FIELD OF THE DISCLOSURE

[0001] .This disclosure relates to the depolymerization of polymeric waste materials. More specifically, this disclosure relates to a process for directly converting polymeric waste material into olefins via a depolymerization reaction.

BACKGROUND OF THE DISCLOSURE

[0002] .Plastics include a wide range of synthetic and semi-synthetic materials that use polymers as their main ingredient. Their plasticity makes it possible for plastics to be molded, extruded or pressed into solid objects of various shapes. This adaptability, in combination with a wide range of other properties, such as light weight, durability and low production cost, has led to their widespread use. The production of plastics has increased dramatically over the last few decades. At the same time, the increasing amount of plastics give rise to environmental concerns as most plastics are resistant to natural degradation processes. As such, the material may persist for centuries or longer, filling up landfill sites and even appearing in the food chain as microplastics.

[0003] .Therefore, increasing efforts are undertaken to improve the recycling of polymeric waste materials. The current procedures of recycling primarily rely on mechanical recycling and chemical recycling. For mechanical recycling, the plastics are mechanically transformed without changing their chemical structure so that they can be used to produce new materials. Typical mechanical recycling steps include collecting polymeric waste material, sorting the polymeric waste material into different types of plastic and colors, packaging the plastic waste material by pressing or milling, washing and drying the polymeric waste material and reprocessing the polymeric waste material into pellets by agglutinating, extruding and cooling the plastic to obtain the recycled raw material which can then be formed into new articles.

[0004]. During chemical recycling, the plastics are re-processed, and their structure and chemical nature modified so that they can be used as raw materials for different industries or as basic input or feedstock for manufacturing new polymeric products. Chemical recycling typically includes the steps of collecting plastic waste material, followed by heating the plastic waste material to break down the polymers to obtain smaller organic molecules which are then recirculated in the petrochemical industry.

[0005]. Typically, the main effluent from the pyrolysis step is a liquid stream, also called pyrolytic oil, which can be either refined and used as a fuel or subject to a further steam cracking step to generate a gaseous fraction composed by C2-C4 olefins.

[0006]. The pyrolysis stage can be carried out in the presence of a catalyst which helps in facilitating the hydrocarbon chain breakdown. However, use of the catalyst has also several drawbacks. In particular, although the overall yield in depolymerization product may increase, the composition of the gaseous depolymerization product can result in a too high content of oxygenated products such as CO and CO2. These oxygenated gases prevent the gaseous depolymerization product containing olefins to be directly fed to the cracker backend separation section and need to be removed beforehand. Moreover, the generation of CO2 partially jeopardize the attempt to reduce CO2 footprint of plastic waste handling. In addition, the use of a catalyst in the depolymerization, also increase the costs and make the process more complex as devices for catalyst handling and feeding have to be added to the plant design.

[0007]. It would therefore be important to develop a pure thermal process for the direct conversion of plastic waste into olefins generating a low amount of CO and CO2 gases. SUMMARY OF THE DISCLOSURE

[0008]. In one aspect, the present disclosure provides a process for the conversion of plastic waste into olefin comprising:

[0009].- depolymerizing at a temperature ranging from 480 to 700°C, a plastic waste feedstock comprising more than 80% wt of polyolefins based on the polymeric content of the plastic waste feedstock;

[00010]. - collecting the gaseous fraction generated during pyrolysis and

[00011]. - separating the collected gaseous fraction to obtain a gaseous and a liquid depolymerization product in which the amount of gaseous depolymerization product is higher than 40%wt base on total polyolefin content, and provided that in the said gaseous depolymerization product the amount of C2-C4 olefins is equal to or higher than 50%wt based on the total amount of hydrocarbons.

DETAILED DESCRIPTION OF THE DISCLOSURE

[00012]. Preferably the plastic waste feedstock is characterized by: (a) a polyolefin content, in particular a total content of polypropylene (PP) and polyethylene (PE) of more than 85 wt.%, more preferably more than 90 wt.%, especially more than 95 wt.% based on the total weight of the polymeric waste material feedstock.

[00013]. Preferably, the upper limit of polyolefin content is 99 wt%, more preferably 98 wt% and especially 97 wt% based on the total amount of plastic waste feedstock.

[00014]. It is also a preferred embodiment that the weight ratio PE/PP in the polymeric waste material feedstock be equal to or higher than 3.5, more preferably equal to or higher than 5, and especially equal to or higher than 6. [00015]. Furthermore, the total ash content of the plastic waste feedstock is preferably less than 10 wt.%, more preferably less than 5 wt.%, and most preferably less than 3 wt.%, determined as residue after heating the polymeric waste material feedstock at 800 °C for 120 hours in air.

Preferably, the plastic waste feedstock is also characterized by (i) a bulk density from 70 to 500 g/1, preferably from 100 to 450 g/1 for cases in which the polymeric waste material feedstock is present in shredded form or a bulk density from 300 to 700 g/1 for cases in which the polymeric waste material feedstock is in pellet form, the bulk density being determined according to DIN 53466, respectively. It has been found that the above mentioned value of bulk density greatly helps to achieve a continue flowless depolymerization process and to prevent blockage of feeding lines and reactor fouling. Furthermore, it also helps to obtain low amounts of residues and an enhanced depolymerization reaction increasing the yield of desired products. Preferably, the polymeric waste material is obtained from a shredded pipe with a particle size of <50mm, preferably <30mm, more preferably <20mm and most preferably <15mm.

[00016]. In a preferred embodiment, the plastic waste feedstock is additionally characterized by: (i) a content of total volatiles (TV), measured as the weight loss of a 10 g sample at 100°C after 2 hours at 200 mbar, of less than 4%, preferably less than 3%.

[00017].

[00018]. In addition to the polyolefin components mentioned above, the polymeric waste material feedstock employed in the process of the present disclosure may include essentially all polymeric materials, in particular those materials formed from synthetic polymers. Non-limiting examples include polyolefins other than PE and PP, such as polybutene- 1 and ethylene- propylene elastomers etc., polystyrene, polyethylene terephthalate (PET), polyvinyl chloride (PVC), polyamide, polycarbonate, polyurethane, polyester, natural and synthetic rubber, tires, filled polymers, composites and plastic alloys, plastics dissolved in a solvent, etc.

[00019]. However, according to the present disclosure which aims at maximizing the production of light gas olefins, the plastic feedstock preferably consists primarily of polyolefins and the non-polyolefin polymeric materials may be present only in an amount lower than 10%, preferably lower than 5% based on the total amount of plastic waste feedstock.

[00020]. As mentioned above, the polymeric waste material feedstock can be composed of one type of polyolefin waste material or may be a mixture of two or more different polymeric waste materials. The embodiment in which the polyolefin waste material is composed entirely by polyethylene (PE) is particularly preferred.

[00021]. The polymeric waste material feedstock may be provided in a variety of different forms. In smaller scale operations, the polymeric waste material feedstock may be in the form of a powder. In larger scale operations, the polymeric waste material feedstock may be in the form of pellets, such as those having a particle size from 1 to 20 mm, preferably from 2 to 10 mm, and more preferably from 2 to 8 mm, or in form of shredded flakes and/or small pieces of film, preferably having a particle size from 1 to 20 mm. In the context of the present disclosure, having a particles size in a defined range means that 90 wt.% of the particles have a particle size which is in the defined range. The particle size may be determined by sieving or by using a Beckman Coulters LSI 3320 laser diffraction particle size analyzer.

[00022]. The plastic waste material disclosed above mostly consists of plastic material and is generally named after the type of polymer which forms the predominant component of the polymeric waste material. Preferably, the plastic waste material employed as feedstock in the process of the present disclosure contains more than 50 wt.% of its total weight of the polymeric material, preferably more than 6 wt.% and more preferably more than 70 wt.%. Other components in the polymeric waste material feedstock may, for example, be additives, such as fillers, reinforcing materials, processing aids, plasticizers, pigments, light stabilizers, lubricants, impact modifiers, antistatic agents, inks, antioxidants, etc.

[00023]. In a specific embodiment, the polymeric waste materials used in the process of the present disclosure preferably comprises polyolefins and polystyrene, such as high-density polyethylene (HDPE), linear low-density polyethylene (LLDPE), low-density polyethylene (LDPE), ethylene-propylene-diene monomer (EPDM), polypropylene (PP), and polystyrene (PS). Particularly preferred are polymeric waste materials comprising a mixture of polyolefins and polystyrene.

[00024]. Other non-polyolefin polymeric waste materials, such as polyamide, polyvinyl chloride, polyvinylidene chloride, polyethylene terephthalate, polyurethane (PU), acrylonitrile- butadiene-styrene (ABS), nylon and fluorinated polymers can also be employed in the process of the present disclosure. If present in the polymeric waste material, those polymers are preferably present in an amount of less than 10% and especially less than 5% of the total weight of the dry weight polymeric waste material feedstock.

[00025]. Preferably, the polymeric waste material comprises is essentially free of thermosetting polymers. Essentially free in this regard is intended to denote a content of thermosetting polymers of less than 10 wt.% and even more preferably less than 5 wt.% of the polymeric waste material feedstock.

[00026]. The polymeric waste materials used in the process of the present disclosure are preferably selected from the group consisting of single plastic waste, mixed plastics waste, rubber waste. Single plastic waste, single virgin plastic off spec, mixed plastics waste, rubber waste or a mixture thereof are preferred. Single virgin plastic off-spec, mixed plastics waste or a mixture thereof are particularly preferred.

[00027]. The polymeric waste material may also contain limited quantities of non- pyrolysable components such as water, glass, stone, metal and the like as contaminants. "Limited quantities" preferably mean an amount of less than 15 wt.%, and more preferably less than 10 wt.% of the total weight of the dry polymeric waste material feedstock.

[00028]. The polymeric waste material can optionally be extruded prior to being employed as feedstock in the process of the present disclosure. In preferred embodiments, the polymeric waste material is pelletized, and the pellets are employed as feedstock in the process of the present disclosure. In other preferred embodiments, the polymeric waste material is employed in a molten state, for example at temperatures from 200°C to 300°C.

[00029]. A particularly preferred type of polymeric waste material employed as feedstock in the process of the present disclosure is characterized by the following features:

[00030] . i) A polyolefin content, in particular the content of polypropylene (PP) and/or polyethylene (PE) in the polymeric waste material of more than 80 wt.%, preferably more than 85 wt.%, and more preferably more than 90 wt.%, especially more than 95 wt.% based on the total weight of the polymeric waste material feedstock;

[00031]. ii) The polymeric waste material is a shredded and optionally compacted polymeric waste material having a bulk density from 70 to 500 g/1, preferably from 100 to 450 g/1 or the polymeric waste material is in pellet form and has a bulk density from 300 to 700 g/1, the bulk density being determined according to DIN 53466; [00032]. iii) A total content of volatiles (TV), measured as the weight loss of a 10 g sample at 100 °C and a pressure of 200 mbar after 2 hours of less than 5%, preferably less than 3%, and more preferably less than 2%, especially less than 1%;

[00033]. iv) An amount of polar polymer contaminants in the polymeric waste material of less than 5 wt.%, and more preferably less than 3 wt.%, based on the total weight of the polymeric waste material;

[00034] . v) An amount of cellulose, wood and/or paper in the polymeric waste material of less than 5 wt.%, and more preferably less than 3%, based on the total weight of the polymeric waste material;

[00035]. vi) A total chlorine content of less than 1.0 wt.%, preferably less than 0.5 wt.%, more preferably less than 0.1 wt.%, based on the total weight of the polymeric waste material;

[00036]. vii) A total ash content of the polymeric waste material feedstock of less than

10 wt.%, more preferably less than 5 wt.%, and most preferably less than 3 wt.%, determined as residue after heating the polymeric waste at 800°C for 120 hours in air. In other preferred embodiments, the ash content is from 0.01 to 2 wt.%, preferred from 0.02 to 1.5 wt.%, and more preferred from 0.05 to 1.0 wt.%.

[00037]. In a preferred embodiment of the present disclosure, the polymeric waste materials employed as feedstock in the process of the present disclosure is defined by upper limits of minor components, constituents or impurities expressed as percent by weight. The lower limits for the amounts of these components, constituents or impurities in the preferred polymeric waste materials are preferably below the detection limit, or the lower limits are 0.001 wt.% or 0.01 wt.% or 0.1 wt.%, respectively. [00038]. A variety of techniques are known to separate materials in a polymeric waste stream. Moving beds, drums and screens, and air separators are used to differentiate materials by size, weight and density. Advanced sorting of plastic waste by spectroscopy techniques (MIR, NIR [near- infrared]), X-ray or fluorescence spectroscopy deliver high quality plastic waste streams with high polyolefin content.

[00039]. Automatic Separation Techniques of waste plastics comprise dry sorting technique, electrostatic sorting technique, mechanical sorting method (involves centrifugal force, specific gravity, elasticity, particle shape, selective shredding and mechanical properties) as well as wet sorting technique (e.g. sink float sorting method) and chemical sorting methods.

[00040]. A suitable feedstock to be employed in the process of the present disclosure may be obtained by applying any of the known sorting techniques, as e.g. summarized in B. Ruj et al: Sorting of plastic waste for effective recycling, Int. J. Appl. Sci. Eng. Res 4, 2015, 564-571.

[00041]. Depolymerization

[00042]. According to the present disclosure the process for the depolymerization of plastic waste material, comprising pyrolyzing the plastic waste material at a temperature ranging from 480 to 700°C, preferably from 500 to 650°C, more preferably from 500 to 600°C and especially from 500 to 580°C.

[00043]. The gaseous effluent from the pyrolysis reactor is then (a) collected and (b) separated into a gaseous and a liquid depolymerization product.

[00044]. The collected gaseous fractions may be separated into liquid and gaseous depolymerization products by condensation. Thus, the liquid depolymerization product and the gaseous depolymerization product may be further processed. [00045]. The process of the present disclosure may generate little to no char. Therefore, in preferred embodiments, the residue of the depolymerization process of the present disclosure has a char content of less than 5 wt.%, preferably less than 2 wt.%, based on the total weight of the product.

[00046]. The obtained liquid depolymerization product may be further separated. Therefore, the process of the present disclosure may further comprise a step of distilling the liquid depolymerization product.

[00047]. The process of the present disclosure yields a depolymerization product with a high gaseous content. In a preferred embodiment, the gaseous content in the depolymerization product is preferably more than 45 wt.%, more preferably more than 50 wt.% and especially more than 65 wt.%, based on the initial total weight of polyolefin in the plastic waste feed.

[00048]. Moreover, the gaseous fraction of the depolymerization product is further distinguished by high content of monomeric olefinic C2-C4-compounds which are especially useful for further processing, e.g. for the production of polymers. In particular, the amount of olefinic C2- C4-compounds is equal to or higher than 55% and preferably higher than 60% and especially higher than 65% based on the total amount of hydrocarbons.

[00049]. In a specific embodiment, the percentage of ethylene on the total of olefinic C2-C4- compounds, is higher than 28%wt and preferably higher than 30%wt.

[00050]. Moreover, the amount of C2-C4 hydrocarbons in the gaseous fraction of the depolymerization product is preferably higher than 80% preferably higher than 85% and especially higher than 90% based on the total amount of hydrocarbons. Due to the high amount of such compounds generated during depolymerization, the gaseous depolymerization product may be directly used as feedstock in cracking processes and subsequent polymerization. The gaseous product comprising light olefins and light alkanes can, for example be transferred to a downstream cracker by passing the ovens to produce polymerization grade monomer streams.

[00051]. Other side products such as ethane, propane and butanes can be cracked in the oven. The usually required steps of treating the product obtained after depolymerization to obtain the desired monomers can thus be bypassed, saving valuable energy and reducing CO2 output.

[00052]. The depolymerization process according to the present disclosure can be carried out in a reactor comprising: (a) feeding devices for introducing polymeric waste material and catalyst into the reactor; (b) a pyrolysis device equipped with heating units, gas discharge units and a solid discharge unit; and (c) a condensation device.

[00053]. Preferably, the gas discharge units are distributed throughout the pyrolysis device and are provided with an outlet to discharge the gaseous fraction of the depolymerization and an inlet for introducing cleaning gas into the pyrolysis device.

[00054]. In a preferred embodiment, the reactor may comprise more than one pyrolysis unit. [00055]. The polymeric waste feedstock and, if employed, the catalyst are introduced into the pyrolysis unit via at least one feeding device and then heated to achieve depolymerization. The gaseous fractions generated during depolymerization are discharged through the outlet of the gas discharge units and conveyed to the condensation unit for further processing. Any solid residue of the depolymerization is discharged via the solid discharge unit. Cleaning gas for cleaning the gas discharge units and the pyrolysis unit may be introduced through the inlet of the gas discharge units.

[00056]. In a preferred embodiment, the gas discharge units are equipped with filter membrane to avoid solids to be present in the gaseous fractions after being discharged from the pyrolysis device. The gas discharge units are preferably made of metallic or ceramic grain or fiber materials.

[00057]. The pyrolysis device is preferably further equipped with a screw for homogenously mixing the polymeric waste material in the pyrolysis device throughout the depolymerization. The residence time of the solids in the pyrolysis device could be well-defined by adjusting the rotational speed of the screw.

[00058]. The discharged gaseous fractions of the depolymerization are conveyed to the condensation device to obtain a liquid and a gaseous depolymerization product. In a preferred embodiment, the condensation device comprises several condensers which are preferably operated at different temperatures. The temperatures of the condensers may be set according to the boiling points of the condensates.

[00059] . Depolymerization product

[00060]. The gaseous fractions generated during pyrolysis are separated into liquid and gaseous depolymerization products, e.g. by condensation.

[00061]. The process of the present disclosure yields a depolymerization product of surprising very high selectivity for the gaseous fraction.

[00062] . Liquid depolymerization product

[00063]. The obtained liquid depolymerization product, especially when the run is carried out in the presence of a catalyst, shows a surprisingly low content of aromatic compounds and in particular a surprisingly low content of polycyclic aromatic compounds and asphaltanes. The liquid depolymerization product obtained by the process of the present disclosure is accordingly characterized by a low content of aromatic and olefinic components as well as a high degree of purity. [00064]. Preferably, the content of aromatic compounds in the obtained liquid depolymerization product is less than 10 mol%, preferably less than 5 mol%, and in particular no more than 3 mol%, the content of aromatic components being measured as contents of aromatic protons in mol% as determined by 1H-NMR -spectroscopy.

[00065]. Further, the liquid depolymerization product obtained by the depolymerization process of the present disclosure is characterized by a low content of olefinic compounds. The content of olefinic compounds in the liquid depolymerization product is preferably less than 7 mol%, more preferably less than 5 mol%, even more preferably less than 3 mol%, based on the total number of hydrocarbon protons; the content of olefinic compounds being determined based on the contents of olefinic protons as determined by 1H-NMR -spectroscopy.

[00066]. Another measure for the content of double bonds in a given sample is the Bromine number (BrNo.) which indicates the degree of unsaturation. In preferred embodiments, the liquid depolymerization product obtained by the process of the present disclosure has a Bromine number, expressed as gram bromine per 100 grams of sample, of less than 150, preferably from 10 to 100, more preferably from 15 to 80, even more preferably from 20 to 70 and in particular from 25 to 100, determined according to ASTM D1159-01.

[00067]. The liquid depolymerization product obtained in the process of the present disclosure has preferably a boiling range from 30 to 650°C, more preferably from 50 to 250°C. By separation techniques such as distillation, the depolymerization product may be separated into hydrocarbon fractionations of different boiling ranges, for example a light naphtha fraction mainly containing Cs and Ce hydrocarbons having a boiling range from 30°C and 130°C, a heavy naphtha fraction mainly containing Ce to C12 hydrocarbons having a boiling range from 130°C to 220°C, a kerosene fraction mainly containing C9 to C17 hydrocarbons having a boiling range from 220°C to 270°C or into other high boiling point fractions such as diesel fuel, fuel oil or hydrowax.

[00068]. It was further surprisingly found that the liquid depolymerization product contains little to no solid residue. In preferred embodiments, the content of residues of the liquid depolymerization product upon evaporation, determined according to ASTM D381, is no more than 5 ppm (w).

[00069]. Gaseous depolymerization product

[00070]. The gaseous depolymerization product obtained shows a surprisingly low content of low molecular hydrocarbons such as methane or ethane. Rather, it was surprisingly found that the gaseous depolymerization product contained unusually high amounts of higher olefins such as ethylene, propylene, and butenes which are commonly desired for polyolefin production.

[00071]. As mentioned above, the amount of olefinic C2-C4-compounds is equal to or higher than 55% and preferably higher than 60% and especially higher than 65% based on the total amount of hydrocarbons in the gaseous depolymerization product. Accordingly, the gaseous depolymerization product obtained by the process of the present disclosure is characterized by a high content of any of ethylene, propylene, and butenes and also by a low content of saturated low molecular hydrocarbons, in particular hydrocarbons of the general formula C _n H2n+2 wherein n is a real number ranging from 1 to 4.

[00072]. In a preferred embodiment, the gaseous depolymerization product of the process of the present disclosure is characterized by a content of CO of at most 2 wt.%, preferably at most 1 wt.%, more preferably at most 3 wt.%, most preferably at most 2 wt.%, especially at most 0.1 -0.5 wt.%, based on the total weight of the gaseous depolymerization product after step (e) of the process of the present disclosure. [00073]. In a preferred embodiment, the gaseous depolymerization product of the process of the present disclosure is characterized by a content of CO2 of at most 5 wt.%, preferably at most 3 wt.%, more preferably at most 2 wt.%, based on the total weight of the gaseous depolymerization product after step (e) of the process of the present disclosure

[00074]. In view of the very high olefinic content, the gaseous fraction could thus be directly used as feedstock for further processing in a cracker downstream, e.g. a raw gas compressor to obtain purified monomer streams, and thereafter for the subsequent production of polymers, allowing bypassing the highly energy consuming stream cracking ovens usually required while at the same time reducing the output of CO2.

[00075]. The gaseous depolymerization product may contain small quantities of HC1, HCN, H2S, H2O, NH3, COS etc. which can be optionally separated in a refining step before the introduction to the steam cracker downstream segments.

[00076]. The present disclosure will be explained in more detail with reference to the figures and the examples provided below.

EXAMPLES

[00077]. The following analytical methods were employed:

[00078]. 1) GC MS was used for liquid and gas analysis.

[00079]. 2) Char residue was determined according to mass balance after decoking the residues of the reactor at 800 °C.

[00080]. 3) Liquid contents were characterized using simulated distillation (SimDist) analysis according to ASTM D 7213 : 2012. Final boiling point (FBP), boiling temperature at 50% and initial boiling point (IBP) are taken from SimDist. [00081]. 4) The total content of unsaturated components in the liquid condensates were characterized via Bromine number determination using a 848 Titrino Plus (Metrohm AG, Herisau, Switzerland) equipped with an double PT-wire electrode which has integrated a PT1000 temperature sensor, and a 10 ml buret in accordance with ASTM DI 159-01 as described in Metrohm Application Bulletin 177/5e, December 2018. The Bromine number (BrNo.) represents the amount of bromine in grams absorbed by 100 grams of a sample.

[00082]. 5) 1H-NMR analysis was conducted by dissolving a sample of the liquid condensate in CDC13 and characterizing the sample using proton NMR spectroscopy. Aromatic, olefinic and aliphatic protons were assigned according to the chemical shifts summarized in Table 1:

[00083]. Table 1 - Integral Regions in 1H-NMR spectroscopy

[00084]. The listed types of olefinic protons are assumed to correspond to the following structures:

Type 1 Type 2 Type 3 Type 4

[00085]. The amount of aromatic, olefinic and aliphatic protons may be determined based on the assigned peak integrals according to the following equations:

[00086]. Mol% Aromatic Protons = [(Ii + 12) / (Ii + 12 + 13 + 14 + Is + le + 17+ Is + I9)] %

[00087]. Mol% Olefinic Protons Type 1 = [(I4 + 17) / (Ii + 12 + 13 + 14 + Is + le + 17+ Is + I9)]

%

[00088]. Mol % Olefinic Protons Type 2 = [(I3 + Is) / (Ii + 12 + 13 + 14 + Is + le + 17+ Is + I9)] %

[00089]. Mol % Olefinic Protons Type 3 = [(le) / (Ii + 12 + 13 + 14 + Is + le + 17+ Is + I9)] %

[00090]. Mol % Olefinic Protons Type 4 = [(Is) / (Ii + 12 + 13 + 14 + Is + le + 17+ Is + I9)] %

[00091] . Mol% Paraffinic Protons = [(I9) / (Ii + 12 + 13 + 1 ₄ + 1 ₅ + le + 17+ Is + 19)] %

[00092]. 6) The water content of the catalyst was determined using a Sartorius MA45

(Sartorius AG, Goettingen, Germany) on a sample of 0.5 to 1 g at 180 °C.

[00093] . 7) For the determination of a pH value of the hydrodepolymerization products, by extraction of a liquid sample of the hydrodepolymerization product was extracted with water in a volume ratio water: sample of 1:5 and the pH value of the aqueous solution was measured.

[00094]. 8) Properties of the employed organic waste material feedstock were determined as follows: [00095]. As the composition of the organic waste material may vary, samples from 20 to 100 g of the polymeric waste were milled and analyzed. Alternatively, a pelletized sample of the polymeric waste was analyzed. The following methods are used:

[00096]. i) Total Volatiles (TV) were measured as the weight loss of a 10 g sample at

100 °C and after 2 hours at 200 mbar.

[00097]. ii) Water content was determined by Karl -Fischer titration using an apparatus from Metrohm 915 KF Ti-Touch equipped with a PT100 indicator electrode for volumetric KF titration according to Metrohm Application Bulletin 77/3e in compliance with ASTM E203.

[00098]. iii) IR-Spectroscopy was used for a qualitative identification of various polymers (PP, PE, PS, PA, PET, PU, Polyester) and additives such as CaCCh.

[00099]. iv) Standard elemental analysis was used for determination of wt.% of H, C, N

(DIN 51732: 2014-07) and S (tube furnace, ELTRA GmbH, Haan, Germany, DIN 51724-3: 2012- 07).

[000100]. v) 1H-NMR was used for determining the composition of polymers soluble in solvents adequate for recording a 1H-NMR spectrum: PE/PP balance (copolymers are also included), PET, PS.

[000101]. vi) Ash Content analysis of plastics was determined at 800 °C according to DIN EN ISO 3451-1 (2019-05).

[000102]. vii) Bulk density of the polymer waste was determined according to DIN 53466.

[000103]. viii) Corrosivity was determined as the pH value of an aqueous solution after a contact time of 3 h (5 g sample in 50 ml distilled water)

[000104]. ix) Inductively coupled plasma atomic emission spectroscopy (ICP-AES) was used for quantitative element determination (total chlorine content, content of Si or metals) [000105]. x) The ash content of a liquid feedstock such as pyrolysis oil, is measured according to ASTM D482-19.

[000106]. Feedstock:

[000107]. Some of the following organic waste materials were employed as feedstocks:

[000108]. A: Pelletized agricultural and industrial packaging film.

[000109]. The properties of the feedstocks averaged on analysis of three samples are summarized in Table 2.

[000110]. Table 2:

[000111]. * ) Other content includes inorganic, polymer or organic contaminants and volatile components

[000112]. Ash: ash content

[000113]. TV: total volatiles

[000114]. BD: bulk density

[000115]. Cl: total chlorine content

[000116]. PE: polyethylene content

[000117]. PP: polypropylene content

[000118]. PET: content of polyethylene terephthalate

[000119]. PS: polystyrene content

[000120]. PA: polyamide content [000121]. Other cont. : content of other contaminants

[000122]. The feedstock was introduced into a reactor device equipped with heating units, gas discharge units, solid discharge unit; a condensation device and a screw for homogenously mixing the reactor content (plastic waste and sand) during depolymerization. Conditions of the depolymerization conducted are summarized in Table 6. The obtained gaseous fractions were further separated into liquid and gaseous depolymerization products by condensation. The amounts of the obtained fractions are also given in Table 3.

[000123]. Table 3: Process parameter and mass balance ^(a)

[000124]. ^(a) Amount missing to 100% is due to losses; (b) high amount of waxes flouting in an inhomogeneous liquid

* Liquid is the combination of all fractions, may contain some waxy solid particles and agglomerates which disappear upon heating to >50 °C

[000125]. Run#2 was performed only plastic waste A without using any sand.

[000126]. The above data show that the catalysts of the present disclosure produce high amounts of gaseous depolymerization products and that are able to maintain good performances even when the feedstock is added with heterogeneous material. The results of the analysis of the gaseous depolymerization product are summarized in Table 4.

[000127]. Table 4: mass balance of the gaseous depolymerization product

[000128]. *> Catalyst which was used in three successive runs maintaining good selectivity and then regenerated by heating up to 800 °C in air and sieving out the smaller particles <500 pm (ashes)

[000129]. HC: Hydrocarbons

[000130]. Olefins: sum of ethylene, propylene and butenes

[000131]. Olefins/HC: percentage of all olefins over total hydrocarbons

[000132]. As can be seen from Table 4, the process of the present disclosure yielded gaseous depolymerization products with high amounts of monomers useful as feedstock for polymerization after purification. Any saturated gaseous hydrocarbons can be processed in the usual manner back to the steam cracker ovens.

[000133]. Comparative runs with the polymeric waste material with bulk density of 60 g/cm ³ were also carried out in the same reactor set-up. The runs were impacted repeatedly by blockage of feeding line and reactor fouling which rendered the runs troublesome.