Classifications

• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
  • C08J11/00—Recovery or working-up of waste materials
  • C08J11/04—Recovery or working-up of waste materials of polymers
  • C08J11/10—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation
  • C08J11/105—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation by treatment with enzymes
• • C—CHEMISTRY; METALLURGY
  • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
  • C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
  • C12N9/00—Enzymes; Proenzymes; Compositions thereof; Processes for preparing, activating, inhibiting, separating or purifying enzymes
  • C12N9/14—Hydrolases (3)
  • C12N9/16—Hydrolases (3) acting on ester bonds (3.1)
  • C12N9/18—Carboxylic ester hydrolases (3.1.1)
• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
  • C08J2367/00—Characterised by the use of polyesters obtained by reactions forming a carboxylic ester link in the main chain; Derivatives of such polymers
  • C08J2367/02—Polyesters derived from dicarboxylic acids and dihydroxy compounds
• • C—CHEMISTRY; METALLURGY
  • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
  • C12Y—ENZYMES
  • C12Y301/00—Hydrolases acting on ester bonds (3.1)
  • C12Y301/01—Carboxylic ester hydrolases (3.1.1)
  • C12Y301/01074—Cutinase (3.1.1.74)
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
  • Y02W30/00—Technologies for solid waste management
  • Y02W30/50—Reuse, recycling or recovery technologies
  • Y02W30/62—Plastics recycling; Rubber recycling

Definitions

• the present invention relates to a process for the enzymatic depolymerization of polyethylene terephthalate (PET), in particular contained in a plastic material.
• PET polyethylene terephthalate
• the method according to the invention can in particular be implemented on an industrial or semi-industrial scale.
• Plastic products are inexpensive, durable materials that can be used to make a wide variety of products for a variety of applications (food packaging, clothing textiles, etc.).
• the production of plastics has increased dramatically in recent decades. Most of them are used for short-term applications, which results in an accumulation of plastic waste and the need to treat it.
• PET polyethylene terephthalate
• an aromatic polyester produced from terephthalic acid and ethylene glycol and which is used in many applications such as food packaging (bottles , bottles, pots, trays, pockets), but also in the production of textiles for clothing, decoration (carpet), household linen, etc.
• the Applicant has managed to develop an optimized process allowing the enzymatic depolymerization of plastics containing PET at a temperature close to the Tg of this PET, in order to make the chains of said polymer more readily accessible to the depolymerization enzyme and thus increase the rate of depolymerization.
• the inventor had to respond to conflicting problems.
• the enzymes capable of depolymerizing polymers are mainly more active on amorphous polymers than on semi-crystalline polymers.
• a process of depolymerization at a temperature close to the Tg of a polymer could theoretically make it possible to improve the accessibility of the enzyme to the chains of said polymer to be depolymerized, via an increase in the mobility of the chains of this polymer, when a polymer is subjected to a temperature close to or above its Tg, the latter tends to recrystallize more quickly, thus making the polymer more difficult to depolymerize for the enzyme.
• the inventor has thus demonstrated that it is possible to carry out a depolymerization process of PET at a temperature close to or above the Tg of said PET, while ensuring on the one hand that the degree of crystallinity of the PET is sufficiently low prior to the depolymerization step and on the other hand by selecting an enzyme capable of depolymerizing this PET in a depolymerization time less than the time necessary for said PET to reach a level of crystallinity incompatible with an enzymatic depolymerization.
• the process developed by the inventor makes it possible to maintain depolymerization rates within of a reactor compatible with an implementation on an industrial scale.
• the inventor has succeeded in depolymerizing more than 90% of a PET in less than 10 h at a temperature of 72 ° C.
• the method of the invention can be implemented for the depolymerization and / or recycling of plastics containing PET.
• the subject of the invention is therefore a process for the enzymatic depolymerization of polyethylene terephthalate (PET) by bringing said PET into contact with an enzyme capable of depolymerizing said PET, characterized in that the PET has an initial degree of crystallinity of at most 25 %, the depolymerization step is carried out at a temperature T equal to the Tg +/- 10 ° C of said PET, and the enzyme is selected so that a depolymerization time (tD) of the PET by said enzyme is strictly less than a crystallization time (tR) of said PET, in which the time tD represents the time necessary for said enzyme to depolymerize at least 80% of said PET at said temperature T, and the time tR represents the time necessary for said PET to achieve a degree of crystallinity of at most 35% at said temperature T.
• tD depolymerization time
• tR crystallization time
• the depolymerization step is preferably carried out at a temperature T of between 66 ° C and 80 ° C, preferably between 68 ° C and 73 ° C, the time tD being less than or equal to 20 hours, preferably less than 16 hours.
• Figure 1 Kinetics of recrystallization of a PET contained in a plastic material during the incubation of said material at different temperatures.
• the expression “plastic material” designates plastic products (such as sheets, trays, films, tubes, blocks, fibers, fabrics, etc.) and the plastic compositions used to make plastic products.
• the plastic material is composed of amorphous and / or semi-crystalline polymers.
• the plastic material may contain, in addition to the polymer or polymers, additional substances or additives, such as plasticizers, mineral or organic fillers, dyes, etc.
• the plastic material refers to any product plastic and / or plastic composition comprising at least one polymer in semi-crystalline and / or amorphous form and more particularly at least one PET.
• Plastic products include in particular manufactured plastic products, such as rigid or flexible packaging (films, bottles, trays), agricultural films, bags, disposable objects, textiles, fabrics, nonwovens, floor coverings, plastic waste or waste fibers, etc.
• polymer refers to a chemical compound whose structure consists of multiple repeating units (i.e. "monomers”) linked by chemical covalent bonds.
• polymer refers more precisely to such chemical compounds used in the composition of plastic materials.
• polyester refers to a polymer which contains an ester functional group in the main chain of its structure.
• the ester functional group is characterized by a bond between a carbon and three other atoms: a single bond with another carbon atom, a double bond with oxygen and a single bond with another oxygen atom. Oxygen bound to carbon by a single bond is itself bound to another carbon by a single bond.
• Polyesters can be made up of only one type of monomer (i.e. homopolymer) or at least two different monomers (i.e. copolymer).
• the polyesters can be aromatic, aliphatic or semi-aromatic.
• polyethylene terephthalate is a semi-aromatic copolymer composed of two monomers, terephthalic acid and ethylene glycol.
• the term "semi-crystalline polymers” refers to partially crystalline polymers, in which crystalline and amorphous regions coexist.
• the degree of crystallinity of a semi-crystalline polymer can be estimated by various analytical methods, and is generally between 10% and 90%. A polymer with a degree of crystallinity of less than 10% can be considered as amorphous.
• a “depolymerization process” in relation to a polymer or plastic material refers to a process by which a polymer or at least one polymer of a plastic material is degraded into smaller molecules, such as monomers and / or oligomers.
• a process for depolymerizing PET or a plastic material containing PET refers to a process in which PET is degraded to monomers such as terephthalic acid and / or ethylene glycol and / or to oligomers such as dimethyl terephthalate (DMT), methyl-2-hydroxyethyl terephthalate (MHET), bis (2-hydroxyethyl) terephthalate (BHET).
• DMT dimethyl terephthalate
• MHET methyl-2-hydroxyethyl terephthalate
• BHET bis (2-hydroxyethyl) terephthalate
• the depolymerization process according to the invention is based on an enzymatic depolymerization of a PET, by bringing said PET into contact with at least one enzyme capable of depolymerizing it. More particularly, the inventor has developed an enzymatic depolymerization process for PET comprising a depolymerization step carried out at a temperature T of between Tg -10 ° C and Tg + 10 ° C of said PET, starting from a PET with an initial degree of crystallinity of at most 25%. Also, according to a particular embodiment of the invention, the PET is selected so that the latter has an initial degree of crystallinity of at most 25%.
• the PET subjected to the depolymerization step is an amorphous and / or semi-crystalline PET at the start of the depolymerization step, the initial degree of crystallinity of which is less than or equal to 25%.
• the term "initial degree of crystallinity” means the degree of crystallinity of the PET at the start of the depolymerization step, that is to say before the contacting of said PET with a depolymerization enzyme.
• the “initial degree of crystallinity” corresponds to the degree of crystallinity after these pretreatment steps.
• the degree of crystallinity of a semi-crystalline polymer can be estimated by various analytical methods, and is generally between 10% and 90%. For example, differential scanning calorimetry (DSC) or X-ray diffraction can be used to determine the degree of crystallinity of polymers. Other techniques are also suitable for determining the crystallinity of polymers, but with lower reliability, such as X-ray scattering at small angles (SAXS) or at large angles (WAXS) and infrared spectroscopy. In the present application, the crystallinity is measured by differential scanning calorimetry (DSC).
• DSC differential scanning calorimetry
• X-ray diffraction can be used to determine the degree of crystallinity of polymers.
• Other techniques are also suitable for determining the crystallinity of polymers, but with lower reliability, such as X-ray scattering at small angles (SAXS) or at large angles (WAXS) and infrared spectroscopy.
• SAXS small angles
• DSC experiments were carried out using the following protocol: a small amount of plastic material (several mg) is heated at a constant heating rate, from room temperature or from a temperature below room temperature to a temperature above the melting temperature (Tf) of the polymer. Heat flow data is collected and plotted against temperature. The degree of crystallinity (Xc) expressed as a percentage (%) is calculated according to the following formula:
• AHf corresponds to the enthalpy of fusion which can be determined by integrating the endothermic fusion peak
• AHcc corresponds to the enthalpy of cold crystallization and determined by integrating the exothermic cold crystallization peak
• wt represents the weight fraction of polyester in the plastic
• AHfl 00% corresponds to the enthalpy of fusion for a fully crystalline polymer and can be found in the literature.
• DHO 00% of PET corresponds in the literature to 125.5 J / g (Polymer Data Handbook, second edition, edited by James E. Mark, OXFORD, 2009).
• the margin of error for measuring the degree of crystallinity is approximately 10%.
• a degree of crystallinity evaluated at 25% corresponds to a degree of crystallinity between 22.5% and 27.5%.
• a PET is selected which has a degree of crystallinity of less than 25%, +/- 10%.
• the PET has an initial degree of crystallinity of less than 20%, +/- 10%.
• the PET subjected to the depolymerization step is an amorphous PET, that is to say having a degree of crystallinity of less than 10%, +/- 10%.
• the depolymerization process according to the invention is implemented with a plastic material comprising at least PET.
• the PET represents at least 80% by weight of said plastic material, preferably at least 85%, 90%, 95%.
• plastic material designates any plastic product in the form of fibers, such as textiles, fabrics, nonwovens, threads, etc.
• the plastic material is selected from fibers and / or fiber and / or textile waste and the PET represents at least 60% by weight relative to the total weight of said plastic material, preferably at least minus 65%, 70%, 75%, 80%, 85%, 90%, 95%.
• the plastic material comprises a mixture of PET and polylactic acid (PLA), a mixture of PET and polyethylene (PE), a mixture of PET and polytrimethylene terephthalate (PTT), a mixture of PET and polyamide (PA), or a mixture of PET and cotton.
• PLA polylactic acid
• PE polyethylene
• PET polytrimethylene terephthalate
• PA PET and polyamide
• the plastic materials used in the reactor are plastic waste or fiber waste. This waste can come from collection channels intended for recycling, but also can be waste from the production or recycling sector, and can therefore contain compounds other than plastic waste. This implies that PET can be engaged in the reactor in combination with other elements present in these flows (such as paper, cardboard, aluminum, glue, etc.).
• the reactor in which the depolymerization step is carried out is loaded with several plastic materials containing at least PET, preferably containing at least 80% by weight of PET, relative to the total weight in plastic materials, preferably at least 85%, 90%, 95%.
• PET is characterized by its initial glass transition temperature (Tg), that is to say before contacting said PET with a depolymerization enzyme.
• Tg initial glass transition temperature
• the PET undergoes a pretreatment step (amorphization, micronization)
• the PET is characterized by its Tg after these pretreatment steps.
• This temperature can be estimated by different analytical methods. For example, differential scanning calorimetry (DSC) or differential thermal analysis (DTA) can be used to determine the Tg of a polymer.
• DSC differential scanning calorimetry
• DTA differential thermal analysis
• the Tg corresponds to the temperature transition glass measured by DSC during the first temperature sweep as indicated in the examples.
• the margin of error for Tg measurement is around 2 ° C.
• the initial Tg of PET is between 60 ° C and 90 ° C, preferably between 60 ° C and 85 ° C. In another particular mode, the initial Tg of the PET is between 65 ° C +/- 1 ° C and 80 ° C +/- 1 ° C. In another particular mode, the initial Tg of the PET is between 65 ° C +/- 2 ° C and 80 ° C +/- 2 ° C. In another particular mode, the initial Tg of PET is between 60 ° C +/- 2 ° C and 70 ° C +/- 2 ° C.
• the PET or the plastic material containing the PET is reduced to powder form by any suitable means known to those skilled in the art.
• the PET, or the plastic material containing the PET is advantageously micronized so as to be transformed into powder form.
• the PET or the plastic material containing the PET used in the reactor is in the form of powder with an average particle size (d50) of less than 2 mm, preferably with a particle size of less than 1 mm.
• the PET or the plastic material containing the PET used in the reactor is in the form of powder with an average particle size (d50) of less than 500 ⁇ m.
• the depolymerization process comprises a step of amorphization of PET, followed by a step of grinding and / or micronization of PET or of the plastic material containing PET before the step of depolymerization of PET.
• the depolymerization process comprises a step of amorphization of PET before the step of depolymerization of PET and, the PET or the plastic material containing the PET is engaged in the reactor in the form of granules derived from the extruder used for amorphization.
• the PET or the plastic material containing the PET is used in the form of granules of size less than 2 mm, preferably of size less than 1 mm.
• the depolymerization process is carried out with an enzyme capable of depolymerizing PET. More particularly, the enzyme is selected so that a depolymerization time (tD) of the PET by said enzyme is strictly less than a crystallization time (tR) of said PET.
• the time required for said PET of an initial crystallinity Xc to reach a rate, or degree, of crystallinity of 35% or less than 35% at temperature T is dependent on the nature of the material and / or the nature of the polymer (ie the presence of additives and / or co-monomers), its molecular weight, its Tg and also its thermal history (previous treatments that have involved cooling and / or heating, such as amorphization or micronization).
• This time is measured under conditions where the temperature T is regulated, and is not affected by agitation and / or the pH during the measurement.
• the crystallization time (tR) of PET it is possible to measure the crystallization time (tR) of PET at a temperature T by incubation of the plastic material containing the PET at this temperature T, and by regular measurement of the crystallinity rate (by DSC) of samples taken at different time intervals.
• the depolymerization time "(tD)" represents the time necessary for the polymer degrading enzyme to depolymerize at least 80% of said polymer at a temperature T.
• this time is determined at the optimum pH of the enzyme and at a saturated concentration of enzyme, ie a concentration above which the reaction rate is not improved by the addition of enzyme.
• the time tD corresponds to the time necessary for the enzyme to release 80% of the monomers present in the polymer.
• the time tD corresponds to the time necessary to obtain after contacting the enzyme and the PET, 80% of terephthalic acid (AT) equivalent present in the PET, the corresponding AT equivalent to free AT and the AT present in the oligomers of BHET and MHET.
• the time tD corresponds to the time necessary to obtain, after contacting the enzyme and the PET, 80% of monoethylene glycol equivalent (ME G) in PET, the MEG equivalent corresponding to the free MEG and to the MEG present in the oligomers of BHET and MHET. It is specified that the measurement of the times tD and tR is carried out at the same temperature T.
• the enzyme is advantageously selected from the enzymes having a melting temperature (Tm) strictly higher than the temperature T at which the depolymerization step is carried out.
• Tm melting temperature
• the temperature Tm corresponds more particularly to the temperature at which half of the quantity of the enzyme considered is unfolded or improperly folded, so that it loses all or part of its activity relative to the activity of the enzyme properly folded.
• the Tm makes it possible in particular to estimate the thermostability of the enzyme considered.
• the Tm can be measured by any means known to those skilled in the art, in particular the DSF (differential fluorimetric analysis). Alternatively, Tm can be assessed by analysis of protein folding using the circular dichroism method. Preferably, the Tm is measured using the DSF as explained in the experimental part.
• the enzyme is selected from the enzymes having a Tm greater than or equal to the temperature T + 10 ° C, preferably greater than or equal to the temperature T + 15 ° C, more preferably greater than or equal to the temperature T + 20 °.
• the depolymerization activity of an enzyme on a polymer can be evaluated by any means known to those skilled in the art. For example, it can be evaluated by the loss of mass of the polymer or the measurement of the rate of depolymerization of the polymer, ie the quantity of monomers and / or oligomers produced over a period of time.
• the depolymerization activity of a PET degrading enzyme can be evaluated by measuring the amounts of oligomers (BHET and / or MHET) and / or of monomers (terephthalic acid and / or ethylene glycol and / or DMT) released under specific conditions of temperature and pH and by bringing the PET or the plastic material containing the PET into contact with said enzyme.
• the depolymerization activity can also be evaluated by monitoring the addition of base during the depolymerization reaction.
• An addition of base is indeed carried out so as to neutralize the terephthalic acid produced by the depolymerization and thus regulate the pH.
• the amount of base added during the reaction makes it possible to measure the amount of terephthalic acid produced during the reaction.
• a basic solution is added so as to maintain the reaction medium at the optimum pH of the enzyme.
• said enzyme is selected from cutinases, lipases and esterases degrading said PET.
• said enzyme is selected from the esterases degrading said PET.
• the enzyme can be selected from the cutinases derived from Thermobifida cellulosityca, Thermobifida halotolerans, Thermobifida fusca, Thermobifida alba, Bacillus subtilis, Fusarium solani pisi, Humicola insolens (such as that referenced A0A075B5G4 in the Uniprot database), Sirococcus conigenus, Pseudomonas mendocina and Thielavia terrestris or a variant thereof.
• cutinase is selected from cutinases from metagenomic libraries such as LC-Cutinase described in Sulaiman et al., 2012 or variants of the latter.
• the enzyme is a lipase, preferably from Ideonella sakaiensis.
• the enzyme can be selected from commercial enzymes such as Novozym 51032 or variants of these enzymes.
• the enzyme is selected from the enzymes having an amino acid sequence having at least 75% identity with SEQ ID No. 1 and / or with SEQ ID No. 2 and / or with SEQ ID N ° 3 and / or with SEQ ID N ° 4 and / or SEQ ID N ° 5, and having a depolymerization activity of PET.
• the enzyme is selected from enzymes having an amino acid sequence having at least 75% identity with SEQ ID No. 1, and a depolymerization activity of PET.
• the enzyme is capable of depolymerizing the polymer to oligomers, in this case it is advantageously associated with an enzyme capable of depolymerizing said oligomers into monomers.
• the two enzymes are then selected from among the enzymes having an amino acid sequence having at least 75% identity with SEQ ID No. 4 and / or SEQ ID No. 5.
• the process of the invention is particularly suitable in the particular case where the selected enzyme has an amino acid sequence having at least 90% identity with SEQ ID No. 1 and comprising at least one combination mutations selected from F208I + D203C + S248C + Y92G, F208W + D203C + S248C + Y92G or F208I + D203C + S248C + VI 701 + Y92G compared to SEQ ID No.1.
• the time tD is less than or equal to 20 hours, preferably less than or equal to 18 hours, 16 hours, 14 hours, 12 hours, 10 hours.
• the time tD is between lh and l6h, preferably between lh and lh.
• the crystallization time tR is preferably greater than or equal to 20 hours, preferably greater than or equal to 18 hours, 16 hours, 14 hours, 12 hours, 10 hours.
• the time tR corresponds to the time necessary for said PET, having an initial crystallinity less than or equal to 25%, to reach a crystallinity of 30%, or less than 30%, at said temperature T.
• the process for the enzymatic depolymerization of polyethylene terephthalate (PET) according to the invention is characterized in that
• - PET has an initial degree of crystallinity of at most 25%
• the depolymerization step is carried out at a temperature T equal to the Tg +/- 10 ° C of said PET, and
• the enzyme is selected so that a depolymerization time (tD) of the PET by said enzyme is strictly less than a crystallization time (tR) of said PET, in which the time tD represents the time necessary for the enzyme selected to depolymerize at least 80% of said PET at said temperature T, and the time tR represents the time necessary for said PET to reach a degree of crystallinity of 30%, or less than 30%, at said temperature T.
• the enzyme is selected from enzymes having a Tm greater than or equal to the temperature T + 10 ° C, preferably greater than or equal to the temperature T + 15 ° C, more preferably greater than or equal to the temperature T + 20 ° .
• the process for the enzymatic depolymerization of polyethylene terephthalate (PET) according to the invention is characterized in that
• a PET having an initial degree of crystallinity of at most 25%; an enzyme capable of degrading the PET is selected, so that a depolymerization time (tD) of the PET by the said enzyme is strictly less than a crystallization time (tR) of the said PET, in which the time tD represents the time required for the selected enzyme to depolymerize at least 80% of said PET at said temperature T, and time tR represents the time required for said PET to reach a degree of crystallinity of 30%, or less, at said temperature T; and
• An enzymatic depolymerization step of said PET is carried out by bringing said PET into contact with said enzyme at a temperature T equal to the Tg +/- 10 ° C of said PET.
• the enzyme is selected from enzymes having a Tm greater than or equal to the temperature T + 10 ° C, preferably greater than or equal to the temperature T + 15 ° C, more preferably greater than or equal to the temperature T + 20 ° .
• the time tD corresponds to the time necessary for said enzyme to depolymerize at least 85% of said PET at said temperature T, preferably at least 90%.
• the process for the enzymatic depolymerization of polyethylene terephthalate (PET) according to the invention is characterized in that
• - PET has an initial degree of crystallinity of at most 25%
• the depolymerization step is carried out at a temperature T equal to the Tg +/- 10 ° C of said PET, and
• the enzyme is selected so that a depolymerization time (tD) of the PET by said enzyme is strictly less than a crystallization time (tR) of said PET, in which the time tD represents the time necessary for the enzyme selected to depolymerize at least 85% of said PET at said temperature T, preferably at least 90%, and the time tR represents the time necessary for said PET to reach a degree of crystallinity of at most 35%, preferably at most 30% at said temperature T.
• the enzyme is selected from the enzymes having a Tm greater than or equal to the temperature T + 10 ° C, preferably greater than or equal to the temperature T + 15 ° C, more preferably greater than or equal to the temperature T + 20 ° .
• the process for the enzymatic depolymerization of polyethylene terephthalate (PET) according to the invention is characterized in that
• - a PET is selected having an initial degree of crystallinity of at most 25%;
• a depolymerization time (tD) of PET by said enzyme is strictly less than a crystallization time (tR) of said PET, in which time tD represents the time required for the selected enzyme to depolymerize at least 85% of said PET at said temperature T, preferably at least 90%, and the time tR represents the time necessary for said PET to reach a degree of crystallinity of at most 35%, preferably a crystallinity rate of at most 30% at said temperature T; and
• a step of depolymerization of said PET is carried out by bringing said enzyme into contact with said PET at a temperature T equal to the Tg +/- 10 ° C of said PET.
• the enzyme is selected from enzymes having a Tm greater than or equal to the temperature T + 10 ° C, preferably greater than or equal to the temperature T + 15 ° C, more preferably greater than or equal to the temperature T + 20 ° .
• the process for the enzymatic depolymerization of PET comprises the steps according to which:
• - a PET is selected having an initial degree of crystallinity of at most 25%;
• an enzyme capable of degrading the PET is selected, so that a depolymerization time (tD) of the PET by the said enzyme is strictly less than a crystallization time (tR) of the said PET, in which the time tD represents the time required for said enzyme to depolymerize at least 80% of said PET at said temperature T, and the time tR represents the time necessary for said PET to reach a degree of crystallinity of 35%, or less than 35%, at said temperature T -
• the depolymerization step is carried out by bringing the enzyme into contact with the PET, at a temperature T equal to the Tg +/- 10 ° C of said PET.
• the depolymerization step according to the invention is advantageously carried out in a reactor whose volume is greater than 500 milliliters (mL), greater than 1 liter (L), preferably greater than 2 L, 5 L, 10 L.
• the method of the invention can be implemented on an industrial and / or semi-industrial scale. It is thus possible to use a reactor whose volume is greater than 100L, 150L, 1000L, 10,000 L, 100,000 L, 400,000 L.
• the quantity of enzyme used during the depolymerization step is advantageously sufficient to allow a total or almost total depolymerization of said PET (ie, degradation up to at least 80% by weight relative to the weight of said PET engaged) in reaction times compatible with implementation on an industrial scale.
• the ratio by weight of quantity of enzyme committed to quantity of PET committed is between 0.01 / 1000 and 3/1000.
• the ratio of quantity of enzyme used to quantity of PET used is between 0.5 / 1000 and 2.5 / 1000, more preferably between 1/1000 and 2/1000.
• the quantity of enzyme used is greater than or equal to the quantity of enzyme necessary to reach a saturated concentration of enzyme.
• the enzyme can be used in the form of a composition comprising, in addition to the enzyme, excipients, which can be selected from the buffers commonly used in biochemistry, preservatives, and / or stabilizing agents. The amount of enzyme then advantageously denotes the amount of enzyme free of any excipient.
• the PET depolymerization step is carried out at a temperature T equal to the Tg +/- 10 ° C of said PET, the Tg being that of said PET before the depolymerization step.
• the temperature is kept below the inactivation temperature of the enzyme.
• the step of depolymerization of PET is carried out at a temperature T of between Tg-10 ° C and Tg + 5 ° C of PET.
• the depolymerization step is carried out at a temperature T of between Tg-8 ° C and Tg + 2 ° C of PET.
• the depolymerization step is carried out at a temperature T of between Tg-10 ° C and Tg -5 ° C of PET.
• the PET has a Tg of 78 ° C +/- 2 ° C and the depolymerization step is carried out at a temperature T equal to 70 ° C +/- 2 ° C.
• the PET has a Tg of 78 ° C +/- 2 ° C and the depolymerization step is carried out at a temperature T equal to 72 ° C +/- 2 ° C.
• the PET has a Tg of 75 ° C +/- 2 ° C and the depolymerization step is carried out at a temperature T equal to 68 ° C +/- 2 ° C.
• the PET has a Tg of 75 ° C +/- 2 ° C and the depolymerization step is carried out at a temperature T equal to 70 ° C +/- 2 ° C.
• the PET has a Tg of between 70 ° C +/- 2 ° C and 75 ° C +/- 2 ° C and the depolymerization step is carried out at a temperature T of between 65 ° C + / -2 ° C and 72 ° C +/- 2 ° C.
• the PET comes from a plastic material selected from fibers and / or waste fibers and / or textiles and has a Tg of between 60 ° C +/- l ° C and 75 ° C +/- l ° C, and the depolymerization step is carried out at a temperature T equal to 65 ° C +/- 2 ° C.
• the PET comes from a plastic material selected from fibers and / or fiber and / or textile waste and has a Tg of between 60 ° C +/- 1 ° C and 70 ° C +/- 1 ° C and the depolymerization step is carried out at a temperature T equal to 60 ° C +/- 2 ° C.
• the depolymerization step is carried out at a temperature T of between 66 ° C and 80 ° C, preferably between 68 ° C and 73 ° C. In one particular mode, the depolymerization step is carried out at a temperature T of 72 ° C. +/- 1 ° C. In another particular mode, the depolymerization step is carried out at a temperature T of 70 ° C. +/- 1 ° C.
• PET polyethylene terephthalate
• the depolymerization step is carried out at a temperature T of between 66 ° C and 80 ° C, preferably between 68 ° C and 73 ° C, and
• the enzyme is selected so that a depolymerization time (tD) of the PET by said enzyme is strictly less than a crystallization time (tR) of said PET, in which the time tD represents the time necessary for the enzyme selected to depolymerize at least 80% of said PET at said temperature T, and the time tR represents the time necessary for said PET to reach a degree of crystallinity of 35%, or less than 35%, at said temperature T.
• a PET is selected having an initial degree of crystallinity of at most 25%, preferably at most 20%.
• a PET is selected having an initial degree of crystallinity of at most 25% and a Tg of between 65 ° C +/- 1 ° C and 80 ° C +/- 1 ° C.
• the process for the enzymatic depolymerization of polyethylene terephthalate (PET) according to the invention is characterized in that
• - PET has an initial degree of crystallinity of at most 25% and a Tg of between 65 ° C +/- l ° C and 80 ° C +/- l ° C;
• the depolymerization step is carried out at a temperature T of 72 ° C +/- 1 ° C, and
• the enzyme is selected so that a depolymerization time (tD) of the PET by said enzyme is strictly less than a crystallization time (tR) of said PET, in which the time tD represents the time necessary for the enzyme selected to depolymerize at least 80%, preferably at least 85%, more preferably at least 90% of said PET at said temperature T, and the time tR represents the time necessary for said PET to reach a degree of crystallinity of at most 35% at said temperature T.
• tD depolymerization time
• tR crystallization time
• tR represents the time necessary for said PET to reach a degree of crystallinity of at most 30% at said temperature T.
• the enzyme is selected from the enzymes having a Tm greater than or equal to the temperature T + 10 ° C. , preferably greater than or equal to the temperature T + 15 ° C, more preferably greater than or equal to the temperature T + 20 °.
• the process for the enzymatic depolymerization of polyethylene terephthalate (PET) according to the invention is characterized in that
• a PET is selected having an initial degree of crystallinity of at most 25% and a Tg of between 75 ° C +/- 1 ° C and 80 ° C +/- 1 ° C;
• the depolymerization step is carried out at a temperature T of 72 ° C +/- 1 ° C, and
• the enzyme is selected so that a depolymerization time (tD) of the PET by said enzyme is strictly less than a crystallization time (tR) of said PET, in which the time tD represents the time necessary for the enzyme selected to depolymerize at least 80%, preferably at least 85%, more preferably at least 90% of said PET at said temperature T, and the time tR represents the time necessary for said PET to reach a degree of crystallinity of at most 35% at said temperature T.
• tR represents the time necessary for said PET to reach a degree of crystallinity of at most 30% at said temperature T.
• the enzyme is selected from the enzymes having a Tm greater than or equal to the temperature T + 10 ° C, preferably greater than or equal to the temperature T + 15 ° C, more preferably greater than or equal to the temperature T + 20 °.
• the process for the enzymatic depolymerization of polyethylene terephthalate (PET) according to the invention is characterized in that - PET has an initial degree of crystallinity of at most 25% and a Tg of between
• the depolymerization step is carried out at a temperature T of 70 ° C +/- 1 ° C, and
• the enzyme is selected so that a depolymerization time (tD) of the PET by said enzyme is strictly less than a crystallization time (tR) of said PET, in which the time tD represents the time necessary for the enzyme selected to depolymerize at least 80%, preferably at least 85%, more preferably at least 90% of said PET at said temperature T, and the time tR represents the time necessary for said PET to reach a degree of crystallinity of at most 35% at said temperature T.
• tR represents the time necessary for said PET to reach a degree of crystallinity of at least plus 30% at said temperature T.
• the enzyme is selected from the enzymes having a Tm greater than or equal to the temperature T + 10 ° C, preferably greater than or equal to the temperature T + 15 ° C, more preferably greater or equal to the temperature T + 20 °.
• a PET is selected having an initial degree of crystallinity of at most 25% and a Tg of between 65 ° C +/- l ° C and 80 ° C +/- l ° C and l
• the depolymerization step is carried out at a temperature T of 70 ° C +/- 1 ° C.
• the process for the enzymatic depolymerization of polyethylene terephthalate (PET) according to the invention is characterized in that
• a plastic material is selected from fibers and / or fiber and / or textile waste comprising PET having an initial degree of crystallinity of at most 25% and a Tg of between 60 ° C +/- 1 ° C and 75 ° C +/- 1 ° C;
• an enzyme capable of degrading the PET is selected, so that a depolymerization time (tD) of the PET by the said enzyme is strictly less than a crystallization time (tR) of the said PET, in which the time tD represents the time required for the selected enzyme to depolymerize at least 80%, preferably at least 85%, more preferably at least 90% of said PET at said temperature T, and the time tR represents the time required for said PET to reach a level of crystallinity d '' at most 35% at said temperature T, and
• the PET depolymerization step is carried out by bringing said enzyme into contact with said plastic material at a temperature T of 65 ° C. +/- 1 ° C.
• tR represents the time necessary for said PET to reach a degree of crystallinity of 30% at said temperature T.
• the enzyme is selected from the enzymes having a Tm greater than or equal to the temperature T + 10 ° C, preferably greater or equal to the temperature T + 15 ° C, more preferably greater than or equal to the temperature T + 20 °.
• the process for the enzymatic depolymerization of polyethylene terephthalate (PET) according to the invention is characterized in that
• a plastic material is selected from fibers and / or fiber and / or textile waste comprising PET having an initial degree of crystallinity of at most 25% and a Tg of between 60 ° C +/- 1 ° C and 70 ° C +/- 1 ° C;
• an enzyme capable of degrading the PET is selected, so that a depolymerization time (tD) of the PET by the said enzyme is strictly less than a crystallization time (tR) of the said PET, in which the time tD represents the time required for the selected enzyme to depolymerize at least 80%, preferably at least 85%, more preferably at least 90% of said PET at said temperature T, and the time tR represents the time required for said PET to reach a level of crystallinity d '' at most 35% at said temperature T, and
• the PET depolymerization step is carried out by bringing said enzyme into contact with said plastic material at a temperature T of 60 ° C. +/- 1 ° C.
• tR represents the time necessary for said PET to reach a degree of crystallinity of at most 30% at said temperature T.
• the enzyme is selected from the enzymes having a Tm greater than or equal to the temperature T + 10 ° C. , preferably greater than or equal to the temperature T + 15 ° C, more preferably greater than or equal to the temperature T + 20 °.
• the crystallization time (tR) of the PET is measured prior to the depolymerization step, on a sample of the said PET.
• the enzyme is selected so that the depolymerization time (tD) of PET by said enzyme is strictly less than the crystallization time (tR) of said PET.
• the enzyme is selected so that the time tD corresponds to the time necessary for said enzyme to depolymerize at least 90% of said PET at said temperature T, and so that the time tR corresponds to the time necessary for said PET to reach a crystallinity rate of at most 30% at said temperature T.
• the time tD is less than 20 hours, preferably less than 18 hours, 16 hours, 14 hours, 14 hours, 12 hours, 10 hours.
• the time tD is between lh and l6h, preferably between lh and lOh.
• the step of depolymerization of PET is carried out by bringing said PET and said selected enzyme into contact at a temperature T.
• the pH is regulated in order to optimize the yield of the depolymerization process in function of the solubility of the monomers / oligomers.
• the pH is regulated to be maintained at the optimal pH of the enzyme +/- 1.
• the pH is thus regulated to be maintained between 6.5 and 9.
• the pH is regulated between 6.5 and 8.5 during the depolymerization step, preferably between 7 and 8.
• the pH is regulated between 7.5 and 8.5.
• the contents of the reactor are kept under stirring during the depolymerization step.
• the speed of stirring is regulated by a person skilled in the art so as to be sufficient to allow a suspension of the plastic / polyester material engaged in the reactor, a uniformity of the temperature and an accuracy of the pH regulation.
• the stirring speed is maintained between 50 rpm and 500 rpm, in particular at 80 rpm,
• Amorphization of PET from plastic material The depolymerization process is carried out using colored and washed plastic flakes from the PET plastic waste recycling sector. These plastic materials, composed of 98% m / m (by weight) of PET with an average crystallinity of 34%, underwent an extrusion step, followed by rapid cooling allowing the amorphization of the PET contained in the waste.
• the extruder used for the amorphization was a KMB ZE 60A twin screw extruder equipped with a gear pump, a filter changer, a die and an underwater cutting system. The set temperature was 265 ° C in the extruder areas, 280 ° C in the gear pump, 280 ° C in the filter changer areas and 360 ° C in the die.
• the water used in the granulation system has been regulated to a temperature of 80 ° C.
• a gravimetric dosing system marketed by Brabender was used. A flow rate of 150 kg / ha was used.
• For the granulation a die comprising 120 holes of 0.8 mm in diameter was used. The cutting speed was 4500 rpm.
• the amorphization made it possible to obtain granules of size less than 1 mm, the degree of crystallinity of which was measured at 16% (by DSC).
• the granules were then subjected to a powder reduction step using a disc sprayer. The powder was subjected to a 400mhi sieve to recover only the smaller powders. The degree of crystallinity of this powder was determined at 16% in accordance with Example 1.2 below.
• a Mettler Toledo DSC 3 device was used with a dry air flow. Only the first temperature scan was carried out to determine the thermal characteristics of the PET powder, from a powder sample from Example 1.1, in particular the glass transition temperature (Tg) and the level of crystallinity initial. The temperature rise was carried out from 25 ° C to 280 ° C with a heating rate of 10 ° C / min with approximately 10 mg of sample using a 40 ⁇ L aluminum crucible.
• Tg glass transition temperature
• the temperature rise was carried out from 25 ° C to 280 ° C with a heating rate of 10 ° C / min with approximately 10 mg of sample using a 40 ⁇ L aluminum crucible.
• the Tg was determined, using the STARe Mettler Toledo software, in the middle of the glass transition represented on the thermogram of the sample, and the initial degree of crystallinity according to the equation detailed in the description.
• the Tg of the PET powder produced in Example 1.1 was evaluated at 78.4 ° C.
• Example 1.2 shows the evolution of the crystallinity of PET as a function of time, at different temperatures: 65 ° C, 70 ° C, 72 ° C, 75 ° C.
• the PET reaches 35% crystallinity after 17.5 hours respectively; 11, 5h and 5h.
• the PET reaches 30% of crystallinity after 16 hours respectively; 10h and 4.3h.
• E. coli BL21 DE3 (New England Biolabs, Ipswich, MA) by culture in a self-inducing medium ZYM (Studier et al., 2005 - Prot. Exp. Pur. 41 , 207-234) for 23 hours at 21 ° C.
• E. coli cells were harvested by centrifugation (6000 x g, 10 min at 4 ° C) and suspended in lysis buffer (20 mM Tris-HCl, pH 8, 300 mM NaCl). The cells were broken by sonication on ice and the lysate was clarified by centrifugation (10,000 x g, 30 min at 4 ° C).
• the soluble fraction was subjected to a TALON metal affinity resin (Clontech, CA). After washing the unbound proteins with the lysis buffer supplemented with 10 mM imidazole, the bound proteins were eluted with an elution buffer (20 mM Tris-HCl, pH 8, 300 mM NaCl, 100 mM imidazole). The buffer was finally exchanged for a storage buffer (20 mM Tris-HCl, pH 8, 300 mM NaCl) by dialysis. The concentration of purified proteins was determined on the basis of the molar extinction coefficient calculated at 280 nm.
• the DSL was used to assess the melting temperatures (Tm) of the enzymes used.
• Protein samples were prepared at a concentration of 14 mM (0.4 mg / mL) and stored in a buffer consisting of 20 mM Tris HCl, pH 8.0, 300 mM NaCl.
• the SYPRO Orange Dye 5000x DMSO stock solution was first diluted 250 times in water.
• the Protein samples were loaded onto a 96-well PCR plate (Lifescience Bio-Rad, France, cat # HSP9601), each well containing a final volume of 25 pL.
• the final concentration of SYPRO Orange protein and dye in each well was 5mM (0.14 mg / ml) and 10 x, respectively.
• the volumes loaded per well were as follows: 15 ⁇ L of buffer, 9 ⁇ L of the 0.4 mg / ml protein solution and 1 ⁇ L of the 250 ⁇ SYPRO Orange diluted solution.
• the PCR plates were then sealed with an optical quality adhesive strip and centrifuged at 2000 rpm for 1 min at room temperature.
• DSF experiments were then performed using a Bio-Rad CFX96 real-time PCR system tuned to the FRET channel to use the 450/490 excitation and 560/580 emission filters.
• the samples were heated from 25 to 100 ° C at a rate of 1 ° C / min.
• a fluorescence measurement was carried out every 0.3 ° C.
• the melting temperature was determined from the peak (s) of the first derivatives of the melting curve using the Bio-Rad CFX Manager software.
• the Tm values correspond to the average of 3 measurements.
• the characterization of the depolymerization rate of PET was carried out by regularly taking samples subjected to analysis by ultra high performance liquid chromatography (UHPLC) to measure the amount of terephthalic acid equivalent produced according to the method described below. below.
• UHPLC ultra high performance liquid chromatography
• the amount of terephthalic acid produced can also be estimated via the amount of base added to the medium during the reaction.
• the concentration of AT equivalent was determined by chromatography (UHPLC). If necessary (in the presence of insoluble TA), the samples were diluted in 100 mM potassium phosphate buffer, pH 8. 150 ⁇ L of methanol and 6.5 ⁇ L of 6 N HCl were added to 150 ⁇ L of sample or dilution. After homogenization and filtration through a 0.45 ⁇ m syringe filter, 20 ⁇ l of sample were injected into the UHPLC, Ultimate 3000 UHPLC system (Thermo Lisher Scientif ⁇ c, Waltham, MA) comprising a pump module, a sampler automatic, a column oven thermostatically controlled at 25 ° C and a UV detector at 240 nm.
• UHPLC Ultimate 3000 UHPLC system
• AT Terephthalic acid
• MHET and BHET Terephthalic acid
• MHET and BHET Terephthalic acid
• MHET and BHET Terephthalic acid
• MHET and BHET Terephthalic acid
• MHET and BHET were separated using a methanol gradient (30% to 90%) in 1 mM H2SO4 at 1 m / min through a Discovery HS C18 HPLC column (150 mm x 4.6 mm, 5 pm) equipped with a guard column (Supelco, Bellefonte, PA).
• AT, MHET and BHET were measured according to standard curves prepared from AT and commercial BHET and MHET synthesized internally.
• the AT equivalent corresponds to the sum of the AT measured and the AT contained in the MHET and BHET measured.
• Example 2 The enzymes of Example 2 were tested at different temperatures (70 ° C +/- 1 ° C and 72 ° C +/- 1 ° C) in order to evaluate which could be selected to implement the method of l invention at these different temperatures. The enzymes were thus tested at a saturated concentration. Tests at a temperature of 60 ° C were also carried out, the temperature of 60 ° C corresponding to the temperature traditionally used in the depolymerization processes of the prior art (negative control).
• the crystallization times tR of the PET from Example 1.1 to reach 30% and 35% of crystallinity are respectively 16h and 17.5h at 70 ° C, and 10h and 11.5h at 72 ° C.
• Tables 2, 3, 4 and 5 below respectively indicate the measurement of the tD times of the enzymes E1, E2, E3, and E4 at different temperatures.
• tD is thus greater than tR at 72 ° C.
• the enzyme cannot therefore be selected for the implementation of the method of the invention.
• One reason is that it is not stable enough and / or active enough to reach 80% conversion before the PET has reached a crystallinity rate above 30%.
• the enzyme E2 can be selected to carry out the process of the invention at 72 ° C allowing a significant improvement in yield compared to a process at 60 ° C (reduction by 2.3 of the time to reach 90% of depolymerization ).
• E3 can be selected to implement the process of the invention at 72 ° C.
• Table 5 Measurement of the tD times of E4 at 60 ° C (control), 70 ° C and 72 ° C.
• E2 and E3, E4 can also be selected to implement the process of the invention at 70 ° C and 72 ° C, allowing a significant improvement in yield compared to a process at 60 ° C.
• Example 4 Process for Degrading a Plastic Material from Textile Waste Comprising PET
• Amorphization of PET from plastic material from textile waste and measurement of the degree of crystallinity of PET The depolymerization process is carried out using production scrap from a water jet weaving process, the material of which is under as a cluster of continuous threads and contains approximately 100% PET. These textile materials have undergone a drying step at 60 ° C for 16 h and then an extrusion step, followed by rapid cooling allowing the amorphization of the PET contained in the waste.
• the extruder used for the amorphization was a ZSE 18 MAXX twin screw extruder from Leistritz. The temperatures of the heating zones have been set according to the following profile:
• the screw rotation speed was set at 150 rpm.
• the introduction of the material into the extruder was carried out manually.
• the rod arriving at the head of the extruder is then immediately immersed in a water bath at 10 ° C.
• the rod obtained was granulated and then reduced to the form of a fine powder using a micronizer (lmm grid).
• the powder was then subjected to a 500mhi sieve to recover only powders smaller than this size.
• the crystallinity of the powder was determined, in accordance with Example 1.2, to be less than 10%. 4.1.2 Measurement of the PET crystallization kinetics of the plastic material
• the measurement of the Tg of the PET was carried out with the same protocol as in Example 1.2.
• the Tg of the PET powder produced in Example 4.1.1 was evaluated at 75.7 ° C.
• a domed bottom reactor with a total volume of 5L (Global Process Concept) was used.
• the reactor was equipped with a temperature probe and a pH probe (Hamilton, EasyFerm HB BioArc 325).
• the regulation of these two parameters at set values was ensured by PID controllers internal to the C-bio software (Global Process Concept).
• a pale 5.5 cm diameter marine fixed to the central shaft rotating at 300 rpm allowed the reaction medium to be agitated.
• the pH is adjusted to 8.0 by adding 20% m.m sodium hydroxide.
• the enzyme E4 was added in a weight ratio of 1/1000 per quantity of PET used. It was produced by fermentation of a recombinant microorganism in a liquid medium. Table 6 below indicates respectively the measurement of the times tD of the enzyme E4 on the plastic material defined in 4.1.1 at different temperatures.
• E4 can therefore be selected to implement the method of the invention at 68 ° C on the plastic material defined in 4.1.1 while allowing a significant improvement in yield compared to a process at 60 ° C.
• Example 5 Process for degrading a plastic material from plastic waste. Selection and scaling up.
• the extruder used for the amorphization was a KMB ZE 60A twin screw extruder equipped with a gear pump, a filter changer, a die and an underwater head cutting system.
• the temperature was set at 265 ° C in the extruder areas, 275 ° C in the gear pump, 275 ° C in the filter changer areas and 350 ° C in the die.
• the screw rotation speed was 160 rpm.
• the water used in the granulation system was regulated to a temperature of 80 ° C.
• 2 gravimetric dosing systems marketed by Brabender were used. A flow rate of 300 kg / h was used.
• For the granulation a die comprising 240 holes of 0.75 mm in diameter was used.
• the cutting speed was 3800 rpm.
• the amorphization made it possible to obtain granules of size less than 1 mm, the degree of crystallinity of which was measured at 12% (by DSC).
• the granules were then subjected to a powder reduction step using a disc sprayer.
• the powder was subjected to a 500mhi sieve to recover only the smaller powders.
• the crystallinity of the powder was determined, in accordance with Example 1.2, to be 16.5% (DSC).
• the measurement of the Tg of the PET was carried out with the same protocol as in Example 1.2.
• the Tg of the PET powder produced in Example 5.1.1 was evaluated at 75.2 ° C. 5.1.3 Measurement of the PET crystallization kinetics of the plastic material
• test A a flat-bottomed stirred reactor with a total volume of 500 mL (MiniBioreactors, Global Process Concept) was used. It was equipped with a temperature probe and a pH probe (Hamilton, EAsyFerm HB BioArc 120). The regulation of these two parameters to set values was ensured by PID controllers internal to the C-bio software (Global Process Concept). A pale marine diameter of 3 cm fixed to the central shaft rotating at 300 rpm allowed the reaction medium to be agitated.
• the pH is regulated at 8.0 by adding 20% sodium hydroxide mm
• the enzyme E4 was added according to a weight ratio of 1/1000 per quantity of PET used It was produced by fermentation of '' a recombinant microorganism in liquid medium.
• Table 7 respectively shows the measurement of the tD times of the E4 enzyme at different temperatures.
• E4 can therefore be selected to implement the process of the invention at these two temperatures on the plastic material defined in 5.1.1. Note that the use of E4 at 66 ° C and 72 ° C should allow a significant improvement in yield compared to a process at 60 ° C.
• a flat-bottom reactor with a total volume of 1000 L was used.
• the reactor was equipped with a temperature probe and a pH probe (In Pro3 l00 / SG / 325, Mettler Toledo).
• a pale navy of variable diameter allowed the agitation of the reaction medium.
• the pH is regulated to 8.0 by adding sodium hydroxide at 20% m.m.
• the enzyme E4 was added according to a weight ratio of 2/1000 per quantity of PET used. It was produced by fermentation of a recombinant microorganism in a liquid medium.

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