Process for removing odor in recycled polyolefin composition

Abstract

A process for removing odor from a recycled polyolefin composition comprising the step of: a) providing a recycled polyolefin composition; b) mixing the recycled polyolefin composition with from 0.5 wt% to 9.0 wt% with respect to the recycled polyolefin composition, of water c) optionally mixing the results of step b) with at least one odor removal component and d) extruding the mixture; wherein the amount of odor removal component ranges from 0.1 wt% to 10 wt% with respect to the recycled polyolefin composition.

Description

TITLEPROCESS FOR REMOVING ODOR IN RECYCLED POLYOLEFIN COMPOSITIONFIELD OF THE INVENTION

[0001] The present disclosure relates to a process for removing odor in a recycled polypropylene composition by adding odor removal componentsBACKGROUND OF THE INVENTION

[0002] It is known that the demand for plastic packaging is increasing and with it the volume of plastic in landfills. While plastic waste from industries can be treated by mechanical recycling obtaining a reusable high-quality material as polymeric raw material, domestic plastic waste has a high content of food waste and cleaning products that are absorbed into the polymeric matrix, becoming pollutants and cause of bad odor. These odoriferous substances are volatile organic compounds that currently cannot be removed by conventional washing, which limits their reuse as raw material for products for outdoor use.

[0003] Currently, conventional mechanical recycling consists of a selective classification of plastic waste based on the nature of the polymer, washing with water, which can be add reagents such as soda, surfactants and oxidants, and finally it goes through a mechanical drying stage prior to the extrusion stage where the recycled pellets are obtained.

[0004] WO0110721 refers to a method of reducing odors by ionizing rays in an atmosphere that is not necessarily inert.

[0005] As previously stated, due to the continuous increase in the use of plastic products, the generation of this waste has become a global problem in today's society, so its recycling and its subsequent use as raw material is a necessity, if you want to reduce plastic in landfills. At the same time, using plastic as a raw material allows a reduction in production costs in the industries of the sector, in addition to increasing the added value of the product, since awareness about the care of the environment and with it the demand is increasing, of recycled products in the market.SUMMARY OF THE INVENTION

[0006] Thus an object of the present disclosure is a process for removing odor from a recycled polyolefin composition comprising the step of:a) providing a recycled polyolefin composition; b) mixing the recycled polyolefin composition with from 0.5 wt% to 9.0 wt% with respect to the recycled polyolefin composition, of water c) optionally mixing the results of step b) with at least one odor removal component and d) extruding the mixture; wherein the amount of odor removal component ranges from 0.1 wt% to 10 wt% with respect to the recycled polyolefin composition.DETAILED DESCRIPTION OF THE IN VENTION

[0007] Thus an object of the present disclosure is a process for removing odor from a recycled polyolefin composition comprising the step of: a) providing a recycled polyolefin composition; b) mixing the recycled polyolefin composition with from 0.5 wt% to 9.0 wt%; preferably from 1.1 wt% to 7.2 wt%; more preferably from 1.6 wt% to 4.7 wt% with respect to the recycled polyolefin composition, of water; c) optionally mixing the results of step b) with at least one odor removal component and d) extruding the mixture;

[0008] wherein the amount of odor removal component ranges from 0.1 wt% to 10.0 wt% preferably from 0.3 wt% to 8.0 wt%; more preferably from 0.5 wt% to 6.0 wt%; even more preferably from 0.5 wt% to 3.5 wt% with respect to the recycled polyolefin composition.

[0009] the recycled polyolefin composition is preferably a polyethylene recycled composition or a polypropylene recycled composition or a mixture thereof.

[0010] The recycled polyethylene composition can comprise one or more materials selected from high density polyethylene (HDPE), low density polyethylene (LDPE), linear low density polyethylene (LLDPE).

[0011] More preferably the recycled polyolefin composition is a recycled polypropylene composition.

[0012] The recycled polypropylene composition contains preferably at least 50 wt%; more preferably at least 60 wt% ; even more preferably at least 70 wt% of derived units of propylene. The remaining comonomers can be ethylene; 1 -butene; 1 -hexene or 1 -octene derived units; ethylene being preferred.

[0013] Preferably the Melt Flow Rate of the recycled polypropylene composition, determined according to the method ISO 1133 (230° C, 2.16 kg), ranges from 10 g / 10 min to 150 g / 10 min; preferably from 20 g / 10 min to 100 g / 10 min, more preferably from 25 g / 10 min to 80 g / 10 min.

[0014] The recycled polypropylene composition can be Post-Industrial Resin (PIR) or Post- Consumer Resin (PCR) or mixtures thereof.

[0015] Post-Industrial Resin (PIR) is the waste generated from the manufacturing process that is reclaimed or used again in the same material.

[0016] Post-Consumer Resin (PCR) defined as a resin used by the consumer for its intended purpose, that has reached its end of use, and then tossed into a recycling bin is excluded.

[0017] The process of the present invention give rises to a deodorized polypropylene composition.

[0018] The limonene content of the extruded polymers from the process of the present disclosure is lower than 4.5 ppm; preferably 4.3 ppm, more preferably lower than 4.0 ppm; even more preferably lower than 3.5 ppm, the higher value being 0.5 ppm. he limonene content can be measured according to methods know in the art such as the method described in W02023062058.

[0019] The SHS (120°C) measured according to VDA277 content of the extruded polymers from the process of the present disclosure is lower than 30pgC / g; preferably lower than 28pgC / g; more preferably lower than 25pgC / g; even more preferably lower than 20pgC / g.

[0020] The higher value of SHS (120°C) measured according to VDA277 content of the extruded polymers from the process of the present disclosure being 5pgC / g.

[0021] In the process of the present disclosure the addition of water reduce the level of odor. The odor can be further reduced by adding an odor removal component, so that the odor removal component and water have a synergistic effect.

[0022] The odor removal component can be selected from stripping agents; masking or neutralizing agents; adsorbing agents; molecular sieves; reactive agents; or combination thereof.

[0023] Example of stripping agents is BYK P4200. Example of stripping agents / molecular sieves are Zeoflair 100 and Calcium Oxide. Example of reactive agents is TEGO Sorb PY88TQ. Examples of masking or neutralizing agent are Struktol RP53 or Struktol RP59.

[0024] Preferred odor removal components are stripping agents and in particular BYK P4200 with water are able to drastically remove odor from a recycled propylene composition.

[0025] Preferably the present disclosure is directed to a process for removing odor from a recycled propylene composition comprising the step of: a) providing a recycled polypropylene composition; b) mixing the recycled polypropylene composition with from 0.5 wt% to 9.0 wt%; preferably from 1.1 wt% to 7.2 wt%; more preferably from 1.6 wt% to 4.7 wt% with respect to the total composition, of water; c) mixing the results of step b) with BYK P4200 and d) extruding the mixture; wherein the amount of odor removal component ranges from 0.1 wt% to 10.0 wt% preferably from 0.3 wt% to 8.0 wt%; more preferably from 0.5 wt% to 6.0 wt%; even more preferably from 0.5 wt% to 3.5 wt% with respect to the total composition.

[0026] The following examples are given to illustrate the present invention without limiting purpose.EXAMPLECharacterization methodsMelting temperature and crystallization temperature: Determined by differential scanning calorimetry (DSC)

[0027] It was determined by differential scanning calorimetry (DSC). A sample weighting 6 ±1 mg, is heated to 220 ±1° C at a rate of 20 °C / min and kept at 220 ±1° C for 2 minutes in nitrogen stream and it is thereafter cooled at a rate of 20° C / min to 40 ±2° C, thereby kept at this temperature for 2 min to crystallize the sample. Then, the sample is again fused at a temperature rise rate of 20° C / min up to 220° C ±1. The melting scan is recorded, a thermogram is obtained, and, from this, melting temperatures and crystallization temperatures are read.Melt Flow Rate: Determined according to the method ISO 1133 (230° C, 2.16 kg).Xylene-soluble fraction (XS) at 25°C

[0028] Xylene Solubles at 25°C have been determined according to ISO 16152: 2005; with solution volume of 250 ml, precipitation at 25°C for 20 minutes, 10 of which with the solution in agitation (magnetic stirrer), and drying at 70°C.Intrinsic Viscosity (LV.)

[0029] The sample is dissolved by tetrahydronaphthalene at 135 °C and then it is poured into the capillary viscometer.

[0030] The viscometer tube (Ubbelohde type) is surrounded by a cylindrical glass jacket; this setup allows temperature control with a circulating thermostated liquid.

[0031] The downward passage of the meniscus is timed by a photoelectric device. The passage of the meniscus in front of the upper lamp starts the counter which has a quartz crystal oscillator. The meniscus stops the counter as it passes the lower lamp and the efflux time is registered: this is converted into a value of intrinsic viscosity throughHaze (on 1 mm plaque)

[0032] According to the method used, 5x5 cm specimens are cut molded plaques of 1 mm thick and the haze value is measured using a Gardner photometric unit connected to a Hazemeter type UX-10 or an equivalent instrument having G.E. 1209 light source with filter "C". Reference samples of known haze are used for calibrating the instrument. The plaques to be tested are produced according to the following method.

[0033] 75x75x1 mm plaques are molded with a GBF Plastiniector G235190 InjectionMolding Machine, 90 tons under the following processing conditions:Screw rotation speed: 120 rpmBack pressure: lO barMelt temperature: 260°CInjection time: 5 secSwitch to hold pressure: 50 barFirst stage hold pressure: 30 barSecond stage pressure: 20 barHold pressure profile: First stage 5 secSecond stage 10 secCooling time: 20 secMold water temperature: 40°CEthylene content in the copolymers

[0034] 13C NMR spectra were acquired on a Bruker AV-600 spectrometer equipped with cryoprobe, operating at 160.91 MHz in the Fourier transform mode at 120 °C.

[0035] The peak of the SPP carbon (nomenclature according to “Monomer Sequence Distribution in Ethylene-Propylene Rubber Measured by 13C NMR. 3. Use of Reaction Probability Mode ” C. J. Carman, R. A. Harrington and C. E. Wilkes, Macromolecules, 1977, 10, 536) was used as an internal reference at 29.9 ppm. The samples were dissolved in 1, 1,2,2- tetrachloroethane-d2 at 120 °C with a 8 % wt / v concentration. Each spectrum was acquired with a 90° pulse, and 15 seconds of delay between pulses and CPD to remove 1H-13C coupling. 512 transients were stored in 32K data points using a spectral window of 9000 Hz.

[0036] The assignments of the spectra, the evaluation of triad distribution and the composition were made according to Kakugo (“Carbon- 13 NMR determination of monomer sequence distribution in ethylene-propylene copolymers prepared with 8-titanium trichloride- diethyl-aluminum chloride” M. Kakugo, Y. Naito, K. Mizunuma and T. Miyatake, Macromolecules, 1982, 15, 1150) using the following equations:PPP = 100 Tpp / S PPE = 1OO TP8 / S EPE = 100 T88 / S PEP = 100 SPP / S PEE= 100 SP5 / S EEE = 100 (0.25 Sy8+0.5 S88) / S S = TPP + TP8 + T88 + SPP + Sp8 + 0.25 Sy8 + 0.5 S88

[0037] The molar percentage of ethylene content was evaluated using the following equation:E% mol = 100 * [PEP+PEE+EEE]

[0038] The weight percentage of ethylene content was evaluated using the following equation:100 * E% mol * MWEE% wt. = E% mol * MWE + P% mol * MWP

[0039] where P% mol is the molar percentage of propylene content, while MWE and MWP are the molecular weights of ethylene and propylene, respectively.

[0040] The product of reactivity ratio rlr2 was calculated according to Carman (C.J.Carman, R.A. Harrington and C.E. Wilkes, Macromolecules, 1977; 10, 536) as:

[0041] The tacticity of Propylene sequences was calculated as mm content from the ratio of the PPP mmTPP (28.90-29.65 ppm) and the whole TPP (29.80-28.37 ppm).

[0042] Impact test: ISO 180Preparation of injection molded specimens: test specimens 80 x 10 x 4 mm were obtained according to the method ISO 1873-2:2007.Preparation of injection molded specimens: test specimens 80 x 10 x 4 mm were obtained according to the method ISO 1873-2:2007.Charpy Impact test at 23°C: measured according to ISO 179-1:2010 on injection molded specimens.

[0043] the recycled polypropylene used in the examples is sold by QCP with the tradename QCP300P. It contains residue-drained, rigid, system-compatible items made of polypropylene, volume < 5 litres, e.g. bottles, bottles, cups and trays, incl. secondary components such as lids, labels etc.

[0044] Purity is at least 94 wt%, metallic and mineral impurities with a unit weight of > 100 g and cartridges for sealants are not permitted!Impurities

[0045] Examples of other residues are:GlassPaper, Board, CardboardComposite paper / cardboard materials (e.g. liquid packaging boards) Aluminized plasticsOther materials (e.g. rubber, stones, wood, textiles, nappies)Compostable waste (e.g. food, garden waste)

[0046] The Melt flow rate (230 °C / 2.16 kg) of T1 is 16 g / 10 min and the melting point is 150°CExample 1

[0047] 2.0 wt% of water has been mixed with a sample of QCP300P and the resulting composition has been extruded in a twin screw extruder ZSK 26 with the following process parameters: T = 220-200°C / 600 rpm / Output 20 kg / h / Vacuum system.

[0048] The resulting pellets have been packed to aluminum bags to prevent moisture pick-up and odor venting during transport. Various odor removal has been used. The resulting compositions are reported in table 1.Example 2

[0049] Water 2 wt% and 2 wt% of BYK P4200, a polymer processing additive for thermoplastics, have been mixed with a sample of QCP300P and the resulting composition has been extruded in a twin screw extruder ZSK 26 with the following process parameters: T = 220- 200°C / 600 rpm / Output 20 kg / h / Vacuum system.

[0050] The resulting pellets have been packed to aluminum bags to prevent moisture pick-up and odor venting during transport. Various odor removal has been used. The resulting compositions are reported in table 1.Example 3

[0051] Water 4 wt% and 2 wt% of BYK P4200, a polymer processing additive for thermoplastics, have been mixed with a sample of QCP300P and the resulting composition has been extruded in a twin screw extruder ZSK 26 with the following process parameters: T = 220- 200°C / 600 rpm / Output 20 kg / h / Vacuum system.

[0052] The resulting pellets have been packed to aluminum bags to prevent moisture pick-up and odor venting during transport. Various odor removal has been used. The resulting compositions are reported in table 1.Comparative example 4-5

[0053] 2 wt% and 5 wt% of BYK P4200, a polymer processing additive for thermoplastics, have been mixed with a sample of QCP300P and the resulting composition has been extruded in a twin screw extruder ZSK 26 with the following process parameters: T = 220-200°C / 600 rpm / Output 20 kg / h / Vacuum system.

[0054] The resulting pellets have been packed to aluminum bags to prevent moisture pick-up and odor venting during transport. Various odor removal has been used. The resulting compositions are reported in table 1.Reference example

[0055] QCP300P a has been extruded in a twin screw extruder ZSK 26 with the following process parameters: T = 220-200°C / 600 rpm / Output 20 kg / h / Vacuum system.

[0056] The resulting pellets have been packed to aluminum bags to prevent moisture pick-up and odor venting during transport. Various odor removal has been used. The resulting compositions are reported in table 1.

[0057] Odor of the resulting compositions have been analyzed, SHS (120°C) according to VDA277Table 1From table 1 clearly results that after the treatment, the compositions of the invention are able to reduce the odor

Claims

CLAIMS1. A process for removing odor from a recycled polyolefin composition comprising the step of: a) providing a recycled polyolefin composition; b) mixing the recycled polyolefin composition with from 0.5 wt% to 9.0 wt% with respect to the recycled polyolefin composition, of water; c) optionally mixing the results of step b) with at least one odor removal component and d) extruding the mixture; wherein the amount of odor removal component ranges from 0.1 wt% to 10 wt% with respect to the recycled polyolefin composition; and wherein the recycled polypropylene composition contains at least 60 wt%; of derived units of propylene.

2. The process according to claim 1 wherein the limonene content of the extruded polymers from the process of claim 1 is lower than 4.5 ppm.

3. The process according to any of claims 1-2 wherein the recycled polyolefin composition is a polypropylene recycled composition.

4. The process according to any of claims 1-3 wherein in step b) from 1.1 wt% to 7.2 wt% of water is added.

5. The process according to any of claims 1-4 wherein in step b) from 1.6 wt% to 4.7 wt% of water is added.

6. The process according to any of claims 1-5 wherein in step c) the odor removal is added in an amount ranging from 0.3 wt% to 8.0 wt%.

7. The process according to any of claims 1 -6 wherein the Melt Flow Rate of the recycled polypropylene composition, determined according to the method ISO 1133 (230° C, 2.16 kg), ranges from 10 g / 10 min to 150 g / 10 min..

8. The process according to any of claims 1-7 wherein the limonene content of the extruded polymers from the process of claim 1 is lower than 4.3 ppm.

9. The process according to any of claims 1-8 wherein the recycled polypropylene composition contains at least 70 wt%; of derived units of propylene.

10. The process according to any of claims 1-9 wherein the recycled polypropylene composition contains one or more comonomers selected from the group consisting of ethylene; 1 -butene; 1- hexene and 1 -octene derived units other than derived units of propylene.

11. The process according to any of claims 1-10 wherein the SHS (120°C) measured according to VDA277 content of the extruded polymers from the process of the present disclosure is lower than 30pgC / g.12 The process according to any of claims 1-11 wherein the SHS (120°C) measured according to VDA277 content of the extruded polymers from the process of the present disclosure is lower than 28pgC / g.

13. The process according to any of claims 1-12 wherein the SHS (120°C) measured according to VDA277 content of the extruded polymers from the process of the present disclosure is lower than 25pgC / g14. The process according to any of claims 1-13 wherein the amount of odor removal component in step c) ranges from 0.5 wt% to 3.5 wt%.15 The process according to any of claims 1-14 wherein the Melt Flow Rate of the recycled polypropylene composition, determined according to the method ISO 1133 (230° C, 2.16 kg), ranges from 20 g / 10 min to 100 g / 10 min.

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