DEPOLYMERIZATION OF POLYMERS WITH ESTER, ETHER AND CARBONATE LINKAGES USING ACIDIC IONIC LIQUID (AIL) CATALYST

Abstract

The present invention provides an effective and selective process for the depolymerization of polyethylene terephthalate (PET), polyethylene furanoate (PEF), polylactic acid, polycarbonates, polyethers and polyamides into pure and high yielding valorized products by combining the glycolysis-hydrolysis reactions using a homogeneous acidic ionic liquid (AIL) catalyst, resulting in excellent polymer conversion.

Claims

1. A process for the depolymerization of polymers, the process comprising the steps of: a) heating the reaction mixture of polymer and the acidic ionic liquid (AIL) catalyst, wherein polymer to catalyst ratio is in the range of 20.0:0.01-20:10.0, in an ethylene glycol: dioxane solvent mixture, wherein ethylene glycol: dioxane ratio is in the range of 1.0: 0.01-1.0: 5.0 (v/v), at a temperature in the range of 120-250° C. for a period in the range of 0.5 to 24 hour; b) adding water and diethyl ether into the reaction mixture obtained at step a) after completion of the reaction; c) washing ether layer obtained at step b) with aqueous NaOH solution; and d) acidifying the aqueous layer obtained at step c) to afford valorized product with 100% polymer conversion.

2. The process as claimed in claim 1, wherein the polymer is selected from the group comprising of polyethylene terephthalate (PET), polyethylene furanoate (PEF), Polylactic acid (PLA), polycarbonate, polyethers, and polyamide.

3. The process as claimed in claim 1, wherein said acidic ionic liquid (AIL) catalyst is selected from the group comprising of 1-methyl-3-(3-sulfopropyl)-imidazolium hydrogensulfate, [C.sub.3SO.sub.3HMIM][HSO.sub.4]; 1-methyl-3-(3-sulfopropyl)-imidazolium p-toluenesulfonate, [C.sub.3SO.sub.3HMIM][PTS]; 1-methyl-3-(3-sulfopropyl)-imidazolium dihydrogenphosphate, [C.sub.3SO.sub.3HMIM][H.sub.2PO.sub.4]; 1-methyl-3-(sulfopropyl)-imidazolium chloride, [C.sub.3SO.sub.3HMIM][Cl]; 1-methyl-3-(3-sulfopropyl)-imidazolium cupric chloride, [C.sub.3SO.sub.3HMIM][CuCl.sub.3]; 1-methyl-3-(3-sulfopropyl)-imidazolium ferric chloride, [C.sub.3SO.sub.3HMIM][FeCl.sub.4]; 1-methyl-3-(3-sulfopropyl)-imidazolium stannic chloride, [C.sub.3SO.sub.3HMIM][SnCl.sub.3]; 1-butyl-3-methylimidazolium chloride [BMIM][Cl], 1-butyl-3-methylimidazolium bromide [BMIM][Br], 1-methyl-3-(3-sulfopropyl)-benzimidazolium dihydrogenphosphate, [C.sub.3SO.sub.3HBenzMIM][H.sub.2PO.sub.4], 3-sulfopropyl-P,P,P-triphenylphosphonium hydrogensulfate [C.sub.3SO.sub.3H(C.sub.6H.sub.5)P][HSO.sub.4], N,N,N-triethyl-3-sulfopropanaminium hydrogen sulphate, [C.sub.3SO.sub.3H(C.sub.2).sub.3N][HSO.sub.4]; NN,N-triethyl-3-sulfopropanaminium p-toluenesulfonate, [C.sub.3SO.sub.3H(C.sub.2).sub.3N][PTS]; N,N,N-triethyl-3-sulfopropanaminium chloride, [C.sub.3SO.sub.3H(C.sub.2).sub.3N][Cl] and N,N,N-triethyl-3-sulfopropanaminium dihydrogenphosphate, [C.sub.3SO.sub.3H(C.sub.2).sub.3N][H.sub.2PO.sub.4].

4. The process as claimed in claim 2, wherein said acidic ionic liquid (AIL) is 1-methyl-3-(3-sulfopropyl)-imidazolium hydrogensulfate, [C.sub.3SO.sub.3HMIM][HSO.sub.4] is used as a catalyst.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0025] The detailed description is described with reference to the accompanying figures. In the figures, the left-most digit(s) of a reference number identifies the figure in which the reference number first appears. The same numbers are used throughout the drawings to reference like features and components.

[0026] FIG. 1 depicts Elemental analysis (CHNS): Percentage elemental composition of obtained product and the standard terephthalic acid (Sigma) matches exactly.

[0027] FIG. 2 depicts NMR Spectroscopy (.sup.1HNMR): Terephthalic acid formation was confirmed by comparing .sup.1HNMR spectra of both obtained product and the standard terephthalic acid (Sigma).

[0028] FIG. 3 depicts X-Ray Diffractometry: Powder XRD pattern of both the obtained terephthalic acid and the standard terephthalic acid matching exactly with all the peaks.

[0029] FIG. 4 depicts Chromatography (HPLC): HPLC analysis of both the obtained terephthalic acid (FIG. 4B) and the standard terephthalic acid (FIG. 4A) were done and it was found that the peaks in standard terephthalic acid is also appearing in the HPLC profile of terephthalic acid obtained by the depolymerisation of PET.

[0030] FIG. 5 depicts the GC-MS profile of polycarbonate depolymerisation reaction. From GC-MS profile, the main product of polycarbonate depolymerisation was found to be 4-isopropyl phenol. Further, yield was calculated by taking the area percentage of the peak from GC profile.

[0031] FIG. 6 depicts HPLC profile of polylactic acid depolymerisation reaction. Lactic acid product formation in polylactic acid depolymerisation was confirmed by doing HPLC analysis of water-soluble fraction of reaction mixture and comparing with standards of lactic acid. Yield was calculated by absolute calibration method.

DETAILED DESCRIPTION OF THE INVENTION

[0032] The invention will now be described in detail in connection with certain preferred and optional embodiments, so that various aspects thereof may be more fully understood and appreciated.

Definitions

[0033] For convenience, before further description of the present disclosure, certain terms employed in the specification, and examples are delineated here. These definitions should be read in the light of the remainder of the disclosure and understood as by a person of skill in the art. The terms used herein have the meanings recognized and known to those of skill in the art, however, for convenience and completeness, particular terms and their meanings are set forth below.

[0034] The articles “a”, “an” and “the” are used to refer to one or to more than one (i.e., to at least one) of the grammatical object of the article.

[0035] The terms “comprise” and “comprising” are used in the inclusive, open sense, meaning that additional elements may be included. It is not intended to be construed as “consists of only”.

[0036] Throughout this specification, unless the context requires otherwise the word “comprise”, and variations such as “comprises” and “comprising”, will be understood to imply the inclusion of a stated element or step or group of element or steps but not the exclusion of any other element or step or group of element or steps.

[0037] The term “polyester” refers to a polymeric compound where monomeric units are linked to each other via an ester group. In the present disclosure, the term “polyester” includes but not limited to polyethylene terephthalate (PET), polyethylene furanoate (PEF), polylactic acid (PLA), polyethylene naphthalate (PEN).

[0038] The term “polycarbonate” refers to a polymeric compound produced from monomers where each monomer is linked to the other by a carbonate group. In the present disclosure, the term “polycarbonate” includes but not limited to polycarbonate containing the precursor monomer of bisphenol A (BPA). They are typically produced by reaction between BPA and phosgene.

[0039] The term “polyether” refers to a polymeric compound produced from monomers where each monomer is linked to the other by an ether linkage. In the present disclosure, the term “polyether” includes but not limited to polyethylene glycol, polypropylene glycol, epoxy resins, lignin and carbohydrate based ethers and resins.

[0040] The term “polyamide” refers to a polymeric compound produced from monomers where each monomer is linked to the other by an amide group. In the present disclosure, the term “polyamide” includes but not limited to aliphatic polyamides such as nylon PA 6 and PA 66, polyphthalamides (PA 6T) and aramids.

[0041] Ratios, concentrations, amounts, and other numerical data may be presented herein in a range format. It is to be understood that such range format is used merely for convenience and brevity and should be interpreted flexibly to include not only the numerical values explicitly recited as the limits of the range, but also to include all the individual numerical values or sub-ranges encompassed within that range as if each numerical value and sub-range is explicitly recited. For example, a temperature in the range of 120° C. to 250° C. should be interpreted to include not only the explicitly recited limits of about 125° C. to about 155° C. but also to include sub-ranges, such as 136° C. to 225° C., and so forth, as well as individual amounts, within the specified ranges, such as 140° C., and 168.9° C.

[0042] The present disclosure is not to be limited in scope by the specific embodiments described herein, which are intended for the purposes of exemplification only. Functionally-equivalent products, compositions, and methods are clearly within the scope of the disclosure, as described herein.

[0043] The present invention provides a new process for the depolymerization of polymers with linkages such as ester (such as polyethylene terephthalate, polyethylene furanoate, polylactic acid, Polyethylene naphthalate etc.), carbonates (polycarbonates), ethers (polyethers) and amide (polyamides) into high yielding valorized products.

[0044] In an embodiment of the present disclosure, there is provided a process for the depolymerisation of polymers, wherein the process comprises the steps of: [0045] a) heating the reaction mixture of polymer and the acidic ionic liquid (AIL) catalyst in a suitable solvent mixture at a temperature in the range of 120-250° C. for a period in the range of 0.5 to 24 hr; [0046] b) adding water and diethyl ether into the reaction mixture obtained at step a) after completion of the reaction; [0047] c) washing ether layer obtained at step b) with aqueous NaOH solution; [0048] d) acidifying aqueous layer obtained at step c) to afford valorized product with 100% polymer conversion.

[0049] In another embodiment of the present disclosure, there is provided a process for the depolymerization of polymers, wherein the process comprises the steps of: [0050] a) heating the reaction mixture of polymer and the acidic ionic liquid (AIL) catalyst, wherein polymer to catalyst ratio is in the range of 20.0:0.01-20: 10.0, in an ethylene glycol: dioxane solvent mixture, wherein ethylene glycol: dioxane ratio is in the range of 1.0: 0.01 - 1.0: 5.0 (v/v), at a temperature in the range of 120-250° C. for a period in the range of 0.5 to 24 hour; [0051] b) adding water and diethyl ether into the reaction mixture obtained at step a) after completion of the reaction; [0052] c) washing ether layer obtained at step b) with aqueous NaOH solution; and [0053] d) acidifying the aqueous layer obtained at step c) to afford valorized product with 100% polymer conversion.

[0054] In an embodiment of the present disclosure, there is provided a process for the depolymerization of polymers, wherein the polymer is selected from the group comprising of polyethylene terephthalate (PET), Polyethylene furanoate (PEF), Polylactic acid (PLA), polycarbonate, polyethers, and polyamide. In a preferred embodiment of the present disclosure, there is provided a process for the depolymerization of polymers, wherein the polymer is polyethylene terephthalate (PET).

[0055] In an embodiment of the present disclosure, there is provided a process for the depolymerisation of polymers, wherein the polymer is selected from the group comprising of polyethylene terephthalate (PET), Polyethylene furanoate (PEF), Polylactic acid (PLA), polycarbonate, polyethers, and polyamide, and wherein the process comprises the steps of: [0056] a) heating the reaction mixture of polymer and the acidic ionic liquid (AIL) catalyst in a suitable solvent mixture at a temperature in the range of 120-250° C. for a period in the range of 0.5 to 24 hr; [0057] b) adding water and diethyl ether into the reaction mixture obtained at step a) after completion of the reaction; [0058] c) washing ether layer obtained at step b) with aqueous NaOH solution; [0059] d) acidifying aqueous layer obtained at step c) to afford valorized product with 100% polymer conversion.

[0060] In an embodiment of the present disclosure, there is provided a process for the depolymerization of polymers , wherein the acidic ionic liquid (AIL) catalyst is selected from the group comprising of various cations and anions having acidic functionality. More particularly, the acidic ionic liquid (AIL) catalyst is selected from the group comprising of 1-methyl-3-(3-sulfopropyl)-imidazolium hydrogensulfate, [C.sub.3SO.sub.3HMIM][HSO.sub.4]; 1-methyl-3-(3-sulfopropyl)-imidazolium p-toluenesulfonate, [C.sub.3SO.sub.3HMIM][PTS]; 1-methyl-3-(3-sulfopropyl)-imidazolium dihydrogenphosphate, [C.sub.3SO.sub.3HMIM][H.sub.2PO.sub.4]; 1-methyl-3-(sulfopropyl)-imidazolium chloride, [C.sub.3SO.sub.3HMIM][Cl]; 1-methyl-3-(3-sulfopropyl)-imidazolium cupric chloride, [C.sub.3SO.sub.3HMIM][CuCl.sub.3]; 1-methyl-3-(3-sulfopropyl)-imidazolium ferric chloride, [C.sub.3SO.sub.3HMIM][FeCl.sub.4]; 1-methyl-3-(3-sulfopropyl)-imidazolium stannic chloride, [C.sub.3SO.sub.3HMIM][SnCl.sub.3]; 1-butyl-3-methylimidazolium chloride [BMIM][Cl], 1-butyl-3-methylimidazolium bromide [BMIM] [Br], 1-methyl-3-(3-sulfopropyl)-benzimidazolium dihydrogenphosphate, [C.sub.3SO.sub.3HBenzMIM] [H.sub.2PO.sub.4], 3-sulfopropyl-P,P,P-triphenylphosphonium hydrogensulfate [C.sub.3SO.sub.3H(C.sub.6H.sub.5)P][HSO.sub.4], N,N,N-triethyl-3-sulfopropanaminium hydrogen sulphate, [C.sub.3SO.sub.3H(C.sub.2).sub.3N][HSO.sub.4]; N,N,N-triethyl-3-sulfopropanaminium p-toluenesulfonate, [C.sub.3SO.sub.3H(C.sub.2).sub.3N] [PTS]; N,N,N-triethyl-3-sulfopropanaminium chloride, [C.sub.3SO.sub.3H(C.sub.2).sub.3N][Cl] and N,N,N-triethyl-3-sulfopropanaminium dihydrogenphosphate, [C.sub.3SO.sub.3H(C.sub.2).sub.3N] [H.sub.2PO.sub.4].

[0061] In an embodiment of the present disclosure, there is provided a process for the depolymerisation of polymers, wherein the process comprises the steps of: [0062] a) heating the reaction mixture of polymer and the acidic ionic liquid (AIL) catalyst, wherein the acidic ionic liquid (AIL) catalyst is selected from the group comprising of 1-methyl-3-(3-sulfopropyl)-imidazolium hydrogensulfate, [C.sub.3SO.sub.3HMIM][HSO.sub.4]; 1-methyl-3-(3-sulfopropyl)-imidazolium p-toluenesulfonate, [C.sub.3SO.sub.3HMIM][PTS]; 1-methyl-3-(3-sulfopropyl)-imidazolium dihydrogenphosphate, [C.sub.3SO.sub.3HMIM][H.sub.2PO.sub.4]; 1-methyl-3-(sulfopropyl)-imidazolium chloride, [C.sub.3SO.sub.3HMIM][Cl]; 1-methyl-3-(3-sulfopropyl)-imidazolium cupric chloride, [C.sub.3SO.sub.3HMIM][CuCl.sub.3]; 1-methyl-3-(3-sulfopropyl)-imidazolium ferric chloride, [C.sub.3SO.sub.3HMIM][FeCl.sub.4]; 1-methyl-3-(3-sulfopropyl)-imidazolium stannic chloride, [C.sub.3SO.sub.3HMIM][SnCl.sub.3]; 1-butyl-3-methylimidazolium chloride [BMIM][Cl], 1-butyl-3-methylimidazolium bromide [BMIM][Br], 1-methyl-3-(3-sulfopropyl)-benzimidazolium dihydrogenphosphate, [C.sub.3SO.sub.3HBenzMIM][H.sub.2PO.sub.4], 3-sulfopropyl-P,P,P-triphenylphosphonium hydrogensulfate [C.sub.3SO.sub.3H(C.sub.6H.sub.5)P][HSO.sub.4], N,N,N-triethyl-3-sulfopropanaminium hydrogen sulphate, [C.sub.3SO.sub.3H(C.sub.2).sub.3N][HSO.sub.4]; N,N,N-triethyl-3-sulfopropanaminium p-toluenesulfonate, [C.sub.3SO.sub.3H(C.sub.2).sub.3N][PTS]; N,N,N-triethyl-3-sulfopropanaminium chloride, [C.sub.3SO.sub.3H(C.sub.2).sub.3N][Cl] and N,N,N-triethyl-3-sulfopropanaminium dihydrogenphosphate, [C.sub.3SO.sub.3H(C.sub.2).sub.3N][H.sub.2PO.sub.4], and wherein polymer to catalyst ratio is in the range of 20.0:0.01-20: 10.0, in an ethylene glycol: dioxane solvent mixture, wherein ethylene glycol: dioxane ratio is in the range of 1.0: 0.01 - 1.0: 5.0 (v/v), at a temperature in the range of 120-250° C. for a period in the range of 0.5 to 24 hr; [0063] b) adding water and diethyl ether into the reaction mixture obtained at step a) after completion of the reaction; [0064] c) washing ether layer obtained at step b) with aqueous NaOH solution; [0065] d) acidifying aqueous layer obtained at step c) to afford valorized product with 100% polymer conversion.

[0066] In a particular embodiment of the present disclosure, there is provided a process for the depolymerization of polymers , wherein the 1-methyl-3-(3-sulfopropyl)-imidazolium hydrogensulfate, [C.sub.3SO.sub.3HMIM][HSO.sub.4] is used as an acidic ionic liquid (AIL) catalyst.

[0067] In an embodiment of the present disclosure, there is provided a process for the depolymerization of polymers, wherein the process comprises the steps of: [0068] a) heating the reaction mixture of polymer and the acidic ionic liquid (AIL) catalyst, wherein said acidic ionic liquid (AIL) is 1-methyl-3-(3-sulfopropyl)-imidazolium hydrogensulfate, [C.sub.3SO.sub.3HMIM][HSO.sub.4] is used as a catalyst, and wherein polymer to catalyst ratio is in the range of 20.0:0.01-20: 10.0, in an ethylene glycol: dioxane solvent mixture, wherein ethylene glycol: dioxane ratio is in the range of 1.0: 0.01 - 1.0: 5.0 (v/v), at a temperature in the range of 120-250° C. for a period in the range of 0.5 to 24 hour; [0069] b) adding water and diethyl ether into the reaction mixture obtained at step a) after completion of the reaction; [0070] c) washing ether layer obtained at step b) with aqueous NaOH solution; and [0071] d) acidifying the aqueous layer obtained at step c) to afford valorized product with 100% polymer conversion.

[0072] In an embodiment of the present disclosure, there is provided a process for the depolymerisation of polymers, wherein the polymer is selected from the group comprising of polyethylene terephthalate (PET), Polyethylene furanoate (PEF), Polylactic acid (PLA), polycarbonate, polyethers, and polyamide, and wherein the process comprises the steps of: [0073] a) heating the reaction mixture of polymer and the acidic ionic liquid (AIL) catalyst, wherein the acidic ionic liquid (AIL) catalyst is selected from the group comprising of 1-methyl-3-(3-sulfopropyl)-imidazolium hydrogensulfate, [C.sub.3SO.sub.3HMIM][HSO.sub.4]; 1-methyl-3-(3-sulfopropyl)-imidazolium p-toluenesulfonate, [C.sub.3SO.sub.3HMIM][PTS]; 1-methyl-3-(3-sulfopropyl)-imidazolium dihydrogenphosphate, [C.sub.3SO.sub.3HMIM][H.sub.2PO.sub.4]; 1-methyl-3-(sulfopropyl)-imidazolium chloride, [C.sub.3SO.sub.3HMIM][Cl]; 1-methyl-3-(3-sulfopropyl)-imidazolium cupric chloride, [C.sub.3SO.sub.3HMIM][CuCl.sub.3]; 1-methyl-3-(3-sulfopropyl)-imidazolium ferric chloride, [C.sub.3SO.sub.3HMIM][FeCl.sub.4]; 1-methyl-3-(3-sulfopropyl)-imidazolium stannic chloride, [C.sub.3SO.sub.3HMIM][SnCl.sub.3]; 1-butyl-3-methylimidazolium chloride [BMIM][Cl], 1-butyl-3-methylimidazolium bromide [BMIM][Br], 1-methyl-3-(3-sulfopropyl)-benzimidazolium dihydrogenphosphate, [C.sub.3SO.sub.3HBenzMIM][H.sub.2PO.sub.4], 3-sulfopropyl-P,P,P-triphenylphosphonium hydrogensulfate [C.sub.3SO.sub.3H(C.sub.6H.sub.5)P][HSO.sub.4], N,N,N-triethyl-3-sulfopropanaminium hydrogen sulphate, [C.sub.3SO.sub.3H(C.sub.2).sub.3N][HSO.sub.4]; N,N,N-triethyl-3-sulfopropanaminium p-toluenesulfonate, [C.sub.3SO.sub.3H(C.sub.2).sub.3N][PTS]; N,N,N-triethyl-3-sulfopropanaminium chloride, [C.sub.3SO.sub.3H(C.sub.2).sub.3N][Cl] and N,N,N-triethyl-3-sulfopropanaminium dihydrogenphosphate, [C.sub.3SO.sub.3H(C.sub.2).sub.3N][H.sub.2PO.sub.4], and wherein polymer to catalyst ratio is in the range of 20.0:0.01-20: 10.0, in an ethylene glycol: dioxane solvent mixture, wherein ethylene glycol: dioxane ratio is in the range of 1.0: 0.01 - 1.0: 5.0 (v/v), at a temperature in the range of 120-250° C. for a period in the range of 0.5 to 24 hr; [0074] b) adding water and diethyl ether into the reaction mixture obtained at step a) after completion of the reaction; [0075] c) washing ether layer obtained at step b) with aqueous NaOH solution; [0076] d) acidifying aqueous layer obtained at step c) to afford valorized product with 100% polymer conversion.

[0077] In an embodiment of the present disclosure, there is provided a process for the depolymerization of polymers, wherein the polymer is selected from the group comprising of polyethylene terephthalate (PET), polyethylene furanoate (PEF), Polylactic acid (PLA), polycarbonate, polyethers, and polyamide, and wherein the process comprises the steps of: [0078] a) heating the reaction mixture of polymer and the acidic ionic liquid (AIL) catalyst, wherein said acidic ionic liquid (AIL) is 1-methyl-3-(3-sulfopropyl)-imidazolium hydrogensulfate, [C.sub.3SO.sub.3HMIM][HSO.sub.4] is used as a catalyst, and wherein polymer to catalyst ratio is in the range of 20.0:0.01-20: 10.0, in an ethylene glycol: dioxane solvent mixture, wherein ethylene glycol: dioxane ratio is in the range of 1.0: 0.01 - 1.0: 5.0 (v/v), at a temperature in the range of 120-250° C. for a period in the range of 0.5 to 24 hour; [0079] b) adding water and diethyl ether into the reaction mixture obtained at step a) after completion of the reaction; [0080] c) washing ether layer obtained at step b) with aqueous NaOH solution; and [0081] d) acidifying the aqueous layer obtained at step c) to afford valorized product with 100% polymer conversion.

[0082] In an embodiment of the present disclosure, there is provided a process for the depolymerization of polymers, wherein the polymer is selected from the group comprising of polyethylene terephthalate (PET), polyethylene furanoate (PEF), Polylactic acid (PLA), polycarbonate, polyethers, and polyamide, and wherein the process comprises the steps of: [0083] a) heating the reaction mixture of polymer and the acidic ionic liquid (AIL) catalyst, wherein said acidic ionic liquid (AIL) is 1-methyl-3-(3-sulfopropyl)-imidazolium hydrogensulfate, [C.sub.3SO.sub.3HMIM][HSO.sub.4] is used as a catalyst, and wherein polymer to catalyst ratio is in the range of 20.0:0.50-20:5.0, in an ethylene glycol: dioxane solvent mixture, wherein ethylene glycol: dioxane ratio is in the range of 1.0: 0.50 - 1.0: 1.0 (v/v), at a temperature in the range of 170-200° C. for a period in the range of 3 to 7 hours; [0084] b) adding water and diethyl ether into the reaction mixture obtained at step a) after completion of the reaction; [0085] c) washing ether layer obtained at step b) with aqueous NaOH solution; and [0086] d) acidifying the aqueous layer obtained at step c) to afford valorized product with 100% polymer conversion.

[0087] In an embodiment of the present disclosure, there is provided a process for the depolymerization of polymers, wherein the polymer is polyethylene terephthalate (PET), and wherein the process comprises the steps of: [0088] a) heating the reaction mixture of polymer and the acidic ionic liquid (AIL) catalyst, wherein said acidic ionic liquid (AIL) is 1-methyl-3-(3-sulfopropyl)-imidazolium hydrogensulfate, [C.sub.3SO.sub.3HMIM][HSO.sub.4] is used as a catalyst, and wherein polymer to catalyst ratio is in the range of 16.25: 1.0, in an ethylene glycol: dioxane solvent mixture, wherein ethylene glycol: dioxane ratio is in the range of 1.0: 2.5 (v/v), at a temperature of 180° C. for a period of 6 hours; [0089] b) adding water and diethyl ether into the reaction mixture obtained at step a) after completion of the reaction; [0090] c) washing ether layer obtained at step b) with aqueous NaOH solution; and [0091] d) acidifying the aqueous layer obtained at step c) to afford valorized product with 100% polymer conversion.

[0092] In an embodiment of the present disclosure, there is provided a process for the depolymerization of polymers , wherein the solvent mixture is selected from the list of polar and non-polar solvents with polarity index ranging from 10.2 to 0.1. In another embodiment of the present disclosure, there is provided a process for the depolymerization of polymers , wherein the polar solvent is selected from water, ammonia, sulfuric acid, deuterium oxide, ethanol, methanol, dioxane, acetone, isopropanol, methyl ethyl ketone, n-propanol, acetonitrile, ethylene glycol, DMSO, and DMF and non-polar solvent is selected from chloroform, pentane, hexane, benzene, toluene, octane, decane, dimethyl ether, and dichloromethane. In particular embodiment of the present disclosure, there is provided a process for the depolymerization of polymers , wherein the solvent mixture of ethylene glycol and 1,4-dioxane is used.

[0093] In an embodiment of the present disclosure, there is provided a process for the depolymerization of polymers , wherein the ratio of ethylene glycol to dioxane is in the range of 1.0:0.01 - 1.0:5.0 (v/v). In particular embodiment of the present disclosure, there is provided a process for the depolymerization of polymers, wherein the ethylene glycol to dioxane solvent volume ratio is 1.0: 0.25 (v/v).

[0094] In an embodiment of the present disclosure, there is provided a process for the depolymerization of polymers, wherein the mole ratio of polymer to catalyst is in the range of 20.0:0.01-20.0:10.0. In particular embodiment of the present disclosure, there is provided a process for the depolymerization of polymers, wherein the polymer to catalyst mole ratio is 16.25:1.0.

[0095] The process for the depolymerisation of polyethylene terephthalate, polycarbonate and polylactic acid into corresponding valorized products is depicted below in scheme-1; a)

##STR00005##

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[0096] Several experiments have been conducted to decide the reaction parameters and reagent ratios to obtain maximum yield and purity of the product terephthalic acid from polyethylene terephthalate (PET) as a representative process. Table 1 summarizes the results obtained by using different ionic liquid catalyst, which show that almost all used IL’s can depolymerize PET into larger or smaller extent. Among the ionic liquid catalysts used, [C.sub.3SO.sub.3HMIM][HSO.sub.4] have shown a maximum of 98% yield with 100% PET conversion.

TABLE-US-00001 Sr. No Catalyst Temp. (°C) Time (h) TA Yield (%) PET conversion (%) TA Selectivity (%) 1 Without catalyst 180 6 0 0 0 2 [C.sub.3SO.sub.3HMIM][HSO.sub.4] 180 6 98.6 100 98.6 3 [C.sub.3SO.sub.3HMIM][PTS] 180 6 53.3 88.1 60.5 4 [C.sub.3SO.sub.3HMIM] [H.sub.2PO.sub.4] 180 6 65.8 67.6 97.3 5 [C.sub.3SO.sub.3HMIM][Cl] 180 6 21.8 32.2 67.7 6 [C.sub.3SO.sub.3HMIM] [CuCl.sub.3] 180 6 78.0 100 78.0 7 [C.sub.3SO.sub.3HMIM] [FeCl.sub.4] 180 6 72.3 96.7 74.7 8 [C.sub.3SO.sub.3HMIM] [SnCl.sub.3] 180 6 32.1 42.1 76.2 9 [BMIM] [Cl] 180 6 05.2 07.2 72.2 10 [BMIM] [Br] 180 6 07.7 08.0 96.2 11 [C.sub.3SO.sub.3HBenzMIM] [H.sub.2P O.sub.4] 180 6 55.2 62.1 88.8 12 [C.sub.3SO.sub.3H(C.sub.6H.sub.5)P] [HSO.sub.4] 180 6 41.8 45.0 92.8 13 [C.sub.3SO.sub.3H(C.sub.2).sub.3N] [H.sub.2PO.sub.4] 180 6 36.4 72.2 50.4 14 [C.sub.3SO.sub.3H(C.sub.2).sub.3N] [HSO.sub.4] 180 6 39.6 100 39.6 15 [C.sub.3SO.sub.3H(C.sub.2).sub.3N][PTS] 180 6 24.3 87.9 27.6 16 [C.sub.3SO.sub.3H(C.sub.2).sub.3N] [Cl] 180 6 22.6 36.8 61.4 *Reaction condition: PET (0.5 g), catalyst (0.05 g), solvent (EG: dioxane = 2: 0.5 v/v mL)

[0097] Several experiments have been conducted to analyze effect of reaction time on the conversion and yield of the reaction. The data is summarized below in Table 2. Results show that with [C.sub.3SO.sub.3HMIM][HSO.sub.4] catalyst, PET depolymerisation reaction gives a maximum terephthalic acid yield of 98.6% after 6 h of reaction with 100 % PET conversion and 98.6% selectivity.

TABLE-US-00002 Sr. No Catalyst Temp. (°C) Time (h) TA Yield (%) PET conversion (%) TA Selectivity (%) 1 [C.sub.3SO.sub.3HMIM] [HSO.sub.4] 180 0.5 2.0 2.2 90.9 2 [C.sub.3SO.sub.3HMIM] [HSO.sub.4] 180 2 3.1 3.2 97.0 3 [C.sub.3SO.sub.3HMIM] [HSO.sub.4] 180 4 52.5 57.1 92.0 4 [C.sub.3SO.sub.3HMIM] [HSO.sub.4] 180 6 98.6 100 98.6 5 [C.sub.3SO.sub.3HMIM] [HSO.sub.4] 180 12 96.9 100 96.9 6 [C.sub.3SO.sub.3HMIM] [HSO.sub.4] 180 24 96.7 100 96.7 *Reaction condition: PET (0.5 g), catalyst:[C.sub.3SO.sub.3HMIM][HSO.sub.4] (0.05 g), solvent (EG: dioxane = 2:0.5 v/v mL)

[0098] Several experiments have been conducted to study the effect of temperature on the PET depolymerisation reaction. The data is summarized below in Table 3, which shows that maximum yield of TA is obtained at 180° C.

TABLE-US-00003 Sr. No. Catalyst Temp (°C) Time (h) TA Yield (%) PET conversion (%) TA Selectivity (%) 1 [C.sub.3SO.sub.3HMIM][HSO.sub.4] 120 6 15.1 17.2 87.7 2 [C.sub.3SO.sub.3HMIM][HSO.sub.4] 150 6 75.0 78.0 96.1 3 [C.sub.3SO.sub.3HMIM][HSO.sub.4] 180 6 98.6 100 98.6 4 [C.sub.3SO.sub.3HMIM][HSO.sub.4] 200 6 92.3 100 92.3 5 [C.sub.3SO.sub.3HMIM][HSO.sub.4] 220 6 91.5 100 91.5 6 [C.sub.3SO.sub.3HMIM][HSO.sub.4] 250 6 89.7 100 89.7 *Reaction condition: PET (0.5 g), catalyst- [C.sub.3SO.sub.3HMIM][HSO.sub.4] (0.05 g), solvent (EG: dioxane = 2: 0.5 v/v mL)

[0099] The data of several experiments conducted with different catalyst concentration is summarized below in Table 4, which show that the minimum catalytic concentration at which maximum yield and selectivity of terephthalic acid obtained is 0.05 g (1.6 ×10.sup.-4 mol). (at molar ratio of PET:catalyst= 16.25: 1).

TABLE-US-00004 Sr. No. Catalyst conc (g) Temp. (°C) Time (h) TA Yield (%) PET conversion (%) TA Selectivity (%) 1 0.01 180 6 2.3 4.5 52.3 2 0.05 180 6 98.6 100 98.6 3 0.10 180 6 90.6 100 90.6 4 0.25 180 6 68.5 100 68.5 5 0.50 180 6 43.9 100 43.9 *Reaction condition: PET (0.5 g), catalyst- [C.sub.3SO.sub.3HMIM][HSO.sub.4], solvent (EG: dioxane = 2: 0.5 v/v mL)

[0100] The catalyst is water soluble and hence can be easily recovered in its pure form from the reaction mixture during the work-up. Experiments have been conducted by using recycling the catalyst to check the recycling capacity of the catalyst. The as summarized below in Table 5 shows that the acidic ionic liquid catalyst, [C.sub.3SO.sub.3HMIM][HSO.sub.4] is highly efficient and active even after the reaction and even at 6th catalytic cycle also it gives maximum yield of 98.5% of TA.

TABLE-US-00005 Sr. No. Catalytic run (cycle) Temp. (°C) Time (h) TA Yield (%) PET conversion (%) TA Selectivity (%) 1 1 180 6 98.6 100 98.6 2 2 180 6 98.3 100 98.3 3 3 180 6 98.4 100 98.4 4 4 180 6 98.4 100 98.4 5 5 180 6 98.6 100 98.6 6 6 180 6 98.5 100 98.5 *Reaction condition: PET (0.5 g), catalyst- [C.sub.3SO.sub.3HMIM][HSO.sub.4] (0.05 g), solvent (EG: dioxane = 2: 0.5 v/v mL)

[0101] Table 6 and Table 7 show the summarized results of the experiments conducted with different concentration of PET and with different coloured PET, respectively. Results show that at the molar ratio of 16.25: 1, of PET:catalyst, maximum yield of TA is obtained. Table 7 shows that all the coloured PET can be converted into TA with high yields, purity and selectivity.

TABLE-US-00006 Sr. No. PET conc. (g) Temp. (°C) Time (h) TA Yield (%) PET conversion (%) TA Selectivity (%) 1 0.05 180 6 100 100 100 2 0.1 180 6 98.8 100 98.8 3 0.2 180 6 98.8 100 98.8 4 0.5 180 6 98.6 100 98.6 5 1.0 180 6 50.2 98.7 50.8 6 1.5 180 6 11.8 90.2 13.0 7 2.5 180 6 3.4 88.9 3.8 8 3.0 180 6 1.2 82.3 1.4 *Reaction condition: PET, catalyst- [C.sub.3SO.sub.3HMIM][HSO.sub.4] (0.05 g), solvent (EG: dioxane = 2:0.5 v/v mL)

TABLE-US-00007 Sr. No. PET colour Temp. (°C) Time (h) TA Yield (%) PET Conversion (%) TA Selectivity (%) 1 Colourless 180 6 98.6 100 98.6 2 White 180 6 96.5 100 96.5 3 Blue 180 6 93.6 100 93.6 4 Green 180 6 95.7 100 95.7 5 Red 180 6 90.8 100 90.8 6 Orange 180 6 93.9 100 93.9 7 Yellow 180 6 95.4 100 95.4 *Reaction condition: PET (0.5 g), catalyst- [C.sub.3SO.sub.3HMIM][HSO.sub.4] (0.05 g), solvent (EG: dioxane = 2: 0.5 v/v mL)

[0102] Tables 8 and 9 summarize the results of experiments conducted with different solvents and solvent mixtures. Table 8 shows that uni-phase ethylene glycol: dioxane mixture solvent system of ratio 2: 0.5 v/v mL is more active in PET depolymerisation than solvent system with only ethylene glycol. Addition of stipulated amount of dioxane with ethylene glycol increases the extent of PET depolymerisation, resulting in enhanced TA yield and PET conversion. The effect of added dioxane is more prominent during the course of reaction at a time duration from 3 to 5 h. Table 9 show that uni-phase mixture solvent systems with active AIL catalyst are efficient in depolymerisation of PET to a larger or smaller extent. Ethylene glycol: dioxane mixture solvent system of ratio 2: 0.5 v/v mL is more active in PET depolymerisation than any other solvent systems. Addition of specific amount of dioxane with ethylene glycol solvent results an increase in PET conversion and TA yields.

TABLE-US-00008 Sr. No. Solvent system Temp. (°C) Time (h) TA Yield (%) PET conversion (%) TA Selectivity (%) 1 Ethylene glycol (2 mL) 180 1 0.92 1.12 82.1 2 180 2 2.7 2.9 93.1 3 180 3 22.6 28.3 79.8 4 180 4 39.6 50.5 78.4 5 180 5 73.6 80.2 91.7 6 180 6 92.3 96.1 96.0 7 EG+dioxane (2:0.5 v/v mL) 180 1 0.89 1.08 82.4 8 180 2 3.1 3.2 97.0 9 180 3 36.8 39.2 93.8 10 180 4 52.5 57.1 92.0 11 180 5 85.6 90.2 94.9 12 180 6 98.6 100 96.9 *Reaction condition: PET (0.5 g), catalyst [C.sub.3SO.sub.3HMIM][HSO.sub.4] (0.05 g)

TABLE-US-00009 Sr. No. Solvent (mL) Temp. (oC) Time* (h) TA Yield (%) PET conversion (%) TA Selectivity (%) 1 Water 180 4 3.1 5.3 59.5 2 Ethylene glycol 180 4 39.6 50.5 78.4 3 1,4-dioxane 180 4 26.3 35.1 74.8 4 Water+EG (2:2 v/v) 180 4 11.4 27.7 41.0 5 Water+dioxane (2:2 v/v) 180 4 13.6 20.4 66.9 6 Water+EG+ dioxane (2:2:0.5 v/v) 180 4 11.4 17.4 65.5 7 Water+EG+ Dioxane (1:1:1 v/v) 180 4 42.1 53.8 78.4 8 EG+dioxane (2:0.5 v/v) 180 4 52.5 57.1 92.0 9 EG+dioxane (2:1 v/v) 180 4 46.6 54.5 85.5 10 EG +dioxane (1:1 v/v) 180 4 42.5 52.0 81.7 *Reaction condition: PET (0.5 g), catalyst- [C.sub.3SO.sub.3HMIM][HSO.sub.4] (0.05 g). * To know the real effect of different solvent systems on the PET depolymerisation, all the reactions are quenched after a time duration of 4 h.

[0103] Table 10 summarizes the results of the experiments conducted with mixture of different polymers with polyethylene terephthalate (PET). The data shows that PET depolymerisation into pure terephthalic acid is possible selectively from a mixture of plastics. 100% solubility PET in the plastic mixture is also possible with the efficient catalytic-solvent system under optimum reaction conditions.

TABLE-US-00010 Sr. No. Substrate Temp. (°C) Time (h) TA Yield (%) PET conversion (%) TA Selectivity (%) 1 Only PET (0.5 g) 180 6 98.6 100 98.6 2 PET+PVC (0.25:0.25 g/g) 180 6 58.2 100 58.2 3 PET+ Polycarbonate (0.25:0.25 g/g) 180 6 62.4 100 62.4 4 PET+PP (0.25:0.25 g/g) 180 6 76.5 100 76.5 5 PET+ HDPE (0.25:0.25 g/g) 180 6 61.5 100 61.5 6 PET+ LDPE (0.25:0.25 g/g) 180 6 75.3 100 75.3 7 PET+ Polystyrene (0.25:0.25 g/g) 180 6 84.6 100 84.6 *Reaction condition: Substrate (0.5 g), catalyst- [C.sub.3SO.sub.3HMIM][HSO.sub.4] (0.05 g), solvent (EG: dioxane =2: 0.5 v/v mL)

[0104] Table 11 below summarizes the results for depolymerization of various polymers using AIL.

TABLE-US-00011 Sr. No. Substrate Temp. (°C) Time (h) Monomer Yield (%) Polymer conversion (%) Monomer Selectivity (%) 1 PET 180 6 98.6 100 98.6 2 Polycarbonate 180 6 51.0 100 51.0 3 Polylactic acid 180 6 20.1 100 20.1 4 Polyamide 180 6 38.4 100 38.4 *Reaction condition: Substrate (0.5 g), catalyst- [C.sub.3SO.sub.3HMIM][HSO.sub.4] (0.05 g), solvent (EG: dioxane =2: 0.5 v/v mL)

General Information

[0105] CHNS: Elemental analysis were done in Thermo Finnign, Ilaly, model EA1112 series Flash Elemental Analyzer. This analyzer measures the amount of C,H,N and S in the sample by rapid combustion of small amounts (1-2 mg) of the sample in pure O.sub.2 (Dumas method or flash combustion) The analysis of all elements in the CHNS group was performed simultaneously.

[0106] .sup.1HNMR: Liquid .sup.1HNMR of the sample and the standard product were recorded on Bruker Duel 200 MHz at 25° C. using DMSO-d.sub.6 as solvent with TMS as the internal standard. The sample consists of 20 mg of product dissolved in 0.7 mL DMSO-d.sub.6. No. of scans used were 4.

[0107] XRD: Powder X-Ray diffraction patterns were recorded on a Rigaku Miniflex diffractometer using Ni-filtered monochromatic Cu K.sub.a radiation (λ= 1.5406 A°). The samples were prepares as a thin film on a glass XRD plate and were scanned between a 2θ range of 5 and 90 ° at the scan rate of 2 °/min.

[0108] HPLC: Obtained TA and standard TA were analyzed using Agilent make High Performance Liquid Chromatography (HPLC, 1260 Infinity series) system equipped with autosampler, Rezex ROR-Organic Acid H.sup.+ column (300 mm length x 7.8 mm i.d, 30° C.) and Refractive Index (RI) detector (40° C.). 5 mM H.sub.2SO.sub.4 was used as a mobile phase with a flow rate of 0.6 mL/min. The samples were prepared as 0.025 wt%sodium salt (sodium terephthalate) solution in Millipore water.

EXAMPLES

[0109] Following examples are given by way of illustration and therefore should not be construed to limit the scope of the invention.

[0110] By using the work-up procedure based on the product solubility in water medium at different temperature as reported by Hui Wang et al. in J. Eurpolymj., 2009; (45), 1535-1544, the Bis(2-Hydroxyethyl) terephthalate (BHET) monomer is obtained as main PET depolymerisation product.

Example 1: General Process for the Depolymerisation of Polymers

[0111] In a Teflon autoclave 0.5 g polymer, solvent (EG: dioxane in 2:0.5 v/v= mL ratio) and 0.05 g of the AIL catalyst (16.25: 1 mol ratio of polymer:catalyst)) were added and heated at a temperature of 180° C. for a period of 6 hours, without stirring. After the completion of the reaction, 40 mL water and 40 mL diethyl ether were added into the obtained mixture. Then the ether layer was separated and washed several times with 60 mL of 5 wt% aqueous NaOH solution. Further, the aqueous layer was separated and acidified with 10 mL Conc. HC1 (pH≈ 2) to afford pure corresponding valorized product. Product obtained is then washed with 50 mL distilled water, filtered under vacuum and dried at 60° C. overnight.

TABLE-US-00012 HPLC data for depolymerisation of polyethylene terephthalate (PET) Sample Retention Time Area Standard (TA) 23.645 380374 TA by above process 23.674 441251

ADVANTAGES OF THE INVENTION

[0112] Depolymerisation of PET into terephthalic acid with a newer methodology (Glycolysis-hydrolysis reaction) using mild reaction conditions.

[0113] Depolymerization of Polycarbonate, Polyethylene furanoate, Polylactic acid, Polyethylene naphthalate, and Polyamide was done.

[0114] Utilisation of Acidic Ionic Liquid (AIL) as a homogeneous catalyst. In particular we have used Brønsted acidic ionic liquid (BAIL).

[0115] 100% PET conversion with 98.6 % yield of terephthalic acid by using AIL catalyst under optimum reaction conditions.

[0116] 100% conversion of all polymers was achieved with monomer formation using AIL catalyst under optimum reaction conditions.

[0117] Extra pure product in high yields compared with other methods of depolymerisation.

[0118] 100% solubilisation of PET under optimum reaction conditions even in the absence of stirring.

[0119] Utilisation of water soluble, biodegradable, easily recoverable and recyclable catalyst.

[0120] Cheap, easily available and recoverable solvent system.

[0121] Depolymerisation of coloured PET into pure white terephthalic acid in high yields.

[0122] Selective PET depolymerisation, even in mixture of plastics.