallization operation and

(2) with the terephthalic acid two (2-hydroxyethyl) of separating out ester is the precipitate of main component that while the temperature range that remains on 15～30 ℃ thus its solid-liquid separation to be obtained with terephthalic acid two (2-hydroxyethyl) ester be that the operation of solid-liquid separation process of the filter cake of main component comes the process for purification (hereinafter referred to as the 1st kind of method) of purified, terephthalic acid two (2-hydroxyethyl) ester to reach.

Above-mentioned purpose of the present invention is also passed through, and the second, the ethylene glycol solution employing that contains crude terephthalic acid two (2-hydroxyethyl) ester is comprised

Comprise that (1) (a) imports first evaporation unit to this solution, under the condition of 130～170 ℃ of temperature, pressure 300～1000Pa, boil off low boiling point component, obtain ethylene glycol and free Diethylene Glycol add up to content the fs evaporization process of first melting liquid of 3～10 weight % and

(b) this first melting liquid is imported second evaporation unit, under the condition of 130～170 ℃ of temperature, pressure 50～250Pa, boil off low boiling point component, obtain ethylene glycol and free Diethylene Glycol and add up to the evaporization process of content at the subordinate phase evaporization process of 0.45 weight % or second melting liquid below it, and

(2) this second melting liquid is imported the falling film type molecular distillation apparatus, under 180～220 ℃ of temperature, pressure 25Pa or the condition below it, distill, obtain with terephthalic acid two (2-hydroxyethyl) ester be main component, terephthalic acid 2-hydroxyethyl [2-(2-hydroxyl-oxethyl) ethyl] ester content 1.5 weight % or below it and oligomer come the process for purification (hereinafter referred to as the 2nd kind of method) of purified, terephthalic acid two (2-hydroxyethyl) ester to reach in the operation of the molecular distillation operation of 1 weight % or the cut below it.

Above-mentioned purpose of the present invention is also passed through, and the 3rd, the ethylene glycol solution employing that contains crude terephthalic acid two (2-hydroxyethyl) ester is comprised

(1) this solution from the temperature more than the saturation solubility be cooled to the temperature of 15～30 ℃ of scopes and under the temperature of this scope, keep at least 1 hour the partial crystallization operation,

(2) separate out with terephthalic acid two (2-hydroxyethyl) ester be the precipitate of main component carry out under the temperature that remains on 15～30 ℃ of scopes solid-liquid separation with obtain solid-liquid separation process that terephthalic acid two (2-hydroxyethyl) ester is the filter cake of main component,

Comprise that (3) (a) imports first evaporation unit to the melting liquid of this filter cake, under the condition of 130～170 ℃ of temperature, pressure 300～1000Pa, boil off low boiling point component, obtain ethylene glycol and free Diethylene Glycol add up to content the fs evaporization process of first melting liquid of 3～10 weight % and

(b) this first melting liquid is imported second evaporation unit, under the condition of 130～170 ℃ of temperature, pressure 50～250Pa, boil off low boiling point component, obtain ethylene glycol and free Diethylene Glycol add up to content the evaporization process of the subordinate phase evaporization process of 0.45 weight % or second melting liquid below it and

(4) this second melting liquid is imported the falling film type molecular distillation apparatus, under 180～220 ℃ of temperature, pressure 25Pa or the condition below it, distill, obtain with terephthalic acid two (2-hydroxyethyl) ester be main component, terephthalic acid 2-hydroxyethyl [2-(2-hydroxyl-oxethyl) ethyl] ester content 1.5 weight % or below it and oligomer come the process for purification (hereinafter referred to as the 3rd kind of method) of purified, terephthalic acid two (2-hydroxyethyl) ester to reach in the operation of the molecular distillation operation of 1 weight % or the cut below it.

Enumerate concrete example below and describe the present invention in detail.

Description of drawings

Fig. 1 is the process picture sheet of expression preferred distillation process of the present invention (water distilling apparatus combination state).In Fig. 1,1 is first evaporation unit, the 2nd, and condenser, the 3rd, the melting liquid transferpump, 4 is second evaporation units, the 5th, condenser, the 6th, melting liquid transferpump, the 7th, phlegma receiver, the 8th, molecular distillation apparatus, the 9th, the internal condensation device, the 10th, heating arrangements, the 11st, goods outlet, the 12nd, the residual thing outlet of still kettle, the 13rd, cold medium circulation jar, the 14th, thermal medium jar.

Embodiment

At first, the 1st kind of method of the present invention is described.

(starting raw material)

In the 1st kind of method of the present invention, starting raw material is the EG solution that contains thick BHET, it preferably, with excessive EG is terephthalic acid polyester (particularly PET) depolymerization, in this process or after depolymerization, implement impurity and removed the ethylene glycol solution (EG solution) of processing, or the EG solution that obtains by the transesterification reaction of terephthalic acid and EG (serves as preferred to have carried out breaking away from the solution that son handles).

That is, the EG solution that contains thick BHET preferably, spent glycol the polyester that with the polyethylene terephthalate is main component decompose, then decolouring breaks away from son and handles resulting solution.

These EG solution are that main solute, EG are primary solvent with BHET, but they also can contain at least a composition among DEG ester (solute composition), oligopolymer (solute composition), the DEG (solvent composition) etc. as impurity component usually.Furtherly, can contain in this EG solution and give particularly gas blocking agent composition (solute composition) of functional ingredient.

In these solution, be the former terephthalic acid polyester (particularly PET) depolymerization, so that be used in this process or implemented impurity after the depolymerization and removed the solution of processing for preferred especially with excessive EG.In the operation before the partial crystallization operation that these EG solution are said in the back, normally in the temperature of not separating out solute (for example being higher than 50 ℃ temperature) and be no more than under 100 ℃ the temperature and handle, serve as preferred with Temperature Treatment at 70～90 ℃.

Described impurity is removed having that processing can enumerate out, and processing (for example heat filtering (Hot Time Filter Over)), the activated carbon decolorizing of removing solid foreign materials handles, utilizes disengaging of ion exchange resin to handle (decationized Y sieve is handled, exhaustion of yin ion processing) etc.This handles with the order of removing by foreign matter, activated carbon treatment, disengaging are handled and carries out to preferably.Therefore, contain the occasion of coloring material at EG solution, this coloring material can be handled and remove by breaking away from son.Also have, when containing insoluble polymkeric substance, can heat filtering be removed by this polymkeric substance.

As described terephthalic acid is polyester, serves as preferred with the polyester that constitutes the PET bottle.As described terephthalic acid is the PET bottle that polyester was to use, and can use the painted PET bottle that contains the ultraviolet isolating agent at least a portion of this PET bottle.

Described terephthalic acid is a polyester, except the PET homopolymer, that can also enumerate has its multipolymer, for example by phthalic acid, naphthalene dicarboxylic acids, diphenyl dicarboxylic acid and so on aromatic dicarboxylic acid, pentanedioic acid, hexanodioic acid and so on aliphaticdicarboxylic acid, cyclohexane diacid and so on alicyclic dicarboxylic acid waits other sour composition and 1, the 4-cyclohexanedimethanol is (hereinafter to be referred as 1,4-CHDM), propylene glycol, butyleneglycol, in other the diol component such as hexylene glycol more than one are with the copolyesters of small proportion (for example being equivalent to the 30mol% of all sour compositions or following, preferred 20mol% or following) copolymerization etc.In these, with PET (homopolymer) and multipolymer thereof for preferred especially.These polyester are all right with any method manufacturing.

At described terephthalic acid is in the polyester, if (for example be equivalent to the 40 weight % or following that all constitute polymkeric substance with small proportion, preferably at 30 weight % or following, more preferably at 20 weight % or following) dissimilar polymer, for example blended such as penylene dimethylamine (nylon MXD 6), polyglycolic acid between polyethylene glycol phthalate, PEN, polybutylene terephthalate, poly hexamethylene adipamide are good.Also have, (for example contain catalyzer that the polycondensation of polyester uses, antimony compounds, germanium compound etc.), stablizer (for example phosphorus compound) and tinting material (for example phthalocyanine based dye, anthraquinone based dye, monoazo based dye, ferric oxide, carbon black etc.) etc., also be fine.

At above-mentioned terephthalic acid is in the polyester, also mixes the polymkeric substance that the vapour barrier that constitutes the multilayer bottle is arranged, and for example penylene dimethylamine (nylon MXD 6), polyglycolic acid etc. between poly hexamethylene adipamide are good.

Described terephthalic acid is a polyester, normally decompose (depolymerization) with excessive EG, this decomposition reaction can be in order to by the previous method that proposes such as the inventor and condition, for example the described world discloses and gets off to carry out with regard to method and the condition known in the past headed by method that No. 01/10812 reprint puts down in writing and the condition.

For effectively carrying out this depolymerization reaction, preferably, for example, is terephthalic acid that polyester at first at high temperature contacts with the depolymerizing agent (the preferably distillation residue of thick BHET) that is main component with BHET and/or its condenses (the preferably oligopolymer of mean polymerisation degree in 1.1～10 scopes), carry out depolymerization (pre-depolymerization) in advance, secondly, use excessive EG and depolymerization catalyzer (for example alkali metal compound) further to carry out depolymerization, modulation contains the EG solution of thick BHET.This EG can use through purified EG, also can use by small proportion to contain the EG of other glycol and carry out the thick EG mixing that produces in the partial crystallization solid-liquid separation and the EG that gets at above-mentioned EG solution.Also having, is polyester with respect to 100 weight part terephthalic acids, and the depolymerization catalyzer of use is preferably 0.1～0.5 weight part, and 0.15～0.4 weight part is for more preferably.Used depolymerization catalyzer can have been enumerated sodium hydroxide, sodium methylate etc.

In pre-depolymerization, terephthalic acid is a polyester and the ratio of the consumption of BHET and/or its condenses is, per 1 weight part terephthalic acid is BHET and/or its condenses that polyester preferably uses 0.1～4.5 weight part, to use 0.1～2.0 weight part for more preferably, 0.1～1.0 weight part is for preferred especially.Pre-depolymerization temperature is preferably 180～290 ℃, with 190～270 ℃ for more preferably, 200～260 ℃ for preferred especially.Reaction times is preferably 0.1～5.0 hour, with 0.3～1.5 hour for more preferably.Be preferably by the mean polymerisation degree of pre-depolymerization resulting decomposition resultant (pre-depolymerizing substance) about 2～40, with about 5～30 for more preferably.

Preferably carry out by the depolymerization reaction of resulting pre-depolymerizing substance of pre-depolymerization and EG (formal depolymerization reaction), to carry out to more preferably at 190～220 ℃ at 170～265 ℃.The pre-depolymerizing substance of this pre-depolymerizing substance and preferably per 1 weight part of the ratio of the consumption of EG uses the EG of 0.5～8.0 weight part, to use 2.0～7.0 weight parts for more preferably.When the amount of pre-depolymerizing substance was very few with respect to EG, the amount of the BHET that is generated was lower than the saturation solubility in EG, and the amount that obtains is than lacking with respect to offering resulting maximum must the measuring of total liquid measure that breaks away from the son processing, and is uneconomical.On the other hand, when the amount of pre-depolymerizing substance is too much with respect to EG, increased the oligopolymer of BHET, the yield of BHET descends.Also have, BHET surpasses the saturation solubility of EG and when existing, can not break away from sub-processing because separating out of BHET makes.The depolymerization time is preferably 0.5～5.0 hour, with 0.5～2.0 hour for more preferably.To generate solution be by being that the solute of main component and solvent that EG is main component are constituted with BHET to the decomposition that obtains of depolymerization thus, the polymerization degree that may contain small proportion (the 20 weight % or following that for example are equivalent to total soluble matters are further at 10 weight % or following) is 2～20, further be 2～10 oligopolymer.

From just using the occasion of EG at first as above-mentioned depolymerizing agent, preferably 170～230 ℃ of depolymerization temperature, with at 190～220 ℃ for more preferably.Terephthalic acid be polyester with the ratio of the consumption of EG is 1: 9～3: 7 to serve as preferred with weight ratio during depolymerization.When terephthalic acid is the amount of polyester when very few with respect to the amount of EG, the amount of the BHET that is generated is lower than the saturation solubility in EG, and the amount that obtains is than breaking away from total liquid measure resulting maximum must measure of son in handling and lack with respect to offering, and is uneconomical.On the other hand, terephthalic acid is the amount of polyester when too much with respect to EG, has increased the oligopolymer of BHET, and the yield of BHET descends.Also have, BHET has surpassed the saturation solubility of EG and when existing, can not break away from sub-processing because separating out of BHET makes.

Above-mentioned depolymerization is carried out depolymerization for preferred in the depolymerization reaction device rectifying tower to be set while moisture is steamed outside system from reaction soln.At this moment, it serves as preferred getting back to again in the system with the ethylene glycol that steams.Because the depolymerization of carrying out like this makes the water yield in the EG solution that contacts with cation exchange column to reduce, just can suppress to be accompanied by the hydrolysis reaction that decationized Y sieve is handled.The amount of contained humidity in the EG solution that contacts with cation exchange column is adjusted at 0.5 weight % or following for preferred.MK-SS type Ka Er-Fischer (Karl-Fischer) moisture meter that the amount of moisture is made with capital of a country electronic industry (strain) is measured this EG solution and is obtained.

The decomposition generation solution that is obtained by described depolymerization reaction is main solute (decomposition product) with BHET normally, EG is main solvent, as secondary solute, it contains the raw material terephthalic acid is contained in the polyester (particularly PET), or the DEG ester that generates of the side reaction during by depolymerization, and further contain as other solute, the oligopolymer of BHET and terephthalic acid list (2-hydroxyethyl) ester (hereinafter to be referred as MHET) can also contain as the nonsolute composition, come from the DEG composition that is in the polyester to be contained at the raw material terephthalic acid and the free DEG of the DEG composition that side reaction generated during by depolymerization etc.Furtherly, at the raw material terephthalic acid is to mix the occasion that gas blocking agent is arranged in the polyester (particularly PET), also may contain catalyzer (for example antimony compounds, germanium compound etc.), stablizer (for example phosphorus compound) and tinting material (for example phthalocyanine based dye, anthraquinone based dye, monoazo based dye, ferric oxide, carbon black etc.) etc. that use in the polycondensation of catalyzer (for example alkali metal compound) that gas blocking agent composition and depolymerization use, polyester and the foreign ion that the various pollution that is difficult to expect brought etc.

In the 1st kind of method of the present invention, contain the EG solution of thick BHET, remove with its impurity and handle and solids component (solute) concentration of the solution of partial crystallization when handling serves as preferably at 5～40 weight %, 10～30 weight % are for more preferably, and 17～23 weight % are for preferred especially.Therefore, when the solid component concentration in the EG solution that depolymerization reaction (decomposition reaction) obtains can not satisfy this scope, preferably adjust concentration with EG.

In the 1st kind of method of the present invention, preferably, before carrying out the partial crystallization processing, the EG solution that contains thick BHET in the temperature of not separating out solute (for example being higher than 50 ℃ temperature) and be no more than under 100 ℃ temperature, preferred 70～90 ℃ temperature, decolour by active carbon layer earlier, further contact again, then contact, to reduce coloring components, positively charged ion and anionic content with anion ion exchange body with cation exchange column.

In this ion exchange treatment, the specific conductivity of EG solution is preferably 0.2～0.6 μ S/cm, and 0.2～0.5 μ S/cm is for more preferably.Furtherly, the pH of this EG solution is preferably 2.5～7.0, and 3.0～5.0 for more preferably.When specific conductivity during less than 0.2 μ S/cm, ion exchange treatment will long time, and this has just increased side reaction; And pH is lower than at 2.5 o'clock, that is to say, and near an acid side, also be not preferred.On the other hand, when greater than 0.6 μ S/cm, hindered partial crystallization handle in the growth of precipitation particles, precipitation particles is little, filtering yield is low and descend because of residual impurity makes quality, and is therefore not preferred.Be that specific conductivity can be measured by directly sample being used for the 873CC type electric conductivity meter that Fox Borrow (Off オ Star Network スボロ one) company makes again.

The sub-processing of the disengaging of above-mentioned EG solution can be make this EG solution by for example be filled in the middle of the post etc. the ion exchanger layer so that both contacts carry out.When the occasion that this EG solution is suspension, in the ion exchanger packing layer, to stop up, passing through of this EG solution is not smooth, perhaps by having caused bias current by the impedance spot, makes stable disengaging handle and is difficult to carry out.So, preferably, after as required 1 μ m or above solid impurity (for example particulate) being removed, on one side cation exchange column contact with EG solution with anion ion exchange body, one side the temperature of EG solution remains on below the maximum operation (service) temperature of ion exchange resin and the BHET crystallization is not separated out from EG solution temperature.

Generally, the maximum operation (service) temperature of cation exchange column is higher than anion ion exchange body, after cationic exchange is handled, EG solution being cooled to below the maximum operation (service) temperature of anion ion exchange body, or below the maximum operation (service) temperature of anion ion exchange body, carry out positively charged ion and anionresin is treated to.Under the general case, the positively charged ion proportion is more much more than anionic ratio in the ionic impurity, and, after cationic exchange is handled, EG solution obviously is partial to an acid side, this just with EG solution in side reaction (transesterification reaction of BHET and DEG and the hydrolysis reaction of BHET) interrelated, therefore adjust pH and after cationic exchange is handled, be preferred without just carrying out anionresin for a long time.

Among the present invention, the residence time that EG solution contacts with cation exchange column is 3～30 minutes, is divided into preferred with 3～15.Furtherly, decomposing Generation Liquid is 1～12 hour with the space velocity that contacts of cation exchange column ^-1, with 4～9 hours ^-1Space velocity carry out to more preferably.When this residence time less than 3 timesharing, can not carry out sufficient cationic exchange and handle, residual cationic katalysis makes BHET hang down dimerization; On the other hand, surpassed 30 fens, made BHET surpass permissible value to the inversion quantity of DEG ester by transesterification reaction, not preferred.

Therefore, with after cation exchange column contacts, EG solution must be 3 seconds or above 10 minutes with interior, preferably 3 seconds or above 5 minutes with interior, more preferably in 3 seconds or above 3 minutes, contact with anion ion exchange body.Thus, just can suppress above-mentioned transesterification reaction and hydrolysis reaction.

About the shape of cation exchange column and anion ion exchange body, they can be general shape, for example particle shape, chain, fibrous and amorphous.In emboliform occasion, for example, it is filled in the post, allow above-mentioned EG solution stream cross pillar, both just can contact.

Cation exchange column is preferred with the storng-acid cation exchange resin, and anion ion exchange body serves as preferred with the mixture of weak base anion-exchange resin and storng-acid cation exchange resin.The cationic exchange functional group of Zeo-karb has been enumerated, for example, and-SO ₃H ,-COOH etc.Zeo-karb can use, for example, IR120B, IR120BN, the commercially available products such as IR124,200CT of SK1B, the SK104 of the inferior clothing grace difficult to understand of enlightening (ダイヤイオ Application) of Mitsubishi Chemical's (strain) manufacturing, SK110, SK112, SK116 etc. or An Balaite (ア Application バ one ライト) (ロ-system ア Application De Ha-ス (strain) makes).Stabilized because its common ion exchange functional groups of these commercially available products has for example made salt such as sodium salt, therefore will regenerate in use is transformed into the common acidic group as above-mentioned to it and just uses.

The anion exchange functions of anionite-exchange resin group is being for example to have-NR ₂,-NH (C ₂H ₄NH) _nH ,-N ⁺R ₃(OH) ^-Deng (R: alkyl) person is preferred.As such anionite-exchange resin, IRA400J, IRA67, the commercially available products such as IRA96SB, XE583 of WA10, WA20, WA21J, WA30 etc. or the An Balaite (ロ-system ア Application De Ha-ス (strain) makes) of the inferior clothing of the enlightening that can use Mitsubishi Chemical's (strain) to make grace difficult to understand.In these commercially available products, its ion exchange functional groups that has usually of strongly basic anion exchange resin is not hydroxide ion OH ^-But as having the anionic material of halogen and stabilized, therefore to be transformed into it in use and have common material as above-mentioned hydroxyl.In these, with primary amine, secondary amine or tertiary amine serve as the exchange functional group weak base anion-exchange resin serve as preferred.

Since above-mentioned primary～tertiary amine-type anionite-exchange resin neutral so acid (being preferably acidity) and produce at first ion exchangeable-N ⁺R ₃(OH) ^-, preferably make the mixed bed of weak base anion-exchange resin and storng-acid cation exchange resin.The blending ratio of weak base anion-exchange resin and storng-acid cation exchange resin (volume ratio) is 1: 3～5: 1, serves as preferred with 1: 2～3: 1.

In above-mentioned anionresin was handled, the residence time that EG solution contacts with anion ion exchange body was 3～60 minutes, was divided into preferred with 3～40.Furtherly, EG solution is 0.5～10 hour with the space velocity that contacts of anion ion exchange body ^-1, with 1～8 hour ^-1Space velocity carry out to preferably.

In the 1st kind of method of the present invention,, preferably, measure specific conductivity, the pH of its EG solution, to confirm that these characteristics are in aforesaid scope in order to carry out the ion exchange treatment of EG solution suitably.Be judged as the occasion of improper processing, preferably carrying out ion exchange treatment once more.In the EG solution of (offer partial crystallization handle), the concentration of DEG ester will be equivalent to below the 8 weight % of total soluble matters after ion exchange treatment, more preferably 1～8 weight %, preferred especially 1～6 weight %.

(partial crystallization operation)

The EG solution that contains thick BHET in the 1st kind of method of the present invention, in its temperature (preferred 50～100 ℃, more preferably 70～90 ℃) more than saturation solubility its solute is dissolved fully, then, be cooled to 15～30 ℃, preferred 15～27 ℃ scope, the temperature of this scope insulation at least 1 hour, preferred 1～12 hour, more preferably 2～10 hours, preferred especially 3～8 hours, make that median size with precipitate is that 40～200 μ m (the SALD-200V ER that has been made by Shimadzu Seisakusho Ltd. after EG diluted 10 times measures) separate out BHET.

For example, preferably, be cooled to the preset temperature of 15～30 ℃ of scopes and keep the scheduled time in this temperature from the temperature more than the saturation solubility.After being cooled to preset temperature, so long as in the temperature of 15～30 ℃ of scopes, more or less heat up or lower the temperature all rightly, soaking time is to begin to calculate with the time point that reaches 30 ℃.

By insulation, can reduce the content of DEG composition in the precipitate.When this temperature was lower than 15 ℃, the amount of separating out of DEG ester increased, and on the other hand, when being higher than 30 ℃, the solubleness of BHET increases, and the receipts amount that partial crystallization is handled reduces, and is therefore not preferred.

This EG solution under the temperature refrigerative situation more than the saturation solubility, when using the cooling of intermittent type partial crystallization, slowly be cooled to preferably with for example 0.1～0.5 ℃/minute, preferred 0.1～0.3 ℃/minute speed of cooling.When with this speed of cooling, can prevent that the part of solution is cold excessively, and can reduce the DEG composition in the precipitate.On the other hand, during the continous way partial crystallization, preferably, be cooled to the temperature of 15～30 ℃ of scopes in advance, in containing the EG solution of precipitate, add the EG solution that contains the thick BHET more than the saturation solubility, mix and cooling.

In the 1st kind of method of the present invention, because the described EG solution cooling of having carried out ion exchange treatment and 15～30 ℃, the temperature insulation of preferred 15～27 ℃ scope, make and the crystalline growth of BHET carry out easily thereby solid-liquid separation becomes.Although the partial crystallization temperature is low more, solid component concentration in the filtrate is few more, the filter cake amount of partial crystallization increases more, but this EG solution contains the DEG ester, also contain the gas blocking agent composition according to circumstances, therefore with the partial crystallization decrease of temperature, thereby the problem that partial crystallization that partial crystallization along with BHET also carried out DEG ester and gas blocking agent composition descends the purity of the BHET in the filter cake will take place.

On the other hand, improve the partial crystallization temperature, with regard to produced BHET not the solubleness of partial crystallization, BHET increase and can not get the problem of target yield.Be necessary to be suitable for the temperature optimization of the characteristic of EG solution.

Handle by the partial crystallization in the 1st kind of method of the present invention, the BHET crystalline size of being separated out can satisfy effectively filters, and can do one's utmost to suppress the partial crystallization of DEG ester and gas blocking agent composition.For this reason, in the solid-liquid separation behind partial crystallization, DEG ester, free DEG and gas blocking agent composition mainly remain in the filtrate, and this just can be reduced in the DEG ester in the filter cake and the concentration of gas blocking agent composition.Also have, because the partial crystallization processing, just can be coloring material remaining in the starting raw material and the BHET that separates out Crystallization Separation.

(solid-liquid separation process)

In the 1st kind of method of the present invention, the solid-liquid separation after partial crystallization is handled is the temperature when remaining in the partial crystallization processing, and promptly the temperature of 15～30 ℃ of scopes is carried out.The preferred precipitate solid-liquid separation that adopts after filter type is handled partial crystallization.Furtherly, preferably use has Gas permeability 3～30cm ³/ mincm ²The pressure filter of filter cloth filter precipitate.The Gas permeability of filter cloth is lower than 3cm ³/ mincm ²The time, because of easy stifled order causes processing power to descend, and with the increase of liquid content in the filter cake, the impurity in the filter cake also increases; On the other hand, when Gas permeability greater than 30cm ³/ mincm ²The time, the order footpath of filter cloth is excessive, has particulate in the filtrate, and is therefore not preferred.Owing to passed through described filtration treatment, can obtain solid component concentration at 40～85 weight %, the filter cake of 50～80 weight % more preferably.

In the 1st kind of method of the present invention, the further distillation process of precipitate (for example filter cake) process by solid-liquid separation obtains just can provide the raw material that is used as making once again high-quality polyester.Discussion result according to inventor etc., the distillation efficiency of BHET and the quality of goods etc. are subjected to offering the influence of the impurity (for example DEG ester) that is contained in the raw material of distillation process, in the 1st kind of method of the present invention, impurity in the gained precipitate, particularly DEG ester and the few raw material of gas blocking agent composition are offered this distillation process, thereby, make to reach re-set target and become possibility.

The 2nd kind of method of the present invention is described below.

(starting raw material)

In the 2nd kind of method of the present invention, the EG solution that contains thick BHET as starting raw material, so long as in solvent EG the thick BHET solute of dissolved (solids component) be 5～85 weight % with respect to total solution weight, preferred 10～80 weight % EG solution just, not special restriction.So, this EG solution that contains thick BHET had both comprised the EG solution that uses in above-mentioned the 1st kind of method as starting raw material, also comprised this EG solution has been carried out the melting liquid that concentration and partial crystallization are handled the partial crystallization processing of above-mentioned the 1st kind of method (preferably with) resulting filter cake of after-filtration, promptly in EG, be dissolved with EG solution with respect to the thick BHET of 40～85 weight %, preferred 50～60 weight % of the gross weight of solution.What further specify is, during solution beyond starting raw material is concentration and filter cake, the ratio of thick BHET is preferably 5～40 weight %, and 10～40 weight % are for more preferably.In addition, when starting raw material was concentration thing or filter cake, the ratio of thick BHET was preferably 40～85 weight %, and 50～80 weight % are for more preferably.

Starting raw material in relevant the 2nd kind of method of the present invention contains in the explanation of EG solution of thick BHET, except the explanation of solids component (solute) concentration, all the other can former state be quoted in the 1st kind of method the content in the explanation of used EG solution of starting raw material and the 1st kind of resulting filter cake of method.

So the content that the starting raw material of the 1st kind of method partly illustrates is understood as that in the explanation of the starting raw material that is included in relevant the 2nd kind of method basically.

What further specify is that the EG solution of above-mentioned starting raw material contains thick BHET of solute and solvent EG.Although the thick BHET of solute is to be constituted separately most preferably by BHET, but, usually, except BHET, also contain MHET, 1, the solute more than a kind in 4-CHDM, phthalic acid two (2-hydroxyethyl) ester (hereinafter to be referred as BHEI), DEG ester, the oligopolymer (polymerization degree 2～20) etc.Again, this thick BHET serves as preferred not contain the gas blocking agent composition.

Consider from the viewpoint of the rate of recovery that improves BHET, in this thick BHET, the shared ratio of BHET preferably 70 weight % or more than, at 80 weight % or above for more preferably.Also having, in this thick BHET, at 8 weight % or following, be preferably at 1～8 weight % as the DEG ester content of impurity, and 1～6 weight % is for more preferably.When the described DEG ester that exists surpasses 8 weight %, distillation can not obtain when refining the achieving the goal BHET of quality, therefore not preferred.Equally, as the content of the oligopolymer of impurity preferably at 15 weight % or following, at 10 weight % or following for more preferably.When the described oligopolymer that exists in the starting raw material surpasses 15 weight %, distillation can not obtain when refining the achieving the goal BHET of quality, therefore not preferred.Also have, much less be that the total content of these impurity components and BHET is no more than 100 weight %.

Solvent to be to be to be constituted alone most preferably by EG, but, except EG, also contain usually in free DEG as impurity component, the water etc. more than a kind.In this solvent, the content of EG preferably 95 weight % or more than, more preferably 98 weight % or more than.As EG during less than 95 weight %, the impurity component outside the EG becomes the reason that causes side reaction easily, and is therefore not preferred.Also have, in described solvent, the content of free DEG is preferably at 3 weight % or following, at 2 weight % or following for more preferably.When the described free DEG that exists surpasses 3 weight %, become the DEG ester easily by side reaction, therefore not preferred.

(evaporization process)

Evaporization process in the 2nd kind of method of the present invention is made of the 1st phase evaporation operation and the 2nd phase evaporation operation.The 1st phase evaporation operation is the low boiling point component in the starting raw material (EG, water, free DEG etc.) is steamed and to be obtained the operation of the 1st melting liquid by the 1st evaporation unit.The 2nd phase evaporation operation is the low boiling point component in the 1st melting liquid (EG, free DEG etc.) is steamed and to be obtained the operation of the 2nd melting liquid by the 2nd evaporation unit.Here, low boiling point component is meant the low-boiling composition (compound) of its boiling point than BHET, for example water, EG, free DEG etc.Therefore, offer the EG solution of the 1st phase evaporation operation, the ratio of its thick BHET is when 5～40 weight %, in temperature (for example being higher than 50 ℃ temperature) that solute is not separated out and be no more than under 100 ℃ the temperature, heat under preferred 70～90 ℃ temperature; And the ratio of thick BHET is difficult to cause below 120 ℃ of temperature of side reaction, preferred 70～120 ℃, preferred especially 80～120 ℃ of heating down as melting at thick BHET when 40～85 weight %.

These the 1st and the 2nd evaporation units preferably, have the evaporation unit (that is falling film type evaporation device) of the heating arrangements that when making starting raw material or melting liquid with membranaceous flowing down low boiling point component (EG, free DEG etc.) is steamed.With this device the have solution high temperature of short period of time (be thermal history (Hot carries out Artworks) short) advantage that just can steam low boiling point component only.Like this, just can suppress by the secondary life of EG is DEG.Also have, these evaporation units have the vacuum mechanism that can carry out vacuum-evaporation.

(the 1st phase evaporation operation)

The 1st phase evaporation operation in the 2nd kind of method of the present invention is carried out under 130～170 ℃ of temperature, preferred 140～160 ℃, pressure 300～1000Pa, preferred 300～700Pa.Described temperature is meant the temperature of hot face, and pressure is near the pressure the hot face.Handle if carry out the 1st phase evaporation under less than 130 ℃ temperature condition, low boiling point component (EG, free DEG etc.) is steamed required chronic of preferred concentration, caused BHET hang down dimerization, thus not preferred.Handle and under temperature surpasses 170 ℃ condition, carry out the 1st phase evaporation because the pyritous thermal history makes secondary the giving birth to of EG be DEG, and then by DEG with the BHET reaction the secondary DEG ester that generates, so not preferred.Handle when carry out the 1st phase evaporation under the condition of the discontented 300Pa of pressure, when steaming low boiling point component (EG, free DEG etc.), solute (for example BHET) also splashes, and is therefore not preferred.Handle and carry out the 1st phase evaporation under pressure surpasses the condition of 1000Pa, it is long that low boiling point component (EG, free DEG etc.) is steamed the required time of preferred concentration, caused BHET to hang down dimerization, so not preferred.Even the side in temperature, the pressure does not satisfy condition, also just become not preferred state.

In the 1st phase evaporation operation, solvent (EG, water, DEG etc.) is steamed the EG that makes in resulting the 1st melting liquid and the total content of free DEG is 3～10 weight %, be preferably 3～6 weight %.Treatment time (time that solution contacts with heating arrangements) is preferably 1 second～and 2 minutes, be divided into more preferably with 1 second～1.

Distilled solvent in managing is herein cooled off with condenser, obtain phlegma.This phlegma can directly offer distillation refinement treatment (processing of re-refining) as the solvent use once more, but, among the present invention with its as pay this handle before the required cold medium of the condenser of molecular distillation apparatus inside at least a portion and use, reduced energy expenditure, therefore preferred.The temperature of phlegma is preferably 20～80 ℃, with 30～50 ℃ for more preferably.

(the 2nd phase evaporation operation)

The 2nd phase evaporation operation in the 2nd kind of method of the present invention in the 1st evaporation unit not in most, the 1st melting liquid of evaporation process remaining low boiling point component (EG, free DEG etc.) steam.The 2nd phase evaporation operation is to carry out under 130～170 ℃ of temperature, preferred 140～160 ℃, pressure 50～250Pa, preferred 50～150Pa.Described temperature is meant the temperature of hot face, and pressure also is near the pressure the hot face.If carry out the processing of the 2nd phase evaporation under less than 130 ℃ temperature condition, it is long that low boiling point component (EG, free DEG etc.) is evaporated to the required time of preferred concentration, causes BHET to hang down dimerization, therefore not preferred.And handling above carrying out the 2nd phase evaporation under 170 ℃ the condition, because the pyritous thermal history, making EG derive is free DEG, and then this free DEG and BHET reaction and generation DEG ester, therefore not preferred.Handle when carry out the 2nd phase evaporation under the condition of the discontented 50Pa of pressure, in the evaporation of low boiling point component (EG, free DEG etc.), solute (for example BHET) has also splashed, and is therefore not preferred.And handle above carrying out the 2nd phase evaporation under the condition of 250Pa at pressure, it is long that low boiling point component (EG, free DEG etc.) is evaporated to the required time of preferred concentration, causes BHET to hang down dimerization, therefore not preferred.Even the side in temperature, the pressure condition does not satisfy, just become not preferred state.

In the 2nd evaporation unit, low boiling point component to be evaporated, the total amount that makes the EG that contains in resulting the 2nd melting liquid and free DEG is at 0.45 weight % or following, preferably at 0.40 weight % or following.When EG remaining in the 2nd melting liquid and free DEG surpass 0.45 weight %, in the molecular distillation operation, just become the pair that causes DEG easily and give birth to and cause the side reaction of the described secondary DEG of generation ester to take place thus.The treatment time of this operation (time that solution contacts with heating arrangements) is preferably 1 second～and 2 minutes, be divided into more preferably with 1 second～1.

In the evaporization process in evaporation and the 1st and the 2nd phlegma that cools down the aggregate value of the free DEG content in free DEG content and the 2nd melting liquid that obtains by evaporization process be preferably 2 weight % or following with respect to the total amount of this phlegma and the 2nd melting liquid.Among the present invention, suppressed the generation of free DEG with evaporization process, just can suppress free DEG is the generation of the DEG ester of reason.So, can reduce the content made from extra care DEG ester among the BHET.

And then preferably at 15 weight % or following, promptly the evaporization process among the present invention has suppressed the generation of oligopolymer to the oligomer in the 2nd melting liquid.Consequently can improve the rate of recovery of refining BHET.

It is feature that evaporization process in the 2nd kind of method of the present invention carries out evaporation operation with the two-stage, and only a stage evaporation operation has the following shortcoming of enumerating.That is, only a stage will make solvent strength in the thick BHET melting liquid at 0.45 weight % or following, and solution just must be in the too harsh evaporation conditions (for example surpassing 170 ℃ temperature), compares with the present invention, and the amount of the secondary DEG that gives birth to and the amount of oligopolymer increase.Also have,,, lack the industrial production of BHET from cost because the scale of evaporation unit becomes excessive.

(molecular distillation operation)

Molecular distillation operation in the 2nd kind of method of the present invention is the operation of resulting the 2nd melting liquid of the evaporization process of front being carried out molecular distillation.Molecular distillation apparatus is to have to make that described melting liquid is membranaceous to be flowed down the heating arrangements of part evaporation on one side and make the falling film type molecular distillation apparatus of the solute (cut) of evaporation (vaporization) with the internal condensation device of the stroke condensation of weak point with this heating arrangements on one side.

This molecular distillation apparatus preferably uses the phlegma of the solvent of this evaporization process evaporation as at least a portion of the cold medium in the described internal condensation device.As previously mentioned, this phlegma is cooled to preferred 20～80 ℃, more preferably 30～50 ℃ temperature.Thus, be mixed with the temperature that just can reduce cold medium behind this phlegma.The BHET condensing temperature of internal condensation device serves as preferred with 115～125 ℃.Also have, the BHET that evaporates with above-mentioned heating arrangements is condensation with very short stroke, with below the mean free path of the BHET that the interval of the cooling surface of the hot face of this heating arrangements and internal condensation device remained on evaporation for well.

In the 2nd kind of method of the present invention, the distillation of carrying out with molecular distillation apparatus is 180～220 ℃ of temperature, preferred 185～205 ℃, pressure 25Pa or following, preferred 15Pa or following carrying out.Described temperature is meant the temperature of hot face.Pressure also is near the pressure the hot face.Handle if carry out molecular distillation under less than 180 ℃ temperature condition, do not evaporate as the BHET of target, therefore not preferred.And carry out molecular distillation under 220 ℃ the condition and handle surpassing, because the pyritous thermal history, make that pair bears the DEG ester with the BHET reaction for the free DEG of trace, thus not preferred.Carry out the molecular distillation processing under the condition of 25Pa when surpassing at pressure, even evaporated as the BHET of target, but this BHET just goes to the residual thing effluent of still kettle before by the condensation of internal condensation device, and is therefore not preferred.Even the side in temperature, the pressure condition does not satisfy, just become not preferred state.The time of this processing (time that thick BHET contacts with heating arrangements) is 1 second～1 minute, serves as preferred with 1 second～50 seconds.

In the molecular distillation apparatus, supply with BHET contained in the 2nd melting liquid of this water distilling apparatus and do not evaporated fully, the weight ratio of cut and the residual thing of still kettle is preferably 9: 1～5: 5, with 8: 2～6: 4 for more preferably.When the BHET that this ratio contains in the 2nd melting liquid for example is 80～90 weight %, the weight ratio of cut and evaporating kettle residue with for example 7: 3 for well.After having done like this, just can make with secondary DEG ester of giving birth to like the property class of BHET and remain in the residual thing side of still kettle with BHET, the content that has obtained the DEG ester in the cut at 1.5 weight % or following, oligomer at 1 weight % or the following higher cut of quality.Therefore, in the occasion low slightly, can further improve yield by the evaporation ratio that improves cut to the product requirements characteristic.

Because the residual thing of still kettle that takes place in the molecular distillation operation is main component with BHET, it can be used as the raw material of aforesaid polyester depolymerization and drops into and carry out initial depolymerization.

As previously mentioned, aforementioned molecular distillation operation preferably in the cold medium of its internal condensation device at least a portion be to use the phlegma that obtains by evaporization process, illustrating in greater detail this processing then is, for this phlegma being used as solvent once more and it being distilled refinement treatment (processing of re-refining), before carrying out this processing, the cold medium of this phlegma as the internal condensation device used, vaporization heat by the steam of BHET heats this phlegma, its temperature had uprised when from then on the internal condensation device came out, the raising of this temperature just is equivalent to part has omitted in the thermal pretreatment of this phlegma being gone distill when refining, has played the effect that cuts down the consumption of energy.Also have, can reduce again the amount of the cold medium of preparing, using as the internal condensation device with cold medium.

(distillation process figure)

The process for purification of terephthalic acid two (2-hydroxyethyl) ester in the 2nd method of the present invention is described with figure now.Fig. 1 shows the schema of preferred distillation process (evaporation-water distilling apparatus combination state).Among Fig. 1,1 is first evaporation unit, the 2nd, and condenser, the 3rd, the melting liquid transferpump, 4 is second evaporation units, the 5th, condenser, the 6th, melting liquid transferpump, the 7th, phlegma receiver, the 8th, molecular distillation apparatus, the 9th, the internal condensation device, the 10th, heating arrangements, the 11st, goods outlet, the 12nd, the residual thing outlet of still kettle, the 13rd, cold medium circulation jar, the 14th, thermal

medium jar.Condenser

2 and 5 the mode of choosing any one kind of them in type and the device outer setting type that can using appts inside be provided with is set.Also have, the 1st evaporation unit, the 2nd evaporation unit and molecular distillation apparatus are connected with (not illustrating among the figure) vacuum mechanism separately, become vacuum state in the device thereby can make.

Among Fig. 1, the 1st evaporation unit 1 and the 2nd evaporation unit 4 are falling film type evaporation devices, starting raw material (EG solution) is offered the 1st evaporation unit 1, the low boiling point component that heating steams in this device (EG, water, free DEG etc.) is condensing and become the 1st phlegma in condenser 2 coolings, is received in the phlegma receiver 7.The 1st melting liquid is delivered to the 2nd evaporation unit 4 by melting liquid transferpump 3, and the low boiling point component that heating steams in this device (EG, free DEG etc.) condenses into the 2nd phlegma in condenser 5 coolings, gets back to the distillation refining system.

Melting liquid transferpump 6 offers molecular distillation apparatus 8 to the 2nd melting liquid, and by at the heating arrangements 10 of this device in 8 cut being evaporated, the cut that is evaporated is cooled off by internal condensation device 9.Take out from goods outlet 11 as goods by internal condensation device 9 refrigerative cuts.Raffinate beyond the cut takes out from the residual thing outlet 12 of still kettle.

The phlegma of in phlegma receiver 7, accepting that comes from evaporization process, its preferred scheme is, after the cold medium that comes from cold medium circulation jar 13 mixes, the cooling that offers internal condensation device 9 is used, from then on condenser 9 (temperature improve) the cold medium of discharging is got back to after the cold medium circulation jar 13, with the corresponding amount of the amount of blended phlegma and separate.Here, it is good that isolating liquid is got back to distillation refinement treatment (reclaiming refining) system, and the heating arrangements 10 that perhaps is transported to molecular distillation apparatus 8 provides the thermal medium jar 14 of thermal medium good.With thermal medium jar 14 thermal medium is heated to desired temperature.Also have, the high-temp liquid that produces in distillation refinement treatment (reclaiming refining) system can offer thermal medium storage tank 14 and use as thermal medium.After having done like this, just can reduce multi-stage evaporation, use the energy consumption in the distillating method of water distilling apparatus.

The 3rd kind of method of the present invention is described below.

The 3rd kind of method of the present invention is the combination of above-mentioned the 1st kind of method and the 2nd kind of method.So, in the explanation of the 3rd kind of method here, be identical basically with the explanation of the 1st kind of method and the 2nd kind of method.Below, consider the place of repeat specification, so the 3rd kind of method done simple declaration.

(starting raw material)

The starting raw material of the 3rd kind of method of the present invention is the EG solution that contains thick BHET, and it is the same with the starting raw material of the 1st kind of method of the present invention.So, this EG solution preferably, by being terephthalic acid that polyester is separated coalescence and implemented impurity remove the solution of processing or the solution that is obtained by the transesterification reaction of terephthalic acid and EG (serves as preferred to have carried out breaking away from the solution that son handles) after this process or depolymerization with EG.The modulator approach of these solution can be carried out with reference to the method described in the 1st kind of method of the present invention.The EG solution that contains thick BHET that method is thus obtained offers the partial crystallization operation.

(partial crystallization operation)

The EG solution that contains thick BHET in the 3rd kind of method of the present invention is offered the partial crystallization operation according to the method that illustrates in the 1st kind of method of the present invention.That is, this EG solution is warmed up to temperature more than the saturation solubility, solute is dissolved fully, be cooled to 15～30 ℃ temperature range then, and kept at least 1 hour, just can reach its intended purposes in the temperature of this scope.

(solid-liquid separation process)

Come the precipitate after the partial crystallization processing in the 3rd kind of method of the present invention is separated with the solid-liquid separation process that illustrates in relevant the 1st kind of method of the present invention, can obtain with BHET is the filter cake of main component.That is,,, just can obtain the target filter cake Yi Bian make its solid-liquid separation on one side what partial crystallization was separated out is that the precipitate of main component remains on partial crystallization temperature (15～30 ℃) with BHET.In order to offer the operation of back, this filter cake is taked the form of melting liquid, preferably this filter cake be difficult to melting cause side reaction temperature (for example 120 ℃ or following so 70～120 ℃, particularly 80～120 ℃) down heating.

(evaporization process)

Evaporization process in the 3rd kind of method of the present invention, the raw material of use is aforementioned filter cake, it is implemented described in the 2nd kind of method of the present invention like that.Promptly, just can meet the requirements of purpose according to following evaporization process: the melting liquid of described filter cake is imported the 1st evaporation unit, under 130～170 ℃ of temperature, pressure 300～1000Pa condition, steam low boiling point component, obtain the 1st melting liquid that EG and free DEG add up to content 3～10 weight %, this the 1st melting liquid is imported the 2nd evaporation unit, under 130～170 ℃ of temperature, pressure 50～250Pa condition, steam low boiling point component, obtain EG and free DEG and add up to content 0.45 weight % or the 2nd following melting liquid.

(molecular distillation operation)

Distillation process in the 3rd kind of method of the present invention is that the 2nd melting liquid that is obtained by above-mentioned evaporization process is implemented according to the method that illustrates in the 2nd kind of method of the present invention.That is, described the 2nd melting liquid is imported the falling film type molecular distillation apparatus, under 180～220 ℃ of temperature, pressure 25Pa or following condition, distill, just can meet the requirements of purpose.

So,, make crude terephthalic acid two (2-hydroxyethyl) ester refining, can obtain high-quality terephthalic acid two (2-hydroxyethyl) ester with good efficiency by aforesaid operations according to the present invention.Also have, purified terephthalic two of the present invention (2-hydroxyethyl) ester can be made polyethylene terephthalate by the polymerization in the presence of polymerizing catalyst.

Embodiment

Further specify the present invention with embodiment below.But, it is described to be not that the present invention only is limited to embodiment.Also have, the characteristic in the example is measured by following described method.

1. the mensuration of the separation of each composition, amount

In chloroform, modulation is into about 1 the 5mg sample dissolution, and the solution of 000ppm is measured with the LC-6 type Liquid Chromatograph (HPLC) that Shimadzu Seisakusho Ltd. makes, and condition determination is: 4.6mm ^ID* 250mm ^LSilicon-dioxide 60 posts, 40 ℃ of temperature, flow velocity 1.0mL/ branch, injection rate 5 μ L, moving phase are methylene dichloride/diox, measure wavelength 240nm, the analyzer of ultraviolet extinction photometer.

2. the evaluation of solution composition

In order to point out the peak of HPLC, carry out LC/MS and measure.Use the SX-102A type device of NEC manufacturing under above-mentioned similarity condition, to measure and point out.

3. the optical density (OD) of sample

The 5mg sample dissolution in methyl alcohol, is modulated into the methanol solution of 10 weight %, measures the absorbancy of this solution at 380nm with ultraviolet spectrophotometer (mini-1240, (strain) Shimadzu Seisakusho Ltd. make), 10mm pond, with methyl alcohol as blank to carry out zero correction.

4. specific conductivity

The 873CC type electric conductivity meter made from Foxboro Co. carries out METHOD FOR CONTINUOUS DETERMINATION.

5. water ratio

Measure with MK-SS type Ka Er-Fischer moisture meter that capital of a country electronic industry (strain) is made.

6.pH

According to solid component concentration under 80 ℃ of temperature of " JISZ8802 " mensuration is the pH value of the ethylene glycol solution of 20 weight %.

7. the median size of precipitate

Diluted 10 times partial crystallization liquid with the SALD-200V ER mensuration that (strain) Shimadzu Seisakusho Ltd. makes with EG.

Embodiment 1

(modulation of starting raw material)

(pre-depolymerization)

Be ground into the square fragment of mean sizes 8mm mixing used PET bottle that the painted PET bottle of 10 weight % is arranged (bottle that constitutes by polyethylene terephthalate), get its 57kg and terephthalic acid two (2-hydroxyethyl) ester (BHET) and pack in the autoclave that has stirrer of 800L, under normal pressure, 250 ℃ of conditions, carry out pre-depolymerization with the mixture 25kg of its oligopolymer.

(depolymerization)

Then, in this pre-depolymerizing substance, add ethylene glycol (EG) 418kg and depolymerization catalyzer sodium hydroxide 0.23kg respectively, under pressure 0.15MPa, 220 ℃ of conditions of temperature, carry out depolymerization reaction, obtain depolymerization reaction solution 500kg.

(removing of solid foreign materials)

This solution is cooled to 180 ℃, undecomposed solid foreign materials (bottle cap, label etc.) in depolymerization reaction is removed, be transported in the 800L cooling tank with 60 purpose line filter screens.

(decolouring is handled)

In cooling tank, the temperature of this reaction soln is cooled to 80 ℃, after the solid foreign materials such as the pigment remove particle diameter 1 μ m with core strainer more than, particulate, this reaction soln with space velocity 0.57 hour ^-1By having filled the bleaching tower of gac (" Di Yahaopu (ダイアホ-プ) 008 " 105kg that Mitsubishi Chemical's (strain) makes), the processing of decolouring.

(cationic exchange processing)

Next, under 80 ℃ of temperature with space velocity 4.8 hours ^-1Carrying out cationic exchange in the decationized Y sieve tower of having filled cation exchange column (Zeo-karb " An Balaite IR-120B " 25L that ロ-system ア Application De バ-ス company makes) handles.

(anionresin processing)

Thereafter, in the 30s by connecting piece, under 80 ℃ of temperature with space velocity 2 hours ^-1Carrying out anionresin in the exhaustion of yin ion tower of having filled anion ion exchange body (Zeo-karb " An Balaite IRA96SB " 30L that ロ-system ア Application De バ-ス company makes and the mixture of Zeo-karb " An Balaite IR-120B " 30L) handles.

The pH of this reaction soln was 5.2 before cationic exchange is handled, and cationic exchange is 1.8 after handling, and anionresin is 4.9 after handling.The specific conductivity of this reaction soln was 537 μ s/cm before cationic exchange is handled, and anionresin is 0.4 μ s/cm after handling.The concentration of the solids component (solute) of the reaction solution after anionresin is handled is 19.5 weight %.In the solids component (solute) of reaction soln, contain terephthalic acid 2-hydroxyethyl [2-(2-hydroxyl-oxethyl) ethyl] ester (DEG ester) of 4.0 weight %.

(partial crystallization operation)

The solution that above-mentioned disengaging is handled is cooled to 25 ℃ with the speed of 0.2 ℃/min from 80 ℃ in the partial crystallization groove, kept 5 hours at 25 ℃, makes its partial crystallization.The median size of precipitate is 60 μ m.

(solid-liquid separation process)

Thereafter, being maintained under 25 ℃ of conditions, with Gas permeability 5cm is housed ³/ mincm ²The pressure filter of filter cloth carry out solid-liquid separation, obtained containing the filter cake 145kg (taking rate 29 weight %) of thick BHET of 60 weight % and the filtrate 355kg (taking rate 71 weight %) of solid component concentration 3.5 weight %.The DEG ester that contains 1.8 weight % in this filter cake.

Embodiment 2

(modulation of starting raw material)

Method is similarly to Example 1 carried out.

(partial crystallization operation)

Except the partial crystallization temperature is 15 ℃, method is similarly to Example 1 carried out.The median size of precipitate is 61 μ m.

(solid-liquid separation process)

Method is similarly to Example 1 carried out and is obtained filter cake.

The result is, obtains containing the filter cake 150kg (taking rate 30 weight %) of thick BHET of 61 weight % and the filtrate 350kg (taking rate 70 weight %) of solid component concentration 2.5 weight %.The DEG ester that contains 2.3 weight % in this filter cake.

By these facts as can be known, usually, can improve partial crystallization efficient, in the present invention, confirm that solid component concentration and the solid component concentration in the filter cake in the filtrate has this trend but reduce the partial crystallization temperature phase.Meanwhile, be that decline with the solubleness in EG increases as the content of the DEG ester that contains thing beyond the BHET in the filter cake.Thus the result as can be known, in order to obtain more highly purified BHET, to be taken as the partial crystallization temperature be good obtaining BHET crystalline top temperature.

Comparative example 1

(modulation of starting raw material)

Method is similarly to Example 1 carried out.

(partial crystallization operation)

Except the partial crystallization temperature is 5 ℃, method is similarly to Example 1 carried out.The median size of precipitate is 62 μ m.

(solid-liquid separation process)

Method is similarly to Example 1 carried out and is obtained filter cake.

The result is, obtains containing the filter cake 155kg (taking rate 31 weight %) of thick BHET of 62 weight % and the filtrate 345kg (taking rate 71 weight %) of solid component concentration 1.7 weight %.See that from the aspect of amount the effect that temperature is descended shows clearly, contains the DEG ester of 3.0 weight % in this filter cake.

Comparative example 2

(modulation of starting raw material)

Method is similarly to Example 1 carried out.

(partial crystallization operation)

Except the partial crystallization temperature is 35 ℃, operation is similarly to Example 1 carried out, and can not obtain sufficient partial crystallization result, and the solid component concentration in the filtrate reaches 7 weight %, can not enter subsequent processing.

Table 1 has been concluded the yield of solids component of the partial crystallization operation in embodiment 1,2 and the comparative example 1 and the content of DEG ester.

Table 1

	Partial crystallization liquid characteristic	The partial crystallization condition	The filter cake characteristic			The filtrate characteristic		Add up to solids component ratio weight %
	Partial crystallization liquid characteristic	The partial crystallization condition	The filter cake characteristic			The filtrate characteristic			DEG composition containing ratio weight %	Temperature ℃	Taking rate weight %	Solids component containing ratio weight %	DEG composition containing ratio weight %	Taking rate weight %	Solids component containing ratio weight %
	Embodiment 1	4.0	25	29	60	1.8	71		DEG composition containing ratio weight %	Temperature ℃	Taking rate weight %	Solids component containing ratio weight %	DEG composition containing ratio weight %	Taking rate weight %	Solids component containing ratio weight %	3.5	19.9
Embodiment 2	Embodiment 1	4.0	25	29	60	1.8	71	4.0	15	30	61	2.3	70	2.5	20.1	3.5	19.9
Embodiment 2	Embodiment 3	4.0	05	31	62	3.0	69	4.0	15	30	61	2.3	70	2.5	20.1	1.7	20.0

Embodiment 3

(modulation of starting raw material)

Method is similarly to Example 1 carried out.The sub-treatment soln of resulting disengaging is made with extra care with distillation process shown in Figure 1 and is used as raw material.

(the 1st phase evaporation operation)

With the feed rate of 138kg/h falling film type evaporation unit feeding starting raw material, under 150 ℃ of temperature, pressure 500Pa condition, steam low boiling point component to the 1st stage.The evaporation process time is 3.6 hours, and the amount of being cooled off the 1st phlegma that generates by low boiling point component is 109kg/h, and the growing amount of the 1st melting liquid is 29kg/h.

Table 2 shows EG in the 1st melting liquid and the total amount of free DEG, the content of oligopolymer.

(the 2nd phase evaporation operation)

Then, the 1st melting liquid is supplied with the falling film type evaporation device in the 2nd stage, under 150 ℃ of temperature, pressure 80Pa condition, steam remaining low boiling point component with the feed rate of 29kg/h.The evaporation process time is 3.7h, and the amount of being cooled off the 2nd phlegma that generates by low boiling point component is 2kg/h, and the growing amount of the 2nd melting liquid is 27kg/h.

Table 2 shows free DEG content, the EG in the 2nd melting liquid and the total content of free DEG in the 1st, the 2nd phlegma and the 2nd melting liquid, the content of oligopolymer.

(molecular distillation operation)

Feed rate with 27kg/h offers the falling film type molecular distillation apparatus to the 2nd melting liquid, is like that to distillate cut at 7: 3 in order to make weight ratio with cut and the residual thing of still kettle, carries out molecular distillation under 195 ℃ of temperature, pressure 13Pa condition.Distillate cut with 19kg/h, distillation takes 3.7h.In the molecular distillation, resulting the 1st whole phlegma has used as the part of the cold medium of internal condensation device in the 1st phase evaporation operation.Table 3 shows the analytical results of resulting cut.

Embodiment 4

(modulation of starting raw material)

Method is similarly to Example 1 carried out.

(partial crystallization operation)

Method is similarly to Example 1 carried out.Resulting filter cake is melted in 100 ℃ of heating under nitrogen atmosphere, as the refining starting raw material in the distillation process shown in Figure 1.

(the 1st phase evaporation operation)

To the 1st stage falling film type evaporation unit feeding starting raw material, under 150 ℃ of temperature, pressure 500Pa condition, steam low boiling point component with the feed rate of 50kg/h.The evaporation process time is 2.9h, and the amount of being cooled off the 1st phlegma that generates by low boiling point component is 18kg/h, and the growing amount of the 1st melting liquid is 32kg/h.

(the 2nd phase evaporation operation)

Then, the 1st melting liquid is offered the falling film type evaporation device in the 2nd stage, under 150 ℃ of temperature, pressure 80Pa condition, steam remaining low boiling point component with the feed rate of 32kg/h.The evaporation process time is 2.9h, and the amount of being cooled off the 2nd phlegma that generates by low boiling point component is 2kg/h, and the growing amount of the 2nd melting liquid is 30kg/h.

(molecular distillation operation)

Feed rate with 30kg/h offers the falling film type molecular distillation apparatus to the 2nd melting liquid, is like that to distillate cut at 7: 3 in order to make weight ratio with cut and the residual thing of still kettle, carries out molecular distillation under 195 ℃ of temperature, pressure 13Pa condition.Distillate cut with 21kg/h, distillation takes 2.9h.Table 3 shows the analytical results of resulting cut.

Comparative example 3

(modulation of starting raw material)

Method is similarly to Example 1 carried out.

(evaporization process)

By as getting off to carry out the 1st phase evaporation operation, do not carry out the 2nd phase evaporation operation.That is, supply with starting raw material to evaporation unit, under 150 ℃ of temperature, pressure 500Pa condition, steam low boiling point component with the feed rate of 25kg/h.The evaporation process time is 20h, and the amount of being cooled off the phlegma that generates by low boiling point component is 20kg/h, and the growing amount of melting liquid is 5kg/h.

Table 2 shows free DEG content, the EG in the 1st melting liquid and the total amount of free DEG in the 1st phlegma and the 1st melting liquid, the content of oligopolymer.

(molecular distillation operation)

Feed rate with 5kg/h is supplied with the falling film type molecular distillation apparatus to the 1st melting liquid that is obtained by aforesaid operations, in order to make weight ratio with cut and the residual thing of still kettle is like that to distillate cut at 7: 3, carries out molecular distillation under 190 ℃ of temperature, pressure 13Pa condition.Distillate cut with 3.5kg/h, distillation takes 20.1h.Table 3 shows the analytical results of resulting cut.

As shown in Table 3, owing to only carry out evaporation process in the 1st phase evaporation device, carry out long solvent evaporation under the many conditions of the amount of low boiling point component EG, the content of the DEG in the cut becomes 1.9 weight %.

Comparative example 4

(modulation of starting raw material)

Method is similarly to Example 1 carried out.

(evaporization process)

Till the 1st phase evaporation operation, method is similarly to Example 1 carried out, and does not carry out the 2nd phase evaporation operation.

(molecular distillation operation)

Feed rate with 29kg/h offers the falling film type molecular distillation apparatus to the 1st melting liquid that is obtained by aforesaid operations, in order to make weight ratio with cut and the residual thing of still kettle is like that to distillate cut at 7: 3, carries out molecular distillation under 197 ℃ of temperature, pressure 13Pa condition.Distillate cut with 20.3kg/h, distillation takes 3.6 hours.Table 3 shows the analytical results of resulting cut.

Comparative example 4 is to carry out molecular distillation to handle under the state of remaining low boiling point component 5.1 weight %, in evaporating solvent, solutes such as BHET also splash thereupon, on the condenser inner-wall surface of solute before attached to vacuum mechanism, are difficult to carry out stable molecular distillation operation.

Table 2

The phlegma of evaporization process, the analytical results of melting liquid

	Embodiment

3	Embodiment 4	Comparative example 3	Comparative example 4
3	Embodiment 4	Comparative example 3	Comparative example 4	Free DEG content (weight %) in phlegma in evaporization process and the melting liquid ¹⁾	1.4	1.2	3.1	1.4
EG in the 1st melting liquid and the content of free DEG (weight %)	5.1	5.1	0.4		1.4	1.2	3.1	1.4	5.1
	5.1	5.1	0.4	The content of the oligopolymer in the 1st melting liquid (weight %)	11.1	11.1	20.4	11.1	5.1
EG in the 2nd melting liquid and the content of free DEG (weight %)	0.3	0.3	-		11.1	11.1	20.4	11.1	-
	0.3	0.3	-	The content of the oligopolymer in the 2nd melting liquid (weight %)	12.0	12.0	-	-	-

1) is free DEG content in the 1st, the 2nd phlegma and the 2nd melting liquid in embodiment 3

In comparative example 3,4 the free DEG content in the 1st phlegma and the 1st melting liquid

DEG: Diethylene Glycol

EG: ethylene glycol

Table 3

The analytical results of the cut of molecular distillation

The quality of refining BHET behind the molecular distillation	Embodiment	3	Embodiment 4	Comparative example 3	Comparative example 4
	Embodiment	3	Embodiment 4	Comparative example 3	Comparative example 4	The receipts amount (kg) of refining BHET	70	61	70	61
Optical density (OD) (380nm)	0.002	0.000	0.005	0.007		The receipts amount (kg) of refining BHET	70	61	70	61
Optical density (OD) (380nm)	0.002	0.000	0.005	0.007	BHET content (weight %)	99.0	99.2	96.8	97.0
DEG ester content (weight %)	0.7	0.5	1.9	2.5	BHET content (weight %)	99.0	99.2	96.8	97.0
DEG ester content (weight %)	0.7	0.5	1.9	2.5	Oligomer (weight %)	0.2	0.2	1.2	0.3
Other (weight %)	0.1	0.1	0.1	0.2	Oligomer (weight %)	0.2	0.2	1.2	0.3

BHET: terephthalic acid two (2-hydroxyethyl) ester

DEG ester: terephthalic acid 2-hydroxyethyl [2-(2-hydroxyl-oxethyl) ethyl] ester

MHET: terephthalic acid list (2-hydroxyethyl) ester

Comparative example 5～12

(modulation of starting raw material)

Method is similarly to Example 1 carried out.

(the 1st phase evaporation operation)

To the falling film type evaporation unit feeding starting raw material in the 1st stage, making EG in the 1st melting liquid and the total content of free DEG with the evaporation conditions of table 4 is 5 weight %.

Table 4

Comparative example	5	6	7	8	9	10	11	12
Comparative example	5	6	7	8	9	10	11	12	Temperature (℃)	120	120	120	180	180	180	150	150
Pressure (Pa)	200	500	2000	200	500	2000	200	2000	Temperature (℃)	120	120	120	180	180	180	150	150
Pressure (Pa)	200	500	2000	200	500	2000	200	2000	Evaporation time (h)	4.0	4.6	5.5	2.8	3.2	3.9	3.2	4.3

Table 5 shows EG in the 1st melting liquid and the total amount of free DEG, the content of oligopolymer.

(the 2nd phase evaporation operation)

Carry out with method similarly to Example 3.Table 5 shows free DEG content, the EG in the 2nd melting liquid and the total content of free DEG in the 1st, the 2nd phlegma and the 2nd melting liquid, the content of oligopolymer.

(molecular distillation operation)

The 2nd melting liquid that is obtained by aforesaid operations is offered the falling film type molecular distillation apparatus, and making weight ratio with cut and the residual thing of still kettle is like that to distillate cut at 7: 3.Table 6 shows the analytical results of resulting cut.

In comparative example 5～12,, can know that under any circumstance, quality and the receipts amount of refining BHET all have been subjected to influence although under various evaporation conditionses, carry out the 1st phase evaporation operation.

Table 5

The phlegma of evaporization process, the analytical results of melting liquid

	Comparative example 5	Comparative example 6	Comparative example 7	Comparative example 8	Comparative example 9	Comparative example 10	Comparative example 11	Comparative example 12
	Comparative example 5	Comparative example 6	Comparative example 7	Comparative example 8	Comparative example 9	Comparative example 10	Comparative example 11	Comparative example 12	1st, the free DEG content (weight %) in the 2nd phlegma and the 2nd melting liquid	2.1	2.2	2.3	1.9	2.3	5.0	1.4	2.9
EG in the 1st melting liquid and free DEG content (weight %)	5.0	5.0	5.0	5.0	5.0	5.0	5.0	5.0		2.1	2.2	2.3	1.9	2.3	5.0	1.4	2.9
	5.0	5.0	5.0	5.0	5.0	5.0	5.0	5.0	Oligomer in the 1st melting liquid (weight %)	14.2	15.0	16.3	10.1	10.7	12.2	10.8	15.1
EG in the 2nd melting liquid and free DEG content (weight %)	0.3	0.3	0.3	0.3	0.3	0.3	0.3	0.3	Oligomer in the 1st melting liquid (weight %)	14.2	15.0	16.3	10.1	10.7	12.2	10.8	15.1
	0.3	0.3	0.3	0.3	0.3	0.3	0.3	0.3	Oligomer in the 2nd melting liquid (weight %)	15.1	15.9	17.2	11.0	11.6	13.1	11.7	16.0

Table 6

The analytical results of the cut of molecular distillation

The quality of refining BHET behind the molecular distillation	Comparative example 5	Comparative example 6	Comparative example 7	Comparative example 8	Comparative example 9	Comparative example 10	Comparative example 11	Comparative example 12
	Comparative example 5	Comparative example 6	Comparative example 7	Comparative example 8	Comparative example 9	Comparative example 10	Comparative example 11	Comparative example 12	The receipts amount (kg) of refining BHET	68	70	70	50	66	70	63	70
Optical density (OD) (380nm)	0.005	0.005	0.006	0.004	0.006	0.008	0.003	0.007	The receipts amount (kg) of refining BHET	68	70	70	50	66	70	63	70
Optical density (OD) (380nm)	0.005	0.005	0.006	0.004	0.006	0.008	0.003	0.007	BHET content (weight %)	97.0	96.9	96.6	98.1	97.3	96.6	98.7	96.2
DEG ester content (weight %)	1.8	1.8	1.9	1.1	1.9	2.8	0.7	2.5	BHET content (weight %)	97.0	96.9	96.6	98.1	97.3	96.6	98.7	96.2
DEG ester content (weight %)	1.8	1.8	1.9	1.1	1.9	2.8	0.7	2.5	Oligomer (weight %)	1.1	1.1	1.2	0.2	0.2	0.4	0.2	1.2
Other (weight %)	0.1	0.2	0.1	0.4	0.4	0.2	0.4	0.1	Oligomer (weight %)	1.1	1.1	1.2	0.2	0.2	0.4	0.2	1.2

Comparative example 13～20

(modulation of starting raw material)

Method is similarly to Example 1 carried out.

(the 1st phase evaporation operation)

Method is similarly to Example 3 carried out.

(the 2nd phase evaporation operation)

The 1st melting liquid is offered the falling film type evaporation device in the 2nd stage, make EG in the 2nd melting liquid and the total content of free DEG become 0.3 weight % by the evaporation conditions of table 7.

Table 7

Comparative example	13	14	15	16	17	18	19	20
Comparative example	13	14	15	16	17	18	19	20	Temperature (℃)	120	120	120	180	180	180	150	150
Pressure (Pa)	40	80	300	40	80	300	40	300	Temperature (℃)	120	120	120	180	180	180	150	150
Pressure (Pa)	40	80	300	40	80	300	40	300	Evaporation time (h)	4.2	4.7	5.6	2.9	3.3	4.1	3.4	4.4

Table 8 shows free DEG content, the EG in the 2nd melting liquid and the total content of free DEG in the 1st, the 2nd phlegma and the 2nd melting liquid, the content of oligopolymer.

(molecular distillation operation)

The 2nd melting liquid that is obtained by aforesaid operations is offered the falling film type molecular distillation apparatus, and making weight ratio with cut and the residual thing of still kettle is like that to distillate cut at 7: 3.Table 9 shows the analytical results of resulting cut.

In comparative example 13～20, the same although be under various evaporation conditionses, to have carried out the 2nd phase evaporation operation with comparative example 5～12, can know that under any circumstance, quality and the receipts amount of refining BHET all have been subjected to influence.

Table 8

The phlegma of evaporization process, the analytical results of melting liquid

	Comparative example 13	Comparative example 14	Comparative example 15	Comparative example 16	Comparative example 17	Comparative example 18	Comparative example 19	Comparative example 20
	Comparative example 13	Comparative example 14	Comparative example 15	Comparative example 16	Comparative example 17	Comparative example 18	Comparative example 19	Comparative example 20	1st, the free DEG content (weight %) in the 2nd phlegma and the 2nd melting liquid	1.9	2.0	2.1	1.7	2.1	2.9	1.2	2.4
EG in the 1st melting liquid and free DEG content (weight %)	5.1	5.1	5.1	5.1	5.1	5.1	5.1	5.1		1.9	2.0	2.1	1.7	2.1	2.9	1.2	2.4
	5.1	5.1	5.1	5.1	5.1	5.1	5.1	5.1	Oligomer in the 1st melting liquid (weight %)	11.1	11.1	11.1	11.1	11.1	11.1	11.1	11.1
EG in the 2nd melting liquid and free DEG content (weight %)	0.3	0.3	0.3	0.3	0.3	0.3	0.3	0.3	Oligomer in the 1st melting liquid (weight %)	11.1	11.1	11.1	11.1	11.1	11.1	11.1	11.1
	0.3	0.3	0.3	0.3	0.3	0.3	0.3	0.3	Oligomer in the 2nd melting liquid (weight %)	14.4	15.2	16.5	11.7	12.0	13.5	11.0	15.3

Table 9

The analytical results of the cut of molecular distillation

The quality of refining BHET behind the molecular distillation	Comparative example 13	Comparative example 14	Comparative example 15	Comparative example 16	Comparative example 17	Comparative example 18	Comparative example 19	Comparative example 20
	Comparative example 13	Comparative example 14	Comparative example 15	Comparative example 16	Comparative example 17	Comparative example 18	Comparative example 19	Comparative example 20	The receipts amount (kg) of refining BHET	69	70	70	67	69	70	68	70
Optical density (OD) (380nm)	0.004	0.004	0.005	0.003	0.005	0.007	0.003	0.006	The receipts amount (kg) of refining BHET	69	70	70	67	69	70	68	70
Optical density (OD) (380nm)	0.004	0.004	0.005	0.003	0.005	0.007	0.003	0.006	BHET content (weight %)	97.6	97.6	97.0	98.3	97.6	96.9	98.8	97.3
DEG ester content (weight %)	1.5	1.5	1.8	1.0	1.8	2.3	0.7	1.9	BHET content (weight %)	97.6	97.6	97.0	98.3	97.6	96.9	98.8	97.3
DEG ester content (weight %)	1.5	1.5	1.8	1.0	1.8	2.3	0.7	1.9	Oligomer (weight %)	0.5	0.6	1.1	0.2	0.2	0.4	0.2	0.6
Other (weight %)	0.4	0.3	0.1	0.5	0.4	0.4	0.3	0.2	Oligomer (weight %)	0.5	0.6	1.1	0.2	0.2	0.4	0.2	0.6

Embodiment 5

(modulation of starting raw material)

Mixture 118kg under 280 ℃ heating the pre-depolymerization of the reducing cuttings 202kg of used PET bottle with BHET and its oligopolymer, then, adding depolymerization catalyzer sodium hydroxide 0.96kg respectively and make in depolymerization liquid thick BHET concentration in this pre-depolymerizing substance is the EG 1 of 20 weight %, 800kg, further depolymerization is carried out in heating under 220 ℃, obtaining with EG is the depolymerization liquid 2 of solvent, 120kg.

This depolymerization liquid is cooled to 80 ℃, remove after contained foreign matter and the impurity with existent method, be cooled to 25 ℃, carry out the partial crystallization of 5 hours BHET, containing the BHET crystalline is that the slurry of solvent carries out solid-liquid separation with pressure filter with EG, has obtained containing the thick BHET crystallization filter cake 770kg of 45 weight %EG.

Melting, as the starting raw material of the refining usefulness of distillation process shown in Figure 1 by the 100 ℃ of heating under nitrogen atmosphere of the resulting filter cake of aforesaid operations.The concentration of whole solutes is 19.5 weight % in this starting raw material, contains the DEG ester of the 4.0 weight % that are equivalent to whole solutes, and specific conductivity is 0.4 μ s/cm.

(the 1st phase evaporation operation)

To the 1st stage falling film type evaporation unit feeding starting raw material, under 150 ℃ of temperature, pressure 500Pa condition, steam low boiling point component with the feed rate of 50kg/h.The evaporation process time is 15.4h, and the amount of being cooled off the 1st phlegma that generates by low boiling point component is 21kg/h, and the growing amount of the 1st melting liquid is 29kg/h.

Table 10 shows EG in the 1st melting liquid and the total amount of free DEG, the content of oligopolymer.

(the 2nd phase evaporation operation)

Then, the 1st melting liquid is offered the 2nd stage falling film type evaporation device, under 150 ℃ of temperature, pressure 80Pa condition, steam remaining low boiling point component with the feed rate of 29kg/h.The evaporation process time is 15.9h, and the amount of being cooled off the 2nd phlegma that generates by low boiling point component is 2kg/h, and the growing amount of the 2nd melting liquid is 27kg/h.

Table 10 shows free DEG content, the EG in the 2nd melting liquid and the total content of free DEG in the 1st, the 2nd phlegma and the 2nd melting liquid, the content of oligopolymer.

(molecular distillation operation)

Feed rate with 27kg/h offers the falling film type molecular distillation apparatus to the 2nd melting liquid, is like that to distillate cut at 7: 3 in order to make weight ratio with cut and the residual thing of still kettle, carries out molecular distillation under 195 ℃ of temperature, pressure 13Pa condition.Distillate cut with 19kg/h, distillation takes 15.7h.In the molecular distillation, use in the 1st phase evaporation operation resulting whole the 1st phlegma as the part of the cold medium of internal condensation device.Table 11 shows the analytical results of resulting cut.

Table 10

The phlegma of evaporization process, the analytical results of melting liquid

	Embodiment

5
5	Free DEG content (weight %) in phlegma in evaporization process and the melting liquid	1.3
EG in the 1st melting liquid and the content of free DEG (weight %)		1.3	5.1
	The content of the oligopolymer in the 1st melting liquid (weight %)	11.1	5.1
EG in the 2nd melting liquid and the content of free DEG (weight %)		11.1	0.3
	The content of the oligopolymer in the 2nd melting liquid (weight %)	12.0	0.3

Table 11

The analytical results of the cut of molecular distillation

The quality of refining BHET behind the molecular distillation	Embodiment	5
	Embodiment	5	The receipts amount (kg) of refining BHET	296
Optical density (OD) (380nm)	0.000		The receipts amount (kg) of refining BHET	296
Optical density (OD) (380nm)	0.000	BHET content (weight %)	99.2
DEG ester content (weight %)	0.5	BHET content (weight %)	99.2
DEG ester content (weight %)	0.5	Oligomer (weight %)	0.2
Other (weight %)	0.1	Oligomer (weight %)	0.2

Embodiment 6

(modulation of starting raw material)

(pre-depolymerization)

Mix have 10 weight %, to be the beer of gas blocking agent be ground into the square fragment 57kg of mean sizes 8mm and BHET 25kg with the used PET bottle of the painted PET bottle of multilayer (bottle that is made of ethylene glycol terephthalate) packs in the autoclave that has stirrer of 800L with penylene dimethylamine (nylon MXD 6) between poly hexamethylene adipamide, carries out pre-depolymerization under normal pressure, 250 ℃ of temperature condition.

(depolymerization)

Then, in this pre-depolymerizing substance, add EG 418kg and depolymerization catalyzer sodium hydroxide 0.23kg respectively, under pressure 0.13MPa, 220 ℃ of conditions, further carry out depolymerization reaction, the limit distillates low boiler cuts such as water from the cat head of the rectifying tower that is provided with autoclave, 60 minutes depolymerization is carried out on the limit, and obtaining with EG is the depolymerization reaction solution 500kg of solvent.

(removing of solid foreign materials)

This reaction soln is cooled to 180 ℃, undecomposed solid foreign materials (bottle cap, label etc.) in depolymerization reaction is removed, be transported in the 800L cooling tank with 60 purpose line filter screens.

(decolouring is handled)

In cooling tank, temperature is cooled to 80 ℃, remove solid foreign materials such as pigment more than the particle diameter 1 μ m, particulate with strainer, then, this depolymerization reaction solution under 80 ℃ with space velocity 0.57 hour ^-1After the bleaching tower of having filled gac (" Di Yahaopu 008 " 105kg that Mitsubishi Chemical's (strain) makes), remove foreign matters such as particulate more than the particle diameter 1 μ m, micro mist charcoal again with strainer.

(cationic exchange processing)

Next, this reaction soln with space velocity 4.8 hours ^-1Under 80 ℃ of temperature, handle by carrying out cationic exchange in the decationized Y sieve tower of having filled cation exchange column (Zeo-karb " An Balaite IR-120B " 25L that ロ-system ア Application De バ-ス company makes).

(anionresin processing)

Thereafter, with 30s by connecting piece, and under 80 ℃ of temperature with space velocity 2 hours ^-1Carrying out anionresin in the exhaustion of yin ion tower of having filled anion ion exchange body (Zeo-karb " An Balaite IRA96SB " 30L that ロ-system ア Application De バ-ス company makes and the mixture of Zeo-karb " An Balaite IR-120B " 30L) handles.

The pH of this reaction soln was 5.2 before cationic exchange is handled, and cationic exchange is 1.8 after handling, and anionresin is 4.9 after handling.The specific conductivity of this reaction soln was 537 μ s/cm before cationic exchange is handled, and anionresin is 0.4 μ s/cm after handling.Whole solutes of the reaction solution after anionresin is handled are 19.5 weight %.The content of DEG ester is equivalent to 4 weight % of whole solutes.Also have, the content of the gas blocking agent composition in the solids component (solute) (composition that comes from nylon MXD 6) is 0.6 weight %.

(partial crystallization operation)

The sub-treatment solution of above-mentioned disengaging is cooled to 25 ℃ with the speed of 0.2 ℃/min from 80 ℃ in the partial crystallization groove, kept 5 hours, make its partial crystallization at 25 ℃.The crystalline median size that obtains is 60 μ m.

(solid-liquid separation process)

Thereafter, being maintained under 25 ℃ of conditions, with Gas permeability 5cm is housed ³/ mincm ²The pressure filter of filter cloth carry out solid-liquid separation, obtained containing the filter cake 145kg (taking rate 29 weight %) of the thick BHET of 60 weight %.The content of gas blocking agent composition is 0.1 weight % in this filter cake.Melt in 100 ℃ of heating under nitrogen atmosphere operating the filter cake that obtains thus, as distillation process purified starting raw material shown in Figure 1.

(the 1st phase evaporation operation)

To the 1st stage falling film type evaporation unit feeding starting raw material, under 150 ℃ of temperature, pressure 500Pa condition, steam low boiling point component with the feed rate of 50kg/h.The evaporation process time is 15.4h, and the amount of being cooled off the 1st phlegma that generates by low boiling point component is 21kg/h, and the growing amount of the 1st melting liquid is 29kg/h.The total amount of EG in the 1st melting liquid and free DEG is 5.0 weight %.

(the 2nd phase evaporation operation)

Then, the 1st melting liquid is offered the 2nd stage falling film type evaporation device, under 150 ℃ of temperature, pressure 80Pa condition, steam remaining low boiling point component with the feed rate of 29kg/h.The evaporation process time is 15.9h, and the amount of being cooled off the 2nd phlegma that generates by low boiling point component is 2kg/h, and the growing amount of the 2nd melting liquid is 27kg/h.The total content of EG in the 2nd melting liquid and free DEG is 0.3 weight %.

(molecular distillation operation)

Feed rate with 27kg/h offers the falling film type molecular distillation apparatus to the 2nd melting liquid, is like that to distillate cut at 7: 3 in order to make weight ratio with cut and the residual thing of still kettle, carries out molecular distillation under 195 ℃ of temperature, pressure 13Pa condition.Distillate cut with 19kg/h, distillation takes 15.7h.Table 12 shows the analytical results of resulting cut.

Resulting refining BHET is 0.002 in the optical density (OD) of 380nm, can't check the composition that comes from the gas barrier properties polymkeric substance.The result can confirm thus, even have the painted PET bottle of gas barrier properties, adopts the method for the present invention also can regeneration.

Table 12

The analytical results of the cut of molecular distillation

The quality of refining BHET behind the molecular distillation	Embodiment 6
	Embodiment 6	The receipts amount (kg) of refining BHET	61
Optical density (OD) (380nm)	0.002	The receipts amount (kg) of refining BHET	61
Optical density (OD) (380nm)	0.002	BHET content (weight %)	99.0
DEG ester content (weight %)	0.6	BHET content (weight %)	99.0
DEG ester content (weight %)	0.6	Oligomer (weight %)	0.2
Other (weight %)	0.2	Oligomer (weight %)	0.2
Other (weight %)	0.2	Gas blocking agent composition (weight %)	Do not detect

The effect of invention

As by above explanation, according to the present invention, spent glycol is the ethylene glycol solution that contains crude terephthalic acid two (2-hydroxyethyl) ester, particularly be that the polyester of main component decomposes that to obtain to contain terephthalic acid two (2-hydroxyethyl) ester be main solute with the polyethylene terephthalate, ethylene glycol is the decomposition Generation Liquid (EG solution) of primary solvent, just can do one's utmost to suppress impurity DEG particularly in the refinement treatment process by it, the pair of DEG ester and oligopolymer is given birth to, and except these impurity, can also be effectively separated the gas blocking agent composition, thereby can obtain highly purified BHET.

The commercial application possibility

Recovery, the recycling of the bottle that process for purification of the present invention is particularly made by PETG for the PETG molded article for so-called material regeneration field, are useful namely.

Claims

1. the process for purification of terephthalic acid two (2-hydroxyethyl) ester, it is characterized in that the ethylene glycol solution that contains crude terephthalic acid two (2-hydroxyethyl) ester through comprising (1) evaporization process, it comprises that (a) imports first evaporation unit to this solution, under the condition of 130～170 ℃ of temperature, pressure 300～1000Pa, steam low boiling point component, obtain ethylene glycol and free Diethylene Glycol add up to content the fs evaporization process of first melting liquid of 3～10 weight % and

(b) this first melting liquid is imported second evaporation unit, under the condition of 130～170 ℃ of temperature, pressure 50～250Pa, steam low boiling point component, obtain ethylene glycol and free Diethylene Glycol add up to content the subordinate phase evaporization process of the 0.45 weight % or following second melting liquid and

(2) this second melting liquid is imported the falling film type molecular distillation apparatus, distill under 180～220 ℃ of temperature, pressure 25Pa or following condition, to obtain with terephthalic acid two (2-hydroxyethyl) ester be main component, terephthalic acid 2-hydroxyethyl [2-(2-hydroxyl-oxethyl) ethyl] ester content makes with extra care in the operation of the molecular distillation operation of 1 weight % or following cut at 1.5 weight % or following and oligomer.

2. the method described in the claim 1 is characterized in that the whole solute concentrations in the described ethylene glycol solution that contains crude terephthalic acid two (2-hydroxyethyl) ester are 5～85 weight %.

3. the method described in the claim 1 is characterized in that the described ethylene glycol solution that contains crude terephthalic acid two (2-hydroxyethyl) ester is terephthalic acid 2-hydroxyethyl [2-(2-hydroxyl-oxethyl) ethyl] ester that contains 1～8 weight % that the is equivalent to whole solutes solution as secondary solute.

4. the method described in the claim 1 is characterized in that the described specific conductivity that contains the ethylene glycol solution of crude terephthalic acid two (2-hydroxyethyl) ester is 0.2～0.6 μ S/cm.

5. the method described in the claim 1, it is characterized in that the described ethylene glycol solution that contains crude terephthalic acid two (2-hydroxyethyl) ester is that to be made with the polyethylene terephthalate by spent glycol be that the polyester of main component decomposes and then breaks away from son through decolouring and handles resulting solution, perhaps this solution is carried out that filter cake that partial crystallization handles, will obtain after filtration melts and liquid.

6. the method described in the claim 1, it is characterized in that the total content by the low boiling point component of the evaporization process free Diethylene Glycol in free Diethylene Glycol and described the 2nd melting liquid in the refrigerative phlegma be described phlegma and described the 2nd melting liquid total weight 2 weight % or below it.

7. the method described in the claim 1 is characterized in that oligomer in described the 2nd melting liquid is at 15 weight % or below it.

8. the method described in the claim 1 is characterized in that the cut of described molecular distillation operation and the weight ratio of the residue in the still kettle are 9: 1～5: 5.

9. the method described in the claim 1 is characterized in that the low boiling point component that it evaporates the 1st phase evaporation operation uses as at least a portion in the cold medium of the condenser of molecular distillation operation.