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    • 专利摘要:
    PROCESS TO CONVERT MIXED POLYETHYLENE WASTE TO PRODUCE WAXES AND GREASE THROUGH CATALYTIC DEPOLIMERIZATION AND PROCESS TO CONVERT PRIMARY POLYETHYLENE BEADS TO PRODUCE CATALYTIC DEPOLIMERIZATION BEADS. The present invention describes a process for depolymerizing mixed polyethylene residue. In one embodiment, in a process for converting mixed polyethylene residue to produce waxes and greases through catalytic depolymerization, the mixed polyethylene residue is preheated to form a melted mixed polyethylene residue. Then the depolymerization reaction uses a catalyst in a high pressure reactor at a desired temperature using heaters in the high pressure reactor. The catalyst is placed on a stirring paddle. The progression of the depolymerization reaction of the melted mixed polyethylene residue is allowed to continue until the pressure in the high pressure reactor reaches a desired value. The heaters are turned off and the depolymerization reaction of the mixed molten polyethylene residue is stopped when the pressure in the reactor reaches the desired value. The mixed polyethylene residue is converted to wax or grease.
    公开号:BR112013001058B1
    申请号:R112013001058-4
    申请日:2011-07-14
    公开日:2020-09-29
    发明作者:Anil Kumar；Pushkar Kumar
    申请人:Greenmantra Recycling Technologies Ltd；
    IPC主号:
    专利说明:

    BACKGROUND
    [0001] Producers of mechanical equipment, food packers and other users of wax and grease for lubrication, sealing and other uses have a continuing need for wax and grease compositions. The production of these waxes and greases is usually expensive. This can typically be due to a need for expensive oil feed in such a production process.
    [0002] Waxes and greases (or grease inputs) are made, in general, from oil feed or gas-to-liquid process. The price of oil inputs is increasing over time, so there is a constant increase in the price of waxes and greases. Recently, some discoveries were made of gas reservoirs (practically methane) and uses of the Fischer-Tropsch process; these can be converted into hydrocarbons with a longer chain length in order to generate gasoline, lubricating oils, grease inputs and waxes. Products produced in this way are relatively more expensive and, therefore, there is a need to use readily available polyethylene residue and recycle it to produce the same materials at considerably lower cost.
    [0003] It would be advantageous to have a relatively inexpensive process for producing wax and grease input. Such a process would ideally use a low-cost input readily available and would be a low-cost process. Plastics / polymer residues have been used in known processes for the production of such products. Plastic waste is among the fastest growing solid waste and using this solid waste to produce useful waxes and greases leads to growing problems with plastics disposal.
    [0004] Additionally, most of the polymer / plastic residues can be made of polyethylene and, due to its non-biodegradation, it has accumulated in nature. The polyethylene waste is, in general, disposed of in landfills or burned - the first leads to loss of material and waste of land while the second results in the emission of greenhouse gases; only a proportion of all plastic waste is currently recycled as secondary polymers, which are of low quality and have low financial returns.
    [0005] In recent times, there have been considerable efforts to convert these solid polymeric residues into useful products with fuels, lubricants, waxes and grease inputs. Existing conversion processes may not be efficient enough and can release greenhouse gases into the environment. Furthermore, current techniques can be sensitive to the quality and quantity of plastic feed waste and they can have an impact on the quality of the final product. This can be especially important since the plastic waste can vary in consistency due to the variation ranges of the plastics. BRIEF DESCRIPTION OF THE FIGURES
    [0006] Several modalities are described here with reference to the figures, being that:
    [0007] Figure 1 shows a block diagram of an exemplary process of converting mixed polyethylene waste to produce waxes and grease inputs through catalytic depolymerization, according to one modality;
    [0008] Figure 2 shows, in the context of the invention, an exemplary graph of gas chromatography results - mass spectroscopy (GC - MS) of microcrystalline wax produced using existing processes;
    [0009] Figure 3 shows an example graph of GC-MS results of the wax obtained from the depolymerization of high density polyethylene (HDPE) residue, according to one modality;
    [0010] Figure 4 shows, in the context of the invention, a graph from an analysis of differential scanning calorimetry (DSC) of microcrystalline wax produced using existing processes;
    [0011] Figure 5 shows a DSC analysis graph of the wax obtained from the depolymerization of the HDPE residue, according to one modality;
    [0012] Figure 6 shows a graph of shear log versus viscosity log of sample 1 of the grease input, according to one modality;
    [0013] Figure 7 shows a graph of shear log versus viscosity log of sample 2 of the grease input, according to one modality; and
    [0014] Figure 8 shows a block diagram of a device for converting mixed polyethylene residue into waxes and grease inputs, according to one modality.
    [0015] The figures described here are for illustrative purposes only and should not be construed as limiting the scope of this description in any way. DETAILED DESCRIPTION
    [0016] A method for producing waxes and grease inputs through the catalytic depolymerization of plastic residues is described. In the following detailed description of the modalities of the present matter, reference is made to the attached figures, which form a part of it, and in which they are shown as an illustration of the specific modalities in which the present invention can be practiced. These modalities are described in sufficient detail to allow those skilled in the art to practice the present invention, and it should be understood that other modalities can be used and changes can be made without departing from the scope of the present invention. The following detailed description should therefore not be taken in a limiting sense and the scope of the present invention is defined by the appended claims.
    [0017] Figure 1 shows a block diagram 100 of an exemplary process for producing waxes and grease inputs through the catalytic depolymerization of mixed polyethylene waste, according to one modality. Waxes are slippery solid materials that are easy to melt. Generally, the melting point of waxes is in the range of 45 ° C to 130 ° C and the flash point (that is, the lowest temperature at which wax can vaporize to form a flammable mixture with air) is in the range 180 ° C and 350 ° C. Waxes can generally be derived from refining crude oil. Waxes can also be derived from natural plant and animal secretions. In addition, waxes can be synthetically produced using processes such as Fischer-Tropsch.
    [0018] Grease or grease input is a semi-solid substance introduced between two moving surfaces to reduce friction between them, improving efficiency and reducing wear. Commercially available greases are generally made by mixing grease inputs with small amounts of specific additives to give them desired physical properties. Greases are generally of four types: (a) mixture of mineral oils and solid lubricants, (b) blends of residues, waxes, unmatched fats, rosin and rosin oils, (c) mineral oils thickened by soap and (d ) synthetic greases with polyalpha-olefins, silicones etc.
    [0019] Mixed polyethylene waste can include low density polyethylene (LDPE) and high density polyethylene (HDPE). For example, polyethylene waste may be available as shopping bags, market bags like HDPE bags, milk bags made from LDPE and PELBD stationery. In one embodiment, the primary polyethylene granules can also be used for the production of waxes and grease inputs. In addition, the mixed polyethylene residue can include impurities (for example, such as polypropylene and polystyrene) up to about 10%.
    [0020] In step 102, the mixed polyethylene residue is heated to form a molded mixed polyethylene residue. For example, the mixed polyethylene residue is preheated in an extruder attached to a high pressure reactor (for example, reactor 804 in Figure 8). The molded mixed polyethylene residue formed in the extruder is substantially and continuously pushed into the high pressure reactor. In step 104, the depolymerization reaction of the molded mixed polyethylene residue is initiated using a catalyst in the high pressure reactor at a desired temperature using heaters in the high pressure reactor. The catalyst used is [Fe-Cu-Mo-P] / AI2O3, which is arranged on a stirring blade of the high pressure reactor. The catalyst is prepared by attaching an iron-copper complex to an alumina support and reacting it with a heteropoly acid to obtain the final catalyst. The temperature in the high pressure reactor is in the range of about 300 ° C to 600 ° C.
    [0021] In step 106, the progression of the depolymerization reaction of the mixed molded polyethylene residue is allowed to continue until the pressure in the high pressure reactor reaches a desired value. The pressure in the high pressure reactor is in the range of about 0.345 MPa - 2.413 MPa (gauge). In step 108, the desired pressure value in the high pressure reactor is varied in order to produce different fractions of waxes and grease inputs. For example, different wax fractions include waxes having different melting points in the range of 60 ° C to 100 ° C.
    [0022] In step 110, the heaters are turned off and the depolymerization reaction of the mixed molded polyethylene residue is stopped as soon as the reactor reaches the desired value. During the depolymerization reaction, the molded mixed polyethylene residue is converted to wax or grease input. In step 112, the converted wax or grease input is drained into a container when the wax or grease input becomes liquid and is substantially above the flash point.
    [0023] It can be noted that, during the depolymerization reaction, there is no gas being released and, then, there is a complete recovery of carbon in the form of waxes or grease inputs. In step 114, the coalescence of pigment particles / impurities is initiated in the wax drain or converted grease input using a high to low pressure cycle. In step 116, particles of pigment / impurities and converted wax or grease input are allowed to settle in the container with separate layers.
    [0024] Figure 2 shows, in the context of the invention, an exemplary graph 200 of gas chromatography-mass spectroscopy (GC-MS) results for microcrystalline wax produced using existing processes. For example, GC-MS is a method that combines features of gas-liquid chromatography and mass spectroscopy to identify different components in microcrystalline wax produced using existing processes. (Microcrystalline waxes are a type of wax that has melting points in the range of 60 ° C to 100 ° C and are generally more rigid than paraffin waxes). The x-axis of graph 200 represents the retention time and the y-axis represents intensity.
    [0025] Figure 3 shows an example graph 300 of GC-MS results of the wax obtained from depolymerization of high density polyethylene (HDPE) residue, according to one modality. The depolymerization reaction of the HDPE waste is carried out according to the process explained in Figure 1. Approximately 3.5 kg of HDPE waste purchased in a local market is taken for the depolymerization reaction in the high pressure reactor (which has a 6.5 liter capacity). Different experiments were carried out in order to compare the properties of the wax obtained from the depolymerization reaction with those of microcrystalline wax produced using existing processes.
    [0026] In Experiment 1, a desired pressure of 0.97 MPa (gauge) (140 pound-force per inch squared (psig)) is chosen. When the pressure inside the high pressure reactor reaches 0.97 MPa, the polymerization reaction is stopped. The obtained wax is drained, cooled and tested for GC-MS. TABLE 1 shows properties of the wax obtained through the depolymerization reaction compared to the commercially available ARGE wax (a type of Fischer-Tropsch wax). TABLE 1

    [0027] Graph 200 and graph 300 are compared. The comparison of the molecular mass distribution (MWD) is shown in TABLE 2. TABLE 2


    [0028] It can be inferred from TABLE 2 and graphs 200 and 300 that the wax obtained from the depolymerization of the HDPE residue has a wider MWD and a slightly higher melting point, but in other respects it is comparable to the wax microcrystalline produced using existing processes.
    [0029] Figure 4 shows, in the context of the invention, a 400 graph of differential scanning calorimetry (DSC) analysis of microcrystalline wax produced using existing processes. DSC is a thermoanalytical technique in which the difference in the amount of heat required to increase the temperature of a sample and the reference is measured as a function of the temperature. The x-axis of graph 400 represents temperature and the y-axis represents heat flow.
    [0030] Figure 5 shows a 500 graph of DSC analysis of the wax obtained from the depolymerization of the HDPE residue, according to one modality. Graph 400 and graph 500 are compared. The melting point of the wax obtained from the depolymerization of HDPE is about 10% higher than that of microcrystalline wax produced using existing processes. In addition, the wax produced from HDPE has been discovered to have a natural adhesion that makes it highly recommended for polishing waxes and shoe polishers.
    [0031] Experiment 2 considers the melting point of the wax, which is an important property. The melting point of the wax is determined by a desired pressure value inside the high pressure reactor. TABLE 3 below shows different pressure values that generate waxes with different melting points. TABLE 3

    [0032] In Experiment 3, the following feed composition is considered in the high pressure reactor. It should be noted that HDPE, LDPE and PELBD are available as primary granules. 1. Primary HDPE, LDPE and PELBD granules as pure feed 2. Residual HDPE, LDPE and PELBD feeds as pure feed 3. Various mixtures of primary HDPE, LDPE and LLDPE granules 4. Various mixtures of residual HDPE, LDPE materials and PELBD 5 .Mixture of (1) and (2) 6. Residual materials of HDPE, LDPE and PELBD as pure feeds with 10% polypropylene and polystyrene impurities.
    [0033] In each case, the desired value inside the high pressure reactor remained unchanged, indicating that the catalyst is specific for breaking CH2-CH2 bonds and is relatively insensitive to the nature of the supply.
    [0034] In Experiment 4, a water emulsion of various waxes produced in Experiment 2 is prepared and the compositions are as follows: Composition A - 5g Wax and 2.5g Stearic Acid Composition B - 300g Water, 3g Morpholine and 2 , 5g Stearic Acid
    [0035] The solids of composition A are mixed and melted. The product is mixed with the previously heated composition B. The emulsion is obtained with stirring. It can be seen that the emulsion is stable and the wax does not separate from the aqueous layer. The emulsion then formed forms a very thin layer of wax in coatings, having resistance depending on the melting point of the wax used.
    [0036] In Experiment 5, a grease input is produced for a cutting pressure of 1.72-2.07 MPa (gauge) (250—300psig) (which is Sample 1) and for a cutting pressure of 2 , 07-2.41 MPa (gauge) (300-350psig) (which is Sample 2). In one embodiment, the viscosities of sample 1 and sample 2 are determined with a function of temperature and shear rate.
    [0037] Figure 6 shows a 600 graph of shear log versus viscosity log of sample 1 of the grease input, according to one modality. The shear log is represented on the x-axis and the viscosity log is represented on the y-axis of graph 600. The shear rate, shear stress and viscosity of sample 1 at 40 ° C, 100 ° C and 150 ° C are shown in the TABLES 4, 5 and 6. TABLE 4 (at 40 °)


    TABLE 5 (100 ° C)

    TABLE 6 (150 ° C)


    [0038] Figure 7 shows a 700 graph of shear log versus viscosity log of sample 2 of the grease input, according to one modality. The shear log is represented on the x axis and the viscosity log is represented on the y axis of graph 700. The shear rate, shear stress and sample viscosity 1 at 40 ° C, 100 ° C and 150 ° C are given in TABLES 7, 8 and 9. TABLE 7 (at 40 ° C)

    TABLE 8 (at 100 ° C)


    TABLE 9 (at 150 ° C)


    [0039] The experiments mentioned above suggest that lower cutting pressures yield grease inputs with higher viscosity. As the temperature of the grease input is increased, the viscosity value is decreased, as expected. For a given temperature and cutting pressure, the viscosity is dependent on the shear rate and drops dramatically. Up to a shear rate of 100 per second, viscosity drops by a factor of 1000, leading to an increase in lubrication by the same factor. This indicates that the grease input has a natural ability to generate a high degree of lubrication.
    [0040] Figure 8 shows a block diagram 800 of a device for producing waxes and grease inputs through catalytic depolymerization of plastic residues, according to one modality. In particular, the device includes an extruder 802, an oven 830, a reactor 804, a condenser 806, a drum 808, a drum 810 and a tray 828.
    [0041] The 802 extruder is a 10.16 cm barrel with a length of 60.96 cm. The 802 extruder preheats the polyethylene residue and pushes the molded polyethylene residue to the 804 reactor. The 802 extruder operates at 300 ° C and pushes the molded polyethylene residue through an 816 valve. In one embodiment, preheat the polyethylene residue can make possible a shorter processing time of the polyethylene residue in the 804 reactor since the preheating occurs outside the 804 reactor (in the 802 extruder). In addition, a semi-continuous process is ensured in the 804 reactor.
    [0042] The 804 reactor is 2 cm thick, 15 cm in diameter and 30 cm long and has an operating capacity of 6.5 liters. As shown, oven 830 includes heaters 812 to heat reactor 804. The temperature in reactor 804 is maintained at 450 ° C. The reactor 804 includes an agitator 814, a pressure gauge 822 and a paddle with catalyst 824. The reactor 804 is designed in such a way that the walls of the reactor 804 sustain high temperatures and pressures during the depolymerization process. The catalytic paddle 824 carries a catalyst that accelerates the depolymerization reaction of the molded polyethylene residue in the 804 reactor. In an exemplary embodiment, the catalyst used in o (Fe-Cu-Mo-P] / AI2O3 •
    [0043] In operation, when the 804 reactor receives the waste of molded polyethylene, the temperature drops from 450 ° C. When the temperature drops, the temperature of heaters 812 is increased to ensure that the pressure inside the reactor 804 is maintained at atmospheric pressure by closing a valve 818 and opening a valve 820. The pressure inside the reactor 804 is measured using the manometer 822. In one embodiment, the pressure inside the 804 reactor affects the quality of the wax formed. It can be noted that the volume of the molded polyethylene waste fed to the 804 reactor is doubled at the temperature inside the 804 reactor.
    [0044] Valve 816 and valve 820 are closed to increase pressure in reactor 804. When a desired pressure (in the range of 0.345 MPa - 2.413 MPa (gauge) - 50-350psig) is reached inside the 804 reactor, the heaters 812 are turned off and the depolymerization reaction is stopped. The depolymerization reaction takes about an hour inside reactor 804. Valve 820 is gradually opened and the pressure inside reactor 804 is allowed to drop to atmospheric pressure. Steam from reactor 804 escapes through valve 820 to condenser 806 and is finally collected in drum 808. The temperature inside reactor 804 remains unchanged.
    [0045] As the pressure inside reactor 804 drops to atmospheric pressure, valve 820 is closed and valve 818 is opened to drain the material produced. The pressure reduction to an atmosphere inside the 804 reactor initiates a process of coalescing impurities from organic and inorganic pigments (such as carbon, calcium carbonate etc.) present together with the polyethylene residue. The pigment impurities coalesce and accommodate themselves as separate layers by manipulating valves 816, 818 and 820. There is no requirement for an additional process to separate the pigment impurities from the waxes and grease inputs formed. Then cycles of high to low pressure inside the 804 reactor separate the pigment impurities, leaving pure waxes and grease supplies behind. The small amount of pressure that is developed inside the 804 reactor pushes the products produced from the 804 reactor to the 810 drum.
    [0046] When products are poured into drum 810 at more than 400 ° C, small amounts of hydrocarbon vapors can be produced. A pipeline 826 over the drum 810 ensures that the hydrocarbon vapors then formed do not escape into the atmosphere and these are completely condensed in the drum 810. These hydrocarbon vapors form a protective layer on top of the wax or grease input, preventing the wax or grease input comes into direct contact with the atmosphere and burns. The products collected in drum 810 are condensed at 200 ° C and are then drained into tray 828. This process ensures that liquid products can be drained at more than 400 ° C, even though that temperature is significantly above the set point. glow of waxes and grease inputs.
    [0047] Reducing pressure and removing material produced from reactor 804 can take about 30 minutes. In this way, a cycle of catalytic depolymerization can take about two and a half hours. It can be seen that the depolymerization reaction is not sensitive to impurities such as polypropylene and polystyrene present in up to 10% in the polyethylene residue. Waxes and grease inputs of specified quality can be obtained by manipulating process conditions and valves 818 and 820. For example, by manipulating the desired pressure inside the 804 reactor, waxes of different degrees (for example, with different set points) fusion) are obtained.
    [0048] In several modalities, the processes described in Figures 1 to 8 use a new catalyst that is not deactivated and lasts for about a year in use in the process, thus making the process economical. The catalyst is stable over the reaction temperatures of 300 ° C-600 ° C and depolymerizes HDPE, LDPE and PELBD equally. The catalyst is also unaffected by any pigment impurities. In addition, the use of an extruder to preheat the polyethylene waste ensures that a high temperature molded polyethylene waste is fed into the reactor. During the process described above, there is a total recovery of carbon from the polyethylene residue in desired products, which makes the process ecologically favorable.
    [0049] Although the present modalities have been described with reference to specific exemplary modalities, it will be evident that several modifications and alterations can be made to these modalities without departing from the broader spirit and scope of the various modalities.
    权利要求:
    Claims (24)
    [0001]
    1. Process for converting mixed polyethylene waste to produce waxes and greases through catalytic depolymerization, characterized by comprising: preheating the mixed polyethylene residue to form a melted mixed polyethylene residue; initiate a depolymerization reaction of the melted mixed polyethylene residue using a catalyst in a pressurized reactor at a desired temperature using heaters in the pressurized reactor and the catalyst is disposed within the pressurized reactor; allow the progression of the depolymerization reaction of the melted mixed polyethylene residue to continue until the pressure in the pressurized reactor reaches a desired value; and turn off the heaters and stop the depolymerization reaction of the melted mixed polyethylene residue after the pressure in the reactor has reached the desired value, in which the mixed polyethylene residue is converted to wax or grease, and where the catalyst is [Fe- Cu-Mo-P] / AI2O3, prepared by attaching an iron-copper complex to an alumina support and reacting it with a heteropoly acid.
    [0002]
    Process according to claim 1, characterized in that the desired pressure is in the range of 0.345 MPa (50 psig) to 2.413 MPa (350 psig).
    [0003]
    3. Process to convert mixed polyethylene residues to produce waxes and greases through catalytic depolymerization, characterized by comprising: preheating the mixed polyethylene residue to form a melted mixed polyethylene residue; effect the catalytic depolymerization of the melted mixed polyethylene residue within a reaction zone of a pressurized reactor; and terminate the depolymerization reaction of the melted mixed polyethylene residue in response to the detection of a pressure within the reaction zone sufficient to effect the conversion of the mixed polyethylene residue into wax or grease, in which a catalyst comprising [Fe-Cu-Mo -P] / AI2O3 is used in the depolymerization reaction, in which the pressure is in the range of 0.345 MPa (50 psig) to 2.413 MPa (350 psig).
    [0004]
    Process according to claim 1 or 3, characterized in that it further comprises: draining the converted wax or grease into a container when the converted wax or grease is liquid and above the flash point.
    [0005]
    Process according to claim 1 or 3, characterized in that the temperature of the catalytic depolymerization is in the range of 300 ° C to 600 ° C.
    [0006]
    Process according to claim 1 or 3, characterized in that the preheating of the mixed polyethylene residue to form the molten mixed polyethylene residue is carried out using an extruder connected to the reactor.
    [0007]
    Process according to claim 6, characterized in that it additionally comprises: continuously pushing the mixed polyethylene residue in the reactor when the mixed polyethylene reaches the molten state in the extruder.
    [0008]
    Process according to claim 1 or 3, characterized in that the mixed polyethylene residue comprises polyethylene selected from the group consisting of low density polyethylene (LPDE), linear low density polyethylene (LLPDE) and high density polyethylene (HPDE) .
    [0009]
    Process according to claim 1 or 3, characterized in that the mixed polyethylene residue comprises impurities of up to 10%, and that the impurities comprise materials selected from the group consisting of polypropylene and polystyrene.
    [0010]
    Process according to claim 1 or 3, characterized in that it further comprises: varying the pressure value in the pressurized reactor to produce different types of waxes and greases.
    [0011]
    Process according to claim 10, characterized in that it further comprises: inducing the coalescence of pigment particles / impurities in the converted wax or grease drained using a high to low pressure cycle; and allowing the pigment particles / impurities and the converted wax or grease to rest in the container as separate layers.
    [0012]
    12. Process for converting primary polyethylene granules to produce waxes and greases through catalytic depolymerization, characterized by comprising: preheating the primary polyethylene granules to form a melt of primary polyethylene granules; initiate the depolymerization reaction of the melt of primary polyethylene granules using a catalyst in a pressurized reactor at a desired temperature using heaters in the pressurized reactor and in which the catalyst is disposed within the pressurized reactor; allow the progression of the depolymerization reaction of the melt of primary polyethylene granules to continue until the pressure in the pressurized reactor reaches a desired value; and turn off the heaters and stop the depolymerization reaction of the primary polyethylene granule melt after the pressure in the reactor has reached the desired value, in which the primary polyethylene granules are converted to wax or grease, and where the catalyst is [ Fe-Cu-Mo-P] / AI2O3, prepared by attaching a ferro-copper complex to an alumina support and reacting it with a heteropoly acid.
    [0013]
    Process according to claim 12, characterized in that the desired pressure is in the range of 0.345 MPa (50 psig) to 2.413 MPa (350 psig).
    [0014]
    14. Process for converting primary polyethylene granules to produce waxes and greases through catalytic depolymerization, characterized by comprising: preheating the primary polyethylene granules to form a melt of primary polyethylene granules; effect the catalytic depolymerization of the melt of primary polyethylene granules within a reaction zone of a pressurized reactor; and terminate the depolymerization reaction of the melt of primary polyethylene granules in response to the detection of a pressure within the reaction zone sufficient to effect the conversion of the mixed polyethylene residue into wax or grease, in which a catalyst comprising [Fe-Cu- Mo-P] / AI2O3 is used in the depolymerization reaction, where the pressure is in the range of 0.345 MPa (50 psig) to 2.413 MPa (350 psig).
    [0015]
    Process according to claim 12 or 14, characterized in that it further comprises: draining the converted wax or grease into a container when the converted wax or grease is liquid and above the flash point.
    [0016]
    Process according to claim 12 or 14, characterized in that the temperature of the catalytic depolymerization is in the range of 300 ° C to 600 ° C.
    [0017]
    Process according to claim 12 or 14, characterized in that the preheating of the primary polyethylene granules to form the melt of primary polyethylene granules is carried out using an extruder connected to the reactor.
    [0018]
    Process according to claim 17, characterized in that it further comprises: continuously pushing the primary polyethylene granules into the reactor when the primary polyethylene granules reach the molten state in the extruder.
    [0019]
    Process according to claim 12 or 14, characterized in that the primary polyethylene granules comprise polyethylene selected from the group consisting of LPDE, LLPDE and HPDE.
    [0020]
    Process according to claim 12 or 14, characterized in that the primary polyethylene granules comprise impurities of up to 10%, and that the impurities comprise materials selected from the group consisting of polypropylene and polystyrene.
    [0021]
    21. Process according to claim 12 or 14, characterized in that it further comprises: varying the pressure value in the pressurized reactor to produce different types of waxes and greases.
    [0022]
    22. The method of claim 21, further comprising: inducing the coalescence of pigment particles / impurities in the converted wax or grease drained using a high to low pressure cycle; and allowing the impurities / pigment particles and the converted wax or grease to rest in a container as separate layers.
    [0023]
    23. Process according to claim 1 or 3, characterized in that the wax or grease is grease.
    [0024]
    Process according to claim 1 or 3, characterized in that the wax or grease is wax.
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    法律状态:
    2019-11-05| B06F| Objections, documents and/or translations needed after an examination request according [chapter 6.6 patent gazette]|
    2020-01-21| B06U| Preliminary requirement: requests with searches performed by other patent offices: procedure suspended [chapter 6.21 patent gazette]|
    2020-07-07| B09A| Decision: intention to grant [chapter 9.1 patent gazette]|
    2020-09-29| B16A| Patent or certificate of addition of invention granted [chapter 16.1 patent gazette]|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 14/07/2011, OBSERVADAS AS CONDICOES LEGAIS. |
    优先权:
    申请号 | 申请日 | 专利标题
    US12/836,594|US8664458B2|2010-07-15|2010-07-15|Method for producing waxes and grease base stocks through catalytic depolymerisation of waste plastics|
    US12/836,564|2010-07-15|
    EP10172039.9A|EP2407528B1|2010-07-15|2010-08-05|Method for producing waxes and grease base stocks|
    EP10172039.9|2010-08-05|
    PCT/IB2011/001642|WO2012007833A2|2010-07-15|2011-07-14|Method and producing waxes and grease base stocks through catalytic depolymerisation of waste plastics|
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