Method for obtaining a purified diester effluent by depolymerising a polyester comprising opaque polyethylene terephthalate
The present invention relates to a process for depolymerizing a polyester feedstock comprising opaque PET, which comprises: a) a conditioning step; b) a step of glycolysis, operated at between 180 and 400° C., a residence time of from 0.1 to 10 h in the presence of diol; c) a diol separation step, at a temperature of between 100 and 250° C., a pressure lower than that of step b) and producing a diol effluent and an effluent rich in monomers; d) a step of separating into a heavy impurities effluent and a prepurified monomers effluent, at a temperature of less than 250° C. and a pressure of less than 0.001 MPa and a residence time of less than 10 min; e) a step of decolourizing the prepurified monomers effluent, by adsorption of a mixture comprising between 20% and 90% by weight of the prepurified monomers effluent and a solvent, at a temperature of between 100 and 200° C., a pressure of between 0.1 and 1.0 MPa and in the presence of at least one adsorbent.
1 . A process for depolymerizing a polyester feedstock comprising opaque polyethylene terephthalate (PET), said process comprising:
a) a conditioning step comprising a conditioning section supplied at least with said polyester feedstock, to produce a conditioned stream;
b) a step of depolymerization by glycolysis, which is supplied at least with the conditioned stream and with a supplement of diol so that the molar amount of diol is adjusted to between 1 to 20 moles of diol per mole of diester in said polyester feedstock, conducted at a temperature of between 18° and 400° C. and for a residence time of between 0.1 and 10 h;
c) a diol separation step, which is supplied at least with the effluent from step b), and is conducted at a temperature of between 10° and 250° C., at a pressure less than that of step b), and which produces a diol effluent and a liquid effluent rich in monomers, wherein said diol separation step is implemented in two to five successive gas-liquid separation sections, each producing a gaseous effluent and a liquid effluent, wherein the liquid effluent from the preceding section supplies the subsequent section, a liquid effluent obtained from a last gas-liquid separation section forms the liquid effluent rich in monomers, and all the gaseous effluents are recovered to form the diol effluent;
d) a step of separation of the liquid effluent rich in monomers obtained from step c) into a heavy impurities effluent and a prepurified monomers effluent, which is conducted at a temperature of less than 250° C. and a pressure of less than 0.001 MPa with a liquid residence time of less than 10 min, and
e) a step for decolorizing the prepurified monomers effluent, comprising at least a mixing section for mixing the prepurified monomers effluent obtained in step d) with a solvent to form a mixture wherein the prepurified monomers effluent represents between 20% and 90% by weight of the total weight of the mixture, and an adsorption section conducted at a temperature of between 10° and 200° C. and at a pressure of between 0.1 and 1.0 MPa in the presence of at least one adsorbent selected from activated carbons, alumina and clays, to obtain a purified monomers effluent.
2 . The process according to claim 1 , wherein said polyester feedstock comprises at least 50% by weight of polyethylene terephthalate.
3 . The process according to claim 1 , wherein said polyester feedstock comprises at least 10% by weight of opaque PET.
4 . The process according to claim 1 , wherein said polyester feedstock comprises colored PET.
5 . The process according to claim 1 , wherein said polyester feedstock comprises between 0.1% and 10% by weight of pigments.
6 . The process according to claim 1 , wherein said polyester feedstock comprises between 0.05% and 1% by weight of dyes.
7 . The process according to claim 1 , wherein the solvent in decolorizing step e) comprises a fraction of the diol effluent obtained from step c), a supplement of diol external to the process, or mixtures thereof.
8 . The process according to claim 1 , wherein the prepurified monomers effluent represents between 30% and 80% by weight of the total weight of the mixture in step e).
9 . The process according to claim 1 , wherein at least one adsorbent in step e) is an activated carbon.
10 . The process according to claim 1 , wherein the adsorption section in step e) is operated in the presence of an adsorbent or two different adsorbents.
11 . The process according to claim 1 , wherein the adsorption section comprises two or more different adsorbents, said different adsorbents being in a mixture or placed in series in said adsorption section.
12 . The process according to claim 11 , wherein each of said different adsorbents are in different reactors placed in series.
13 . The process according to claim 1 , wherein the adsorption section of step e) is implemented in fixed bed adsorption mode.
14 . The process according to claim 1 , wherein the adsorption section of step e) is operated at a temperature of between 10° and 170° C.
15 . The process according to claim 1 , wherein said polyester feedstock comprises at least 70% by weight of polyethylene terephthalate.
16 . The process according to claim 1 , wherein said polyester feedstock comprises at least 90% by weight of polyethylene terephthalate.
17 . The process according to claim 1 , wherein said polyester feedstock comprises at least 15% by weight of opaque PET.
18 . The process according to claim 1 , wherein said polyester feedstock comprises between 0.1% and 5% by weight of pigments.
19 . The process according to claim 1 , wherein the prepurified monomers effluent represents between 50% and 75% by weight, of the total weight of the mixture in step e).
20 . The process according to claim 1 , wherein the adsorption section of step e) is operated at a temperature of between 120° C. and 150° C.
21 . The process according to claim 1 , wherein said polyester feedstock comprises 0.05% and 0.2% by weight of dyes.
22 . Process according to claim 1 , wherein the mixing section employs a static or dynamic mixer, and the residence time of the mixture in the mixing section is between 0.5 second and 20 minutes.
23 . Process according to claim 22 , wherein the mixture from the mixing section supplies the adsorption section which contains at least one adsorber, wherein the adsorption section is operated at a temperature of between 10° and 200° C. and a pressure of between 0.1 and 1.0 MPa, and the residence time of the mixture in each adsorber of the adsorption section is between 20 minutes and 40 hours.