WO2024083783A1

WO2024083783A1 - Hydrocarbon feedstock derived from mixed plastic waste

Info

Publication number: WO2024083783A1
Application number: PCT/EP2023/078761
Authority: WO
Inventors: Robert C. Schucker; Jason LOILAND; Dustin Farmer
Original assignee: SABIC Global Technologies BV
Current assignee: SABIC Global Technologies BV
Priority date: 2022-10-19
Filing date: 2023-10-17
Publication date: 2024-04-25
Anticipated expiration: 2025-04-19
Also published as: EP4605491A1; CN120077116A

Abstract

The invention is directed to a process and a system of producing a hydrocarbon feedstock comprising an oligomeric product derived from waste plastic material wherein such hydrocarbon feedstock is particularly suited for fluidized catalytic cracking. The invention further relates to such hydrocarbon feedstock and its associated properties.

Description

HYDROCARBON FEEDSTOCK DERIVED FROM MIXED PLASTIC WASTE

CROSS REFERENCE TO RELATED APPLICATIONS

[0001] This application claims priority to European Patent Application No. 22202344, filed on October 19, 2022.

FIELD OF INVENTION

[0002] The present invention is directed to a process and a system of producing a hydrocarbon feedstock comprising an oligomeric product derived from waste plastic material and is particularly suitable for fluidized catalytic cracking. The invention further relates to such hydrocarbon feedstock and its associated properties.

BACKGROUND

[0003] Fluidized Catalytic Cracking (FCC) is one of the processes of obtaining gasoline and other high valued chemicals such as ethylene and propylene from a hydrocarbon feedstock. With constant fluctuation of gasoline price impacting world economy, industry practitioners and governmental agencies have been exploring the option of producing gasoline and other high valued chemicals through a reliable and an economical feed source. One of the challenges faced by operators of FCC units, is the need of making the FCC process more operationally efficient and cost effective by increasing the extent of conversion of the hydrocarbon feedstock to obtain high valued chemical products while keeping the extent of coke formation to an acceptable level.

[0004] One possible approach can be to partially substitute expensive feed like vacuum gas oil with a material which is available in relative abundance and can therefore lower the cost of feedstock procurement. Further, it is desirable that the high valued chemicals such as propylene, butylene are produced at desired productivity while managing the extent of coke formation. Managing the coke formation is particularly beneficial as catalyst regeneration and productivity can be kept at an efficient level. As an additional consideration, FCC operators are often faced with the challenge of dealing with hydrocarbon feed having undesirably high amounts of inorganic material and chlorine. Unless such species are removed from the hydrocarbon feed, the presence of such species tend to adversely affect the FCC operation.

[0005] On the other hand, a seemingly unconnected problem to challenges of operating FCC units is the issue of handling waste plastics. Waste plastics are mostly diverted to landfills or are incinerated, with a smaller product being diverted to recycling. Over the years, with increased regulations and levies on landfills, the percentage of the post-consumer waste being recycled or incinerated for energy recovery is gradually increasing making waste plastic disposal through landfills increasingly difficult.

[0006] Some of the possible technologies to treat plastic waste can be technologies based on thermal cracking or catalytic cracking of plastic waste, since these technologies allow the treatment of mixtures of different types of plastics without the need of separation by polymer types, resulting in the generation of hydrocarbons suitable for producing high value chemicals.

[0007] In the past, thermal cracking has been investigated at the laboratory and pilot plant level, for the treatment of plastic waste. However, ordinary processes of thermal cracking generate low quality and unstable hydrocarbons having a wide range of boiling points, which render such processes inefficient and uneconomical for waste plastic treatment. Among the different methods to carry out catalytic cracking of plastic waste is fluidized catalytic cracking (FCC).

[0008] However, certain challenges still persists while using FCC units for processing plastic waste: (1) handling of solid plastic waste is not always easy, (2) plastic waste may not be soluble in vacuum gas oil (VGO) typically used as feed in FCC units, and (3) plastic waste streams may contain levels of chlorine and other inorganic material content that are well in excess of the FCC unit feed specifications, (4) the catalyst system in the FCC unit may not be able to handle polymeric material with large molecular weight.

[0009] Most conventional chemical recycling methodologies for plastic waste involve the pyrolysis of plastic to make pyrolysis oil (also known as “pyoil”). As the term is conventionally understood, this involves the complete or near-complete depolymerization of the plastics. Using pyoil-based feed is an option to address drawbacks related to handling polymeric material with large molecular weight in FCC unit. However, pyrolysis of waste plastic to make pyoil is an energy intensive process that involves breaking down the polymer present in the waste plastic to weight average molecular weight to less than 400 g/mol. The pyrolysis processes not only have high energy requirements but also under certain conditions emit undesirable green house and other undesirable gases. Further, pyoil contains aromatics, olefins, and other unsaturated species which may cause increased char (coke) formation during FCC operation. In addition, use of pyoil and other pyrolysis products may lower carbon efficiency, as production of pyoil from plastic waste results in a significant amount of gas and char as the conditions are severe. [0010] EP3878926A1 discloses a suspension comprising of a (1) vacuum gas oil and (2) between 1 and 15 wt% of a powder of plastic particles, comprising particles obtainable by cryogenic milling of waste polyethylene and/or waste polypropylene and having a size of smaller than 500 micron. Although the technical solution proposed in this patent application is promising, there is still a scope to improve the characteristics of a feedstock suitable for FCC operation.

[0011] Accordingly, one of the object of the present invention is to provide a hydrocarbon feed stream derived, at least in part, from waste plastic material, which is suitable to be used as a feedstock for fluidized catalytic cracking (FCC) so as to produce high value chemicals at desired conversion and yield while mitigating the extent of coke formation.

[0012] It is yet another objective of the present invention is to improve product conversion and reduce coke formation during fluidized catalytic cracking over traditional FCC feed such as VGO. It is yet another objective of the invention to produce hydrocarbon feed suitable to be used in an FCC unit with minimal energy consumption. It is yet another objective of the present invention to produce one or more cracked hydrocarbon product in an energy efficient manner at high conversion and minimal coke formation using a fluidized catalytic cracking process.

BRIEF DESCRIPTION OF THE DRAWINGS

[0013] For a more complete understanding, reference is now made to the following descriptions taken in conjunction with the accompanying drawings, in which:

[0014] FIG. 1 is a schematic diagram illustrating an embodiment of the present invention, where a process involving a step of diluting the product stream (J) once obtained, with an additional vacuum gas oil feed (AV) in a blending unit (E) and subsequently obtaining the feed stream (H)

[0015] FIG. 2 is a schematic diagram illustrating an embodiment of the present invention, where a process involving a step of passing the product stream (J) once obtained, into a separation unit (C) prior to blending with the additional vacuum gas oil feed (AV) in the blending unit (E), to obtain the hydrocarbon feed stream (H).

[0016] FIG. 3 is a schematic diagram illustrating an embodiment of the present invention, where a process involving the step of supplying the waste plastic feed stream (W) and a vacuum gas oil feed (V) to a de-chlorination unit (B) and forming a stream (D) which is subsequently introduced to the thermal cracking unit (A) to obtain the product stream (J). The schematic diagram further illustrates that the product stream (J) is subsequently diluted with an additional vacuum gas oil feed (AV) in a blending unit (E) to subsequently obtain the hydrocarbon feed stream (H). [0017] FIG. 4 is a schematic diagram illustrating an embodiment of the present invention, where a process involving the use of a de-chlorination unit (B), a separation unit (C), and obtaining the hydrocarbon feed stream (H). The hydrocarbon feed stream (H) is subsequently introduced into the fluidized catalytic cracker (FCC).

[0018] FIG. 5-7 is a graphical representation to show that when the hydrocarbon feed stream (R1-R6) from the example section, comprising oligomeric product (Ol) is used as a feed in fluidized catalytic cracking, the use of such a feed resulted in a decrease in coke at constant conversion compared to a traditional FCC feed comprising only of vacuum gas oil (VGO).

[0019] FIG. 8-10 is a graphical representation to show that when the hydrocarbon feed stream (R1-R6) from the example section, comprising the oligomeric product (Ol) is used as a feed in fluidized catalytic cracking, the use of such a feed results in an increase in propylene (C3 olefin) yield at constant conversion compared to a traditional FCC feed comprising only of vacuum gas oil (VGO).

[0020] FIG. 11-13 is a graphical representation to show that when the hydrocarbon feed stream (R1-R6) from the example section, comprising the oligomeric product (Ol) is used as a feed in fluidized catalytic cracking, the use of such feed resulted in an increase in butenes (C4 olefins) yield at constant conversion compared to a traditional FCC feed comprising only of vacuum gas oil (VGO).

DETAILED DESCRIPTION OF THE INVENTION

[0021] The objectives of the invention are achieved at least in part by a process for producing a hydrocarbon feed stream (H), comprising the steps of:

(i) providing a waste plastic feed stream (W) comprising one or more polymers (Pl);

(ii) supplying the waste plastic feed stream (W) and optionally a vacuum gas oil feed (V) to a thermal cracking unit (A) to thermally crack at least a portion of the waste plastic feed stream (W) and forming a product stream (J), wherein the product stream (J) comprises an oligomeric product (Ol) derived from the one or more polymers (Pl), further wherein the oligomeric product (Ol) has a weight average molecular weight of > 1,000 g/mol and < 20,000 g/mol, preferably > 1,000 g/mol and < 15,000 g/mol, preferably > 2,000 g/mol and < 15,000 g/mol, preferably > 2,000 g/mol and < 10,000 g/mol, preferably > 8,000 g/mol and < 18,000 g/mol, preferably > 9,000 g/mol and < 18,000 g/mol, preferably > 12,000 g/mol and < 18,000 g/mol, as determined with gel permeation chromatography; and

(iii) blending the product stream (J) with an additional vacuum gas oil feed (AV) and obtaining the hydrocarbon feed stream (H).

[0022] Preferably, wherein the hydrocarbon feed stream (H) has an oligomeric product (Ol) content of > 0 and < 20.0 wt.%, with regard to the total weight of the hydrocarbon feed stream (H)

[0023] Alternatively in another embodiment, the invention relates to a process for producing a hydrocarbon feed stream (H), comprising the steps of:

(ii) supplying the waste plastic feed stream (W) and optionally a vacuum gas oil feed (V) to a thermal cracking unit (A) to thermally crack at least a portion of the waste plastic feed stream (W) and forming a product stream (J), wherein the product stream (J) comprises an oligomeric product (Ol) derived from the one or more polymers (Pl), further wherein the oligomeric product (Ol) has a weight average molecular weight of > 8,000 g/mol and < 18,000 g/mol, preferably > 9,000 g/mol and < 18,000 g/mol, preferably > 12,000 g/mol and < 18,000 g/mol as determined with gel permeation chromatography; and

(iii) blending the product stream (J) with an additional vacuum gas oil feed (AV) and obtaining the hydrocarbon feed stream (H), preferably, wherein the hydrocarbon feed stream (H) has an oligomeric product (Ol) content of > 0 and < 20.0 wt.%, with regard to the total weight of the hydrocarbon feed stream (H).

[0024] Alternatively in another embodiment, the invention relates to a process for producing a hydrocarbon feed stream (H), comprising the steps of:

(ii) supplying the waste plastic feed stream (W) and optionally a vacuum gas oil feed (V) to a thermal cracking unit (A) to thermally crack at least a portion of the waste plastic feed stream (W) and forming a product stream (J), wherein the product stream (J) comprises an oligomeric product (Ol) derived from the one or more polymers (Pl), further wherein the oligomeric product (Ol) has a weight average molecular weight of > 12,000 g/mol and < 18,000 g/mol as determined with gel permeation chromatography; and (iii) blending the product stream (J) with an additional vacuum gas oil feed (AV) and obtaining the hydrocarbon feed stream (H), preferably, wherein the hydrocarbon feed stream (H) has an oligomeric product (Ol) content of > 0 and < 20.0 wt.%, with regard to the total weight of the hydrocarbon feed stream (H).

[0025] Preferably the hydrocarbon feed stream (H) has an oligomeric product (Ol) content of > 2.0 wt.% and < 10.0 wt.% and the product stream (J) comprises the oligomeric product (Ol) having a weight average molecular weight of > 12,000 g/mol and < 18,000 g/mol as determined with gel permeation chromatography.

[0026] Advantageously, as seen from the examples in this disclosure, the blending of product stream (J) with an additional vacuum gas oil feed (AV) results in obtaining the hydrocarbon feed stream (H), which when subjected to fluidized catalytic cracking results in higher conversion to commercially valuable hydrocarbons. Accordingly, the inventors propose to combine hydrocarbon feed such as VGO with the oligomeric product stream, as a route to chemically recycle plastics, leading to the production of circular polymers and gasoline components at high conversion rate. Considering that a typical refinery processes approximately 4000 kta (kiloton per annum) of VGO, blending up to 20 wt.% of oligomeric products derived from waste plastics, would allow for the processing of up to approximately 800 kta of plastic.

[0027] As a further advantage, the VGO also plays a role as a ‘solvent’ for the product stream (J), which comprises the oligomeric product (Ol). Although fluidized catalytic cracking is exemplified in this disclosure, the hydrocarbon feed stream (H) is suitable for other types of hydrocarbon cracking such as steam cracking.

[0028] The term “vacuum gas oil” or “VGO” is a term commonly used and understood in petroleum refining and is a composition of a complex combination of hydrocarbons produced by vacuum distillation of the residuum from atmospheric distillation of crude oil.

[0029] Although vacuum gas oil feed (AV) is referred to as additional vacuum gas oil feed, it should be understood that it may be the first use of vacuum gas oil in the process if vacuum gas oil is optionally not present in the thermal cracking step.

[0030] The weight average molecular weight may be measured by any suitable gel permeation chromatography method. Preferably, the weight average molecular weight is determined with gel permeation chromatography using polystyrene standard in accordance with ASTM D5296-11. Oligomeric product (Ol)

[0031] The oligomeric product (Ol) has a higher weight average molecular weight than vacuum gas oil and typical pyoil and pyoil derived products. For the purpose of measuring the weight average molecular weight of the oligomeric product (Ol) using gel permeation chromatography, the contribution from vacuum gas oil is not considered.

[0032] As may be appreciated by a skilled person, in gel permeation chromatography, higher molecular weight component elute first. As a result, the vacuum gas oil fraction should be the last fraction to elute, and the contribution therefrom is not considered when determining the weight average molecular weight of the oligomeric product.

[0033] Without wishing to be bound by any specific theory, the inventors believe that, by lowering the weight average molecular weight through thermal cracking, allows the resultant oligomeric product to easily diffuse into the catalyst pores in an FCC unit. On the other hand, the inventors believe that reducing the polymer particle size via cryogenic milling does not usually lower the weight average molecular weight of the polymer and so the ease with which the milled polymer particle enters the catalyst pores in an FCC unit, is usually lower than that of an oligomeric product, which in turn affects hydrocarbon conversion during the FCC process.

[0034] It is preferred that the product stream (J) is substantially free of pyoil or pyrolysis products. Preferably, the product stream (J) comprises 0.0 wt.% of pyoil or pyrolysis products.

[0035] It is important that the oligomeric product (Ol) has a higher weight average molecular weight than pyoil or products derived from pyrolysis of waste plastics. Pyrolysis oil, including that made from plastic feedstock, is commonly understood to have a weight average molecular weight of less than 1000 g/mol, more likely to be less than 600 g/mol even more likely to be less than 400 g/mol and more likely to be about 200 g/mol, and would require an energy intensive process to produce it resulting in increased capital expenditure as well as operational expenditure to produce such low molecular weight species.

[0036] In addition, there may be some carbon efficiency gains as well, as production of pyoil from plastic waste results in a significant amount of gas and char (the pyoil yield from pyrolysis is typically only -70%). When producing oligomers, the yield is much higher (>90%), as there is minimal gas production since the conditions are less severe. [0037] Further, such pyoil samples have high unsaturated product content (such as aromatics) which may not be suitable for producing hydrocarbons with high conversion with low coke formation in an FCC unit. Pyrolysis oil made from plastics is very nearly a complete depolymerization product, with gases and light oils as the product, having almost no oligomeric component remaining, with a corresponding low weight average molecular weight.

[0038] To demonstrate, commercial pyoil samples from five suppliers were analyzed via a simulated distillation (Simdist) gas chromatographic method. The Simdist method generates a boiling point distribution of the commercial pyoil samples. As pyoil is typically predominantly paraffinic (-50-60 wt%), the inventors herein may correlate the Simdist data to the boiling points of paraffins in order to estimate an average molecular weight of the pyoil sample, as shown in Table 1 below. Note that the presence of aromatics, olefins, and other unsaturated species in the pyoil will tend to decrease the average molecular weight compared to the estimates shown here. Therefore, using paraffin boiling points as the basis to estimate average molecular weight of the pyoil sample is likely to provide higher than actual molecular weights for the pyoil samples and the actual average molecular weights are very likely lower than those shown in Table 1.

Table 1

[0039] Advantageously, the conversion to obtain oligomeric product (Ol) requires lower energy requirements than a process involving pyrolysis, which depolymerizes a polymeric material to a significantly larger degree than what is practiced in the present invention. Therefore, the process of thermal cracking to obtain the oligomeric product (Ol) is not only energy efficient and environmentally less harmful but also renders the process economically efficient in terms of lower capital and operational costs.

[0040] Some depolymerization of plastic is necessary for obtaining the oligomeric product (Ol), as there may be compatibility and processing issues during cracking in the FCC unit of a hydrocarbon feed stream (H) comprising oligomeric product (Ol) having high weight average molecular weight, such as that of most plastics.

[0041] While the oligomeric product (Ol) can have a weight average molecular weight as low as 1,000 g/mol, to fully realize the advantages of the present invention, it is preferable to use one with a higher weight average molecular weight, preferably > 2,000 g/mol, preferably > 8,000 g/mol, preferably > 9,000 g/mol, and preferably > 12,000 g/mol, may be even more preferable, but after considering the amount of plastic sought to be processed.

[0042] It should be understood that as the weight average molecular weight of the oligomeric product (Ol) in the hydrocarbon feed stream (H) increases, it will likely require a lower wt% levels of oligomeric product (Ol) in the hydrocarbon feed stream (H) in order to allow ready processing of hydrocarbon feed stream (H) in a FCC unit.

[0043] Preferably, the product stream (J) comprises > 90.0 wt.%, preferably > 95.0 wt.%, preferably > 98.0 wt.%, preferably > 99.0 wt.%, preferably > 99.5 wt.%, preferably 100.0 wt.% of the oligomeric product (Ol), with regard to the total weight of the product stream (J). [0044] In an aspect of the invention, the process of the present invention, comprises a step of supplying the waste plastic feed stream (W) and the vacuum gas oil feed (V) to the thermal cracking unit (A), to thermally crack at least a portion of the waste plastic feed stream (W) and forming the product stream (J). Preferably > 80.0 wt.%, more preferably > 90.0 wt.%, most preferably 100 wt.% of the waste plastic feed stream (W) is thermally cracked to form the product stream (J).

[0045] The waste plastic feed stream (W) and the vacuum gas oil feed (V) may be blended together to form a thermal cracking stream and subsequently introduced into the thermal cracking unit (A). The waste plastic feed stream (W) and the vacuum gas oil feed (V) may be blended in an amount such that the thermal cracking stream has > 80 wt.%, more preferably > 90 wt.% of the thermal cracking stream.

[0046] In an alternate embodiment, the waste plastic feed stream (W) and the vacuum gas oil feed (V) may be introduced separately into the thermal cracking unit (A) and subsequently cracked under conditions of thermal cracking.

[0047] Referring to FIG. 1, the schematic diagram illustrates an embodiment of the invention, involving the steps of supplying the waste plastic feed stream (W) and the vacuum gas oil feed (V) to a thermal cracking unit (A) to thermally crack at least a portion of the waste plastic feed stream (W) and forming the product stream (J). The product stream (J) is subsequently diluted with an additional vacuum gas oil feed (AV) in a blending unit (E) and obtaining the hydrocarbon feed stream (H)

[0048] Although vacuum gas oil feed (AV) is referred to as additional vacuum gas oil feed, it should be understood that it could be the first use of vacuum gas oil in the process if vacuum gas oil is optionally not present in the thermal cracking step.

[0049] The blending unit (E) may be a mixing chamber where the product stream (J) and additional vacuum gas oil feed (AV) are blended. Alternatively, the blending unit (E) may be system of conduits which enables the product stream (J) to be combined additional vacuum gas oil feed (AV).

Hydrocarbon Feedstream (H)

[0050] The product stream (J) obtained from the thermal cracking unit (A) is blended with the additional vacuum gas oil feed (AV) to obtain the hydrocarbon feed stream (H) having a sufficient amount of vacuum gas oil and the oligomeric product (Ol) suspended in the vacuum gas oil. Preferably, the hydrocarbon feed stream (H) has an oligomeric product (Ol) content in an amount of < 20.0 wt.%, preferably < 15.0 wt.%, preferably < 10.0 wt.%, with regard to the total weight of the hydrocarbon feed stream (H).

[0051] Preferably, the hydrocarbon feed stream (H) has an oligomeric product (Ol) content of > 0.5 wt.% and < 20.0 wt.%, preferably > 0.5 wt.% and < 15.0 wt.%, preferably > 0.5 wt.% and < 10.0 wt.%, preferably > 1.0 wt.% and < 8.0 wt.%, preferably > 2.0 wt.% and < 10.0 wt.%, preferably > 2.0 wt.% and < 5.0 wt.%, with regard to the total weight of the hydrocarbon feed stream (H)

[0052] Preferably, the hydrocarbon feed stream (H) has a vacuum gas oil content of > 80.0 wt.%, preferably > 85.0 wt.%, preferably > 90.0 wt.%, with regard to the total weight of the hydrocarbon feed stream (H). Preferably, the hydrocarbon feed stream (H) has a vacuum gas oil content of > 80.0 wt.% and < 99.5 wt.%, preferably > 85.0 wt.% and < 99.5 wt.%, preferably > 90.0 wt.% and < 99.5 wt.%, preferably > 92.0 wt.% and < 99.0 wt.%, preferably > 90.0 wt.% and < 98.0 wt.%, preferably > 95.0 wt.% and < 98.0 wt.%, with regard to the total weight of the hydrocarbon feed stream (H).

[0053] The additional VGO feed serves as a solvent for the oligomeric product (Ol). If the hydrocarbon feed stream (H) has an oligomeric product (Ol) content of > 20.0 wt.%, the solubility of the oligomer will not be sufficient for further processing in the FCC unit. On the other hand, if the amount of oligomeric product (Ol) is < 0.5 wt.%, the desired conversion to cracked products through FCC operation will not be at desired levels.

[0054] Further, it is estimated that for blends of > 20.0 wt.% of oligomeric product (Ol), a substantial degree of depolymerization is necessary, eliminating the commercial cost savings of partial depolymerization.

[0055] The hydrocarbon feed stream (H) is particularly suited for fluidized catalytic cracker unit (FCC). Preferably the hydrocarbon feed stream (H) comprises:

(a) an atomic chlorine content of < 50.0 ppm by weight, preferably < 40.0 ppm by weight, preferably < 30.0 ppm by weight, preferably < 10.0 ppm by weight, preferably < 0.5 ppm by weight, preferably 0.0 ppm by weight; and/or (b) a total inorganic material content of < 1.0 wt.%, preferably < 0.8 wt.%, preferably < 0.5 wt.%, preferably 0.0 wt.%, with regard to the total weight of the hydrocarbon feed stream (H); and/or

(c) the oligomeric product (Ol) having a weight average molecular weight of > 1,000 g/mol and < 20,000 g/mol, > 1,000 g/mol and < 15,000 g/mol, preferably > 2,000 g/mol and < 15,000 g/mol, preferably > 2,000 g/mol and < 10,000 g/mol, preferably > 8,000 g/mol and < 18,000 g/mol, preferably > 9,000 g/mol and < 18,000 g/mol, preferably > 12,000 g/mol and < 18,000 g/mol, as determined with gel permeation chromatography.

[0056] Preferably the hydrocarbon feed stream (H) comprises:

(a) an atomic chlorine content of < 50.0 ppm by weight, preferably < 40.0 ppm by weight, preferably < 30.0 ppm by weight, preferably < 10.0 ppm by weight, preferably < 0.5 ppm by weight, preferably 0.0 ppm by weight; and/or

(b) a total inorganic material content of < 1.0 wt.%, preferably < 0.8 wt.%, preferably < 0.5 wt.%, preferably 0.0 wt.%, with regard to the total weight of the hydrocarbon feed stream (H); and/or

(c) the oligomeric product (Ol) having a weight average molecular weight of > 8,000 g/mol and < 18,000 g/mol, preferably > 9,000 g/mol and < 18,000 g/mol, preferably > 12,000 g/mol and < 18,000 g/mol, as determined with gel permeation chromatography.

[0057] Preferably the hydrocarbon feed stream (H) comprises:

(a) an atomic chlorine content of < 50.0 ppm by weight, preferably < 40.0 ppm by weight, preferably < 30.0 ppm by weight, preferably < 10.0 ppm by weight, preferably < 0.5 ppm by weight, preferably 0.0 ppm by weight; and

(b) a total inorganic material content of < 0.5 wt.%, preferably 0.0 wt.%, with regard to the total weight of the hydrocarbon feed stream (H); and

(c) a weight average molecular weight of > 12,000 g/mol and < 18,000 g/mol, as determined with gel permeation chromatography.

[0058] Preferably, the oligomeric product (Ol) has a weight average molecular weight of > 2,000 g/mol and < 15,000 g/mol, preferably > 8,000 g/mol and < 18,000 g/mol, preferably > 9,000 g/mol and < 18,000 g/mol, preferably > 10,000 g/mol and < 18,000 g/mol, preferably > 12,000 g/mol and < 18,000 g/mol as determined with gel permeation chromatography [0059] The atomic chlorine may be measured by any suitable method. Preferably as determined in accordance with ASTM UOP 779-08.

[0060] The present inventors found that for the hydrocarbon feed stream (H), when used as a feedstock in a fluidized catalytic cracker (FCC), the feedstock conversion is desirably high while minimizing the extent of coke formation. The inventors found that the hydrocarbon feed stream (H) at similar levels of conversion, produces higher yields of polyolefins as compared to traditional FCC feedstock comprising substantially only of vacuum gas oil (VGO). This is particularly surprising as often high feed conversion leads to increased formation of coke. Advantageously, the invention now enables a skilled person of not only improving the efficiency of a fluidized catalytic cracking process but also a method of effectively using waste plastic materials.

[0061] In an aspect of the invention, the invention relates to a hydrocarbon feed stream (H) obtainable by the process of the present invention. Preferably, wherein the hydrocarbon feed stream (H) comprises:

(c) the oligomeric product (Ol) having a weight average molecular weight of > 1,000 g/mol and < 20,000 g/mol, preferably > 1,000 g/mol and < 15,000 g/mol, preferably > 2,000 g/mol and < 15,000 g/mol, preferably > 2,000 g/mol and < 10,000 g/mol, preferably > 8,000 g/mol and < 18,000 g/mol, preferably > 9,000 g/mol and < 18,000 g/mol, preferably > 12,000 g/mol and < 18,000 g/mol as determined with gel permeation chromatography.

[0062] Preferably, the hydrocarbon feed stream (H) comprises (i) a vacuum gas oil content of > 80.0 wt.% and < 99.5 wt.%, preferably > 85.0 wt.% and < 99.5 wt.%, preferably > 90.0 wt.% and < 99.5 wt.%, preferably > 92.0 wt.% and < 99.0 wt.%, preferably > 90.0 wt.% and < 98.0 wt.%, preferably > 95.0 wt.% and < 98.0 wt.%, with regard to the total weight of the hydrocarbon feed stream (H) and (ii) an oligomeric product (Ol) content of > 0.5 wt.% and < 20.0 wt.%, preferably > 0.5 wt.% and < 15.0 wt.%, preferably > 0.5 wt.% and < 10.0 wt.%, preferably > 1.0 wt.% and < 8.0 wt.%, preferably > 2.0 wt.% and < 10.0 wt.%, preferably > 2.0 wt.% and < 5.0 wt.%, with regard to the total weight of the hydrocarbon feed stream (H).

[0063] Preferably, the hydrocarbon feed stream (H) obtainable by the process of the present invention comprises:

(b) a total inorganic material content of < 1.0 wt.%, preferably < 0.8 wt.%, preferably < 0.5 wt.%, preferably 0.0 wt.%, with regard to the total weight of the hydrocarbon feed stream (H); and

(c) the oligomeric product (Ol) having a weight average molecular weight of > 1,000 g/mol and < 20,000 g/mol, preferably > 1,000 g/mol and < 15,000 g/mol, preferably > 2,000 g/mol and

< 15,000 g/mol, preferably > 2,000 g/mol and < 10,000 g/mol, preferably > 8,000 g/mol and < 18,000 g/mol, preferably > 9,000 g/mol and < 18,000 g/mol, preferably > 12,000 g/mol and < 18,000 g/mol as determined with gel permeation chromatography; and

(d) a vacuum gas oil content of > 80.0 wt.% and < 99.5 wt.%, preferably > 85.0 wt.% and < 99.5 wt.%, preferably > 90.0 wt.% and < 99.5 wt.%, preferably > 92.0 wt.% and < 99.0 wt.%, preferably > 90.0 wt.% and < 98.0 wt.%, preferably > 95.0 wt.% and < 98.0 wt.%, with regard to the total weight of the hydrocarbon feed stream (H); and

(e) an oligomeric product (Ol) content of > 0.5 wt.% and < 20.0 wt.%, preferably > 0.5 wt.% and < 15.0 wt.%, preferably > 0.5 wt.% and < 10.0 wt.%, preferably > 1.0 wt.% and < 8.0 wt.%, preferably > 2.0 wt.% and < 10.0 wt.%, preferably > 2.0 wt.% and < 5.0 wt.%, with regard to the total weight of the hydrocarbon feed stream (H).

[0064] In another aspect of the invention, the invention relates to one or more cracked hydrocarbon products obtainable by a process comprising the steps of:

(ii) supplying the waste plastic feed stream (W) and optionally a vacuum gas oil feed (V) to a thermal cracking unit (A) to thermally crack at least a portion of the waste plastic feed stream (W) and forming a product stream (J), wherein the product stream (J) comprises an oligomeric product (Ol) derived from the one or more polymers (Pl), wherein the oligomeric product (Ol) has a weight average molecular weight of > 1,000 g/mol and < 20,000 g/mol, > 1,000 g/mol and

< 15,000 g/mol, preferably > 2,000 g/mol and < 15,000 g/mol, preferably > 2,000 g/mol and < 10,000 g/mol, preferably > 8,000 g/mol and < 18,000 g/mol, preferably > 9,000 g/mol and < 18,000 g/mol, preferably > 12,000 g/mol and < 18,000 g/mol as determined with gel permeation chromatography;

(iii) blending the product stream (J) with an additional vacuum gas oil feed (AV) and obtaining the hydrocarbon feed stream (H); and

(iv) introducing the hydrocarbon feed stream (H) in a fluidized catalytic cracker unit (FCC) operating under conditions suitable for cracking the hydrocarbon feed stream (H) in presence of a catalyst and obtaining a product stream (FP) comprising one or more cracked hydrocarbon products.

[0065] Preferably, wherein the hydrocarbon feed stream (H) has an oligomeric product (Ol) content of < 20.0 wt.%, with regard to the total weight of the hydrocarbon feed stream (H). [0066] In another aspect of the invention, the invention relates to one or more cracked hydrocarbon products obtainable by a process comprising the steps of:

(ii) supplying the waste plastic feed stream (W) and optionally a vacuum gas oil feed (V) to a thermal cracking unit (A) to thermally crack at least a portion of the waste plastic feed stream (W) and forming a product stream (J), wherein the product stream (J) comprises an oligomeric product (Ol) derived from the one or more polymers (Pl), wherein the oligomeric product (Ol) has a weight average molecular weight of > 12,000 g/mol and < 18,000 g/mol as determined with gel permeation chromatography;

[0067] Preferably, wherein the hydrocarbon feed stream (H) has an oligomeric product (Ol) content of < 20.0 wt.%, with regard to the total weight of the hydrocarbon feed stream (H). [0068] The atomic chlorine may be measured by any suitable method. Preferably as determined in accordance with ASTM UOP 779-08. The hydrocarbon feed stream (H) when obtained from the process of the present invention has a suitable content of inorganic material, a suitable atomic chlorine content and an oligomeric product having a suitable weight average molecular weight. The inventors believe that the low molecular weight oligomeric product present in the hydrocarbon feed stream (H) enables improved catalytic conversion in the FCC unit to produce olefins and other high value chemicals while controlling the extent of coke formation. The content of inorganic material and atomic chlorine is kept within a desirable limit so as to prevent poisoning of the catalyst system in the FCC unit and prevent corrosion of the equipment from the hydrochloric acid generated from a chlorine containing feed.

Waste Plastic Material

[0069] The waste plastic feed stream (W) comprising the polymer (Pl) may be derived, at least in part, from a waste plastic material. Non-limiting examples of waste plastic material include mixed plastic waste (MPW), waste plastic film, agricultural waste, waste generated from construction material, post-industrial waste, post-consumer waste and waste from material recycle facilities (MRFs).

[0070] The vacuum gas oil feed (V) may be any distillate product obtained when distilling under vacuum the distillation residue of an atmospheric distillation of a crude petroleum feedstock. The term distillate product means any product not being the residue or bottom product of the vacuum distillation. A suitable vacuum gas oil has an API gravity of between 19 and 23and an initial boiling point between 255 and 300 °C, a 10% boiling point of between 343 and 393 °C, a 50% boiling point of between 438 and 465 °C, a 90 % boiling point of between 500 and 560 °C and a final boiling point of between 527 and 582 °C. The API gravity may be measured by any suitable method such as ASTM D4052. The boiling point of vacuum gas oil may be measured by any suitable method such as ASTM DI 160.

[0071] The one or more polymer (Pl) may be at least one polymer selected from polyethylene, polypropylene, PS (Polystyrene); PVC (Polyvinyl chloride); PET (Polyethylene terephthalate); PUT (Polyurethanes), PP&A fibres (Polyphthalamide fibres), polyvinylidene chloride, ABS (acrylonitrile-butadiene-styrene), nylon, aramid, fluorinated polymers, and combinations thereof. Preferably, the one or more polymer (Pl) is at least one polymer selected from polypropylene or polyethylene.

[0072] Preferably, the polymer (Pl) is polyethylene. The polyethylene may be a low density polyethylene (LDPE), linear low density polyethylene (LLDPE), high density polyethylene (HDPE). Preferably, the polymer (Pl) is a low density polyethylene (LDPE). Preferably, the polymer (Pl) is a low density polyethylene (LDPE) derived from a waste plastic film. Preferably, the one or more polymer (Pl) is a mixture of polyethylene and polypropylene.

[0073] The one or more polymer (Pl) may have a weight average molecular weight of > 40,000 g/mol and < 500,000 g/mol, preferably > 50,000 g/mol and < 200,000 g/mol, preferably > 50,000 g/mol and < 150,000 g/mol as determined with gel permeation chromatography.

Thermal cracking unit (A)

[0074] The oligomeric product (Ol) is derived from the one or more polymer (Pl). The one or more polymer (Pl) under conditions of thermal cracking is depolymerized to form the oligomeric product (Ol) having a weight average molecular weight lower than that of the one or more polymer (Pl).

[0075] The thermal cracking unit (A) may be operated at a temperature of > 350 °C and < 500 °C, preferably at a temperature of > 370°C and < 450 °C, preferably at a temperature of > 375 °C and < 400 °C and at a feed residence time of > 10.0 minutes and < 80.0 minutes, preferably > 15.0 minutes and < 60.0 minutes, preferably > 25.0 minutes and < 60.0 minutes.

[0076] Preferably, the thermal cracking unit (A) may be operated at a temperature of > 350 °C and < 400 °C and at a feed residence time of > 25.0 minutes and < 60.0 minutes. Preferably, the thermal cracking unit (A) may be operated at a temperature of > 375 °C and < 400 °C and at a feed residence time of > 40.0 minutes and < 60.0 minutes.

[0077] Preferably the thermal cracking of the one or more polymer (Pl) is carried out at a temperature of > 375 °C and < 400 °C and at a feed residence time of > 40.0 minutes and < 60.0 minutes. At such operating conditions the polymer (Pl) is only partially depolymerized.

[0078] The expression “feed residence time” as described herein means the residence time of the waste plastic feed stream (W) and optionally the vacuum gas oil feed (V) inside the thermal cracking unit (A). The thermal cracking unit (A) is configured to operate in a manner such that when the feed residence time is high, the feed comprising the waste plastic feed stream (W) and optionally the vacuum gas oil feed (V) is subjected to a lower cracking temperature. On the other hand, when the feed residence time is low, the feed comprising the waste plastic feed stream (W) and optionally the vacuum gas oil feed (V) is subjected to a higher cracking temperature.

Inorganic Material [0079] The product stream (J) may be passed through a separation unit (C) prior to blending the product stream (J) with the additional vacuum gas oil feed (AV) such that the product stream (J) being blended with the additional vacuum gas oil feed (AV) has a total inorganic material content of < 1.0 wt.%, preferably < 0.8 wt.%, preferably < 0.5 wt.%, preferably 0.0 wt.%, with regard to the total weight of the product stream (J). The separation unit (C) is configured to remove inorganic material from the product stream (J) so that the feed stream (H) has desirably low inorganic material content. The inorganic material is preferred to be kept low so as to prevent a possible deactivation of the catalyst in the FCC unit.

[0080] Non-limiting examples of inorganic material include calcium carbonate (CaCCh), inorganic anti-oxidant, light stabilizers, polymerization catalyst residue, titanium dioxide, silicon based materials, which are typically additives present in polymers.

[0081] The separation unit (C) may be any suitable separation apparatus such as a centrifuge separator or a membrane separation unit. The centrifuge separator may be operated at a temperature of about 150 °C or lower while the membrane separation unit can be operated at about 400 °C or lower.

[0082] Referring to FIG. 2, in some embodiments of the invention, the process involves the step of supplying the waste plastic feed stream (W) and the vacuum gas oil feed (V) to a thermal cracking unit (A) to thermally crack at least a portion of the waste plastic feed stream (W) and forming a product stream (J). The product stream (J) is passed through a separation unit (C) prior to blending with the additional vacuum gas oil feed (AV) in the blending unit (E) and obtaining the hydrocarbon feed stream (H).

De-chlorination

[0083] The waste plastic feed stream (W) being supplied to the thermal cracking unit (A) has an atomic chlorine content of < 50.0 ppm by weight, preferably < 40.0 ppm by weight, preferably < 30.0 ppm by weight, preferably < 10.0 ppm by weight, preferably < 0.5 ppm by weight, preferably 0.0 ppm by weight. The atomic chlorine may be measured by any suitable method. Preferably as determined in accordance with ASTM UOP 779-08.

[0084] In the event, if the chlorine content in the waste plastic feed stream (W) is high, the waste plastic feed stream (W) may be passed through a de-chlorination unit (B) to reduce the atomic chlorine content in the waste plastic feed stream (W). [0085] Preferably, in some embodiments of the invention, the process of the present invention comprises a step of passing the waste plastic feed stream (W) and optionally the vacuum gas oil feed (V) through a de-chlorination unit (B) prior to being supplied to the thermal cracking unit (A), such that the waste plastic feed stream (W) being supplied to the thermal cracking unit (A) has an atomic chlorine content of < 50.0 ppm by weight, preferably < 40.0 ppm by weight, preferably < 30.0 ppm by weight, preferably < 10.0 ppm by weight, preferably < 0.5 ppm by weight, preferably 0.0 ppm by weight.

[0086] Preferably, the process comprises a step of passing both the waste plastic feed stream (W) and the vacuum gas oil feed (V) in the de-chlorination unit (B) and obtaining a stream (D); and supplying the stream (D) to the thermal cracking unit (A), wherein the stream (D) has an atomic chlorine content of < 50.0 ppm by weight, preferably < 40.0 ppm by weight, preferably < 30.0 ppm by weight, preferably < 10.0 ppm by weight, preferably < 0.5 ppm by weight, preferably 0.0 ppm by weight. The stream (D) obtained from the de-chlorination unit (B) and comprises the waste plastic feed stream (W) and the vacuum gas oil feed (V).

[0087] The de-chlorination unit is configured to receive a stream with high concentration of atomic chlorine. For example, the waste plastic feed stream (W) being introduced in the dechlorination unit (B) may have an atomic chlorine content of < 6,000 ppm by weight, preferably < 2,000 ppm by weight, preferably < 1,000 ppm, preferably < 500 ppm by weight, preferably < 200 ppm by weight. The atomic chlorine may be measured by any suitable method. Preferably as determined in accordance with ASTM UOP 779-08.

[0088] The de-chlorination unit (B) may be operated at a temperature of > 250 °C and < 400 °C, preferably at a temperature of > 275 °C and < 325 °C and at a feed residence time of > 10.0 minutes and < 80.0 minutes, preferably > 15.0 minutes and < 60.0 minutes.

[0089] Referring to FIG. 3, in some embodiments of the invention, the process involves supplying the waste plastic feed stream (W) and the vacuum gas oil feed (V) in the de-chlorination unit (B) and forming a stream (D). Subsequently, introducing the stream (D) to the thermal cracking unit (A) and obtaining the product stream (J). The product stream (J) is further diluted with the additional vacuum gas oil feed (AV) in the blending unit (E) and obtaining the hydrocarbon feed stream (H).

Fluidized Catalytic Cracker (FCC) [0090] In some aspects of the invention, the process further comprises the step of introducing the hydrocarbon feed stream (H) in a fluidized catalytic cracker unit (FCC) operating under conditions suitable for cracking the hydrocarbon feed stream (H) in presence of a catalyst and obtaining a product stream (FP) comprising one or more cracked hydrocarbon products.

[0091] Alternatively, the invention relates to a process for producing one or more cracked hydrocarbon products comprising the steps of:

(ii) supplying the waste plastic feed stream (W) and optionally a vacuum gas oil feed (V) to a thermal cracking unit (A) to thermally crack at least a portion of the waste plastic feed stream (W) and forming a product stream (J), wherein the product stream (J) comprises an oligomeric product (Ol) derived from the one or more polymers (Pl), further wherein the oligomeric product (Ol) has a weight average molecular weight of > 1,000 g/mol and < 20,000 g/mol, > 1,000 g/mol and < 15,000 g/mol, preferably > 2,000 g/mol and < 15,000 g/mol, preferably > 2,000 g/mol and < 10,000 g/mol, preferably > 8,000 g/mol and < 18,000 g/mol, preferably > 9,000 g/mol and < 18,000 g/mol, preferably > 12,000 g/mol and < 18,000 g/mol as determined with gel permeation chromatography;

[0092] Preferably, wherein the hydrocarbon feed stream (H) has an oligomeric product (Ol) content of < 20.0 wt.%, with regard to the total weight of the hydrocarbon feed stream (H). [0093] Preferably, the hydrocarbon feed stream (H) has an oligomeric product (Ol) content of > 0.5 wt.% and < 20.0 wt.%, preferably > 0.5 wt.% and < 15.0 wt.%, preferably > 0.5 wt.% and < 10.0 wt.%, preferably > 1.0 wt.% and < 8.0 wt.%, preferably > 2.0 wt.% and < 5.0 wt.%, with regard to the total weight of the hydrocarbon feed stream (H)

[0094] The fluidized catalytic cracker unit (FCC) may be operated at catalyst to oil weight ratio ranging from > 3: 1 to < 10: 1 and at a temperature ranging from > 450 °C and < 750 °C, preferably > 500 °C and < 650 °C. [0095] The reaction time of the feed in contact with the catalyst during the fluidized catalytic cracking ranges from > 15 and < 75 seconds, preferably > 45 and < 65 seconds. The pressure may be maintained at atmospheric pressure.

[0096] The expression “catalyst to oil weight ratio” means the ratio of the weight of the catalyst to the amount of feed that is introduced in the fluidized catalytic cracker unit for cracking (hydrocarbon feed stream (H)).

[0097] The catalyst may be an equilibrium catalyst (E-CAT) comprising at least one of USY zeolite, X-type zeolite, mordenite, Faujasite, nano-crystalline zeolites, MCM mesoporous materials, SBA-15, a silica-alumino phosphate, a gallophosphate, a titanophosphate, ZSM-5 zeolite, RE-Y zeolite, RE-USY zeolite, and CREY zeolite.

[0098] The cracked hydrocarbon products are selected from ethylene, propylene, C4-C30 hydrocarbons, and C6-C30 aromatics, gasoline, LPG, diesel oil, heavy oil, dry gas. Preferably wherein the hydrocarbon feed stream (H) is converted to cracked hydrocarbon products at a conversion of at least > 73.0 % at a catalyst to oil weight ratio of 4.5.

[0099] Preferably wherein the hydrocarbon feed stream (H) is converted to cracked hydrocarbon products at a conversion of at least > 75.0 % at a catalyst to oil weight ratio of 6.0. Preferably wherein the hydrocarbon feed stream (H) is converted to cracked hydrocarbon products at a conversion of at least > 76.0 % at a catalyst to oil weight ratio of 9.1.

[00100] The term “conversion” as used herein can be determined by:

((Total weight of dry gas + LPG + Gasoline products obtained from the fluidized catalytic cracker unit)/Total weight of the hydrocarbon feed stream (H)) x 100.

[00101] For the purpose of calculation, the amount of coke formed is excluded. Dry gas comprises C1-C2 hydrocarbons. Gasoline includes light naphtha, which includes C5-C6 hydrocarbons having boiling point in the range of 30-90 °C and heavy naphtha which includes Ce- C12 hydrocarbons having boiling point in the range of 90-200 °C.

[00102] Accordingly, in an aspect of the invention, the invention relates to the use of the hydrocarbon feed stream (H) as a feed for improving product conversion of a fluidized catalytic cracking process. The term “product conversion” as used herein means conversion to one or more cracked hydrocarbon using fluidized catalytic cracking.

[00103] Referring to FIG. 4, in some embodiments of the invention, the process of the present invention comprises the step of (a) introducing the waste plastic feed stream (W) and the vacuum gas oil feed (V) in the de-chlorination unit (B) and obtaining a stream (D); (b) introducing the stream (D) to the thermal cracking unit (A) and obtaining the product stream (J); (c) passing the product stream (J) into a separation unit (C); (d) blending the resultant stream from step (c) with the additional vacuum gas oil feed (AV) in a blending unit (E) and obtaining the hydrocarbon feed stream (H). Hydrocarbon feed stream (H) is then fed to and processed in FCC unit (FCC).

System

[00104] In an aspect of the invention, the invention relates to a system suitable for producing the hydrocarbon feed stream (H). Preferably, the system comprises:

(a) a thermal cracking unit (A) configured to receive the waste plastic feed stream (W) and optionally vacuum gas oil (VGO) feed (V) to produce the product stream (J);

(b) optionally, a de-chlorination unit (B), wherein the de-chlorination unit (B) is in fluid communication with the thermal cracking unit (A) and wherein the de-chlorination unit is positioned upstream of the thermal cracking unit (A) and wherein the de-chlorination unit (B) is configured to receive the waste plastic feed stream (W) and optionally the vacuum gas oil (VGO) feed (V);

(c) a blending unit (E) configured to blend at least a portion of the product stream (J) stream obtained from the thermal cracking unit (A) and at least a portion of the additional vacuum gas oil feed (AV) to obtain the hydrocarbon feed stream (H); and

(d) optionally, a separation unit (C), wherein the separation unit (C) is in fluid communication with the thermal cracking unit (A) and the blending unit (E) such that the separation unit (C) is positioned downstream to the thermal cracking unit (A) and upstream to the blending unit (E).

[00105] In an aspect of the invention, the invention relates to a system suitable for producing one or more cracked hydrocarbon products. Preferably, the system suitable for producing the one or more cracked hydrocarbon products, comprises:

(c) a blending unit (E) configured to blend at least a portion of the product stream (J) stream obtained from the thermal cracking unit (A) and at least a portion of the additional vacuum gas oil feed (AV) to obtain the hydrocarbon feed stream (H);

(d) optionally, a separation unit (C), wherein the separation unit (C) is in fluid communication with the thermal cracking unit (A) and the blending unit (E) such that the separation unit (C) is positioned downstream to the thermal cracking unit (A) and upstream to the blending unit (E); and

(e) a fluidized catalytic cracker unit (FCC), wherein the fluidized catalytic cracker unit (FCC) is configured to receive the hydrocarbon feed stream (H) and produce one or more cracked hydrocarbon products.

[00106] Operation of a commercial scale fluidized catalytic cracker unit (FCC) may be evaluated in an ACE (Advanced Catalyst Evaluation) unit as described in the patent U.S. 6,069,012 incorporated by reference. The thermal cracking unit may be an autoclave reactor.

[00107] Specific examples demonstrating some of the embodiments of the invention are included below. The examples are for illustrative purposes only and are not intended to limit the invention. It should be understood that the embodiments and the aspects disclosed herein are not mutually exclusive and such aspects and embodiments can be combined in any way. Those of ordinary skill in the art will readily recognize parameters that can be changed or modified to yield essentially the same results.

EXAMPLES

[00108] Purpose: To evaluate the process of the present invention to produce six different hydrocarbon feed stream samples (R1-R6). Subsequently, evaluate the performance of the samples R1-R6, as a feed for fluidized catalytic cracking.

[00109] Material and Equipment: The following material and equipment (Table 2) were used:

Table 2

[00110] Process - Six hydrocarbon feed stream samples (R1-R6) were prepared using the following approach: Approximately 30 grams of shredded black mulch film was placed into an autoclave (thermal cracking unit), which was then sealed and flushed with nitrogen. The temperature was set to the desired operating set point but the stirrer was not started until the temperature of 150 °C was reached (which is above the melting point of the LDPE polymer). At this point, the stirrer was turned on to 250 RPM and held at that value until the end of the run. Thermal cracking was carried out at three different temperatures (375°C, 390 °C for 60 minutes each and 410 °C for 30 minutes) and the product stream (J) was obtained for each of the six samples.

[00111] For each of these six samples, entire contents of the reactor (the product stream (J)) was removed and added to a standard VGO at either the 5.0 wt.% or 10.0 wt.% levels and mixed well at 200 °C producing the hydrocarbon feed stream samples shown in Table 2.

[00112] The sample R1-R6 having a certain amount of oligomeric product suspended in VGO are taken as inventive samples while feed stream comprising only VGO was taken as the comparative (Table 3).

Table 3

[00113] The samples R1-R6 and the pure VGO samples were introduced in the ACE unit for fluidized catalytic cracking. FCC testing was carried out in the ACE unit at 555 °C using an equilibrium catalyst comprising ZSM-5 catalyst and specific Catalyst/Oil ratio. The reaction time of the feed w/ the catalyst is ~60 seconds. The catalyst-to-oil (C/O) ratio was varied between 4 and 10, which is adjusted by changing the catalyst addition amount under a fixed feed injection quantity. Testing was performed at atmospheric pressure. The conversion for each sample at different Catalyst/Oil ratio was noted and reported below in Table 4:

Table 4

[00114] From Table 3, it is evident that for each sample R1-R6 at a given catalyst/oil ratio, the conversion is higher than that of a feed comprising of only pure VGO. For example, the sample R6 at a cat/oil ratio of 4.5 has about 4% higher conversion than a feed stream comprising of only pure VGO (75.57 versus 72.95). Similarly, the sample R6 at a cat/oil ratio of 9.1 has about 3.2% higher conversion than a feed stream comprising of only pure VGO (78.14 versus 75.72).

[00115] FIG. 5-7 show that when the inventive hydrocarbon feed stream (R1-R6) comprising oligomeric product (Ol) is used as a feed in fluidized catalytic cracking, the use of such a feed resulted in a decrease in coke at constant conversion compared to a traditional FCC feed comprising only of vacuum gas oil (VGO). For example, referring to FIG. 5, at conversion range of 75-76%, pure VGO generated undesirably higher coke formation than the feed R1 and R2.

[00116] Further, as evident from FIG. 8-10 show that when the hydrocarbon feed stream (R1-R6) comprising the oligomeric product (Ol) is used as a feed in fluidized catalytic cracking, there is a significant increase in propylene (C3 olefin) yield at constant conversion compared to a traditional FCC feed comprising only of vacuum gas oil (VGO). For example, referring to FIG.8, at a conversion of 74-78%, the amount of propylene generated for the feed R1 and R2 is more than the feed comprising pure VGO.

[00117] FIG. 11-13 show that when the hydrocarbon feed stream (R1-R6) comprising the oligomeric product (Ol) is used as a feed in fluidized catalytic cracking, there is a significant increase in butenes (C4 olefins) yield at constant conversion compared to a traditional FCC feed comprising only of vacuum gas oil (VGO). For example, referring to FIG.11, at a conversion of 74-78%, the amount of C4 olefins generated for the feed R1 and R2 is more than the feed comprising pure VGO.

[00118] From the results obtained from the experiments, it is evident that when the hydrocarbon feed (H) is used in the FCC unit, the extent of conversion to high value products such as LPG and other gasoline, is higher compared to traditional FCC feed such as pure VGO, while minimizing coke formation.

Claims

CLAIMS What is claimed is:

1. A process for producing a hydrocarbon feed stream (H), comprising the steps of:

(ii) supplying the waste plastic feed stream (W) and optionally a vacuum gas oil feed (V) to a thermal cracking unit (A) to thermally crack at least a portion of the waste plastic feed stream (W) and forming a product stream (J), wherein the product stream (J) comprises an oligomeric product (Ol) derived from the one or more polymers (Pl), further wherein the oligomeric product (Ol) has a weight average molecular weight of > 1,000 g/mol and < 20,000 g/mol, preferably > 1,000 g/mol and < 15,000 g/mol, preferably > 9,000 g/mol and < 18,000 g/mol, preferably > 12,000 g/mol and < 18,000 g/mol as determined with gel permeation chromatography; and

2. The process according to claim 1, wherein the hydrocarbon feed stream (H) has an oligomeric product (Ol) content of > 0.5 wt.% and < 20.0 wt.%, preferably > 0.5 wt.% and < 15.0 wt.%, preferably > 0.5 wt.% and < 10.0 wt.%, preferably > 1.0 wt.% and < 8.0 wt.%, preferably > 2.0 wt.% and < 10.0 wt.%, preferably > 2.0 wt.% and < 5.0 wt.%, with regard to the total weight of the hydrocarbon feed stream (H).

3. The process according to any one of claims 1-2, wherein the product stream (J) is passed through a separation unit (C) prior to blending the product stream (J) with the additional vacuum gas oil feed (AV) such that the product stream (J) being blended with the additional vacuum gas oil feed (AV) has a total inorganic material content of < 1.0 wt.%, preferably < 0.8 wt.%, preferably < 0.5 wt.%, preferably 0.0 wt.%, with regard to the total weight of the product stream (J).

4. The process according to any one of claims 1-3, wherein the hydrocarbon feed stream (H) comprises:

(a) an atomic chlorine content of < 50.0 ppm by weight, preferably < 40.0 ppm by weight, preferably < 30.0 ppm by weight, preferably < 10.0 ppm by weight, preferably < 0.5 ppm by weight, preferably 0.0 ppm by weight, preferably as determined in accordance with ASTM UOP 779-08; and/or

5. The process according to any one of claims 1-4, wherein the hydrocarbon feed stream (H) has an oligomeric product (Ol) content of > 2.0 wt.% and < 10.0 wt.% and the product stream (J) comprises the oligomeric product (Ol) having a weight average molecular weight of > 12,000 g/mol and < 18,000 g/mol as determined with gel permeation chromatography.

6. The process according to any one of claims 1-5, wherein the one or more polymer (Pl) is at least one polymer selected from polyethylene, polypropylene, PS (Polystyrene); PVC (Polyvinyl chloride); PET (Polyethylene terephthalate); PUT (Polyurethanes), PP&A fibres (Polyphthalamide fibres), polyvinylidene chloride, ABS (acrylonitrile-butadiene-styrene), nylon, aramid, fluorinated polymers, and combinations thereof; preferably the one or more polymer (Pl) is at least one polymer selected from polypropylene or polyethylene.

7. The process according to any one of claims 1-6, wherein the thermal cracking unit (A) is operated at a temperature of > 350 °C and < 500 °C, preferably at a temperature of > 370°C and < 450 °C, preferably at a temperature of > 375 °C and < 400 °C and at a feed residence time of > 10.0 minutes and < 80.0 minutes, preferably > 15.0 minutes and < 60.0 minutes, preferably > 25.0 minutes and < 60.0 minutes.

8. The process according to any one of claims 1-7, wherein the process comprises a step of passing the waste plastic feed stream (W) and optionally the vacuum gas oil feed (V) through a de-chlorination unit (B) prior to being supplied to the thermal cracking unit (A), such that the waste plastic feed stream (W) being supplied to the thermal cracking unit (A) has an atomic chlorine content of < 50.0 ppm by weight, preferably < 40.0 ppm by weight, preferably < 30.0 ppm by weight, preferably < 10.0 ppm by weight, preferably < 0.5 ppm by weight, preferably 0.0 ppm by weight, preferably as determined in accordance with ASTM UOP 779-08.

9. The process according to any one of claims 1-8, wherein the process further comprises the step of introducing the hydrocarbon feed stream (H) in a fluidized catalytic cracker unit (FCC) operating under conditions suitable for cracking the hydrocarbon feed stream (H) in presence of a catalyst and obtaining a product stream (FP) comprising one or more cracked hydrocarbon products.

10. The process according to claim 9, wherein the fluidized catalytic cracker unit (FCC) is operated at catalyst to oil weight ratio ranging from > 3:1 to < 10:1 and at a temperature ranging from > 450 °C and < 750 °C, preferably > 500 °C and < 650 °C.

11. The process according to any one of claims 9-10, wherein the catalyst is an equilibrium catalyst (E-CAT) comprising at least one of USY zeolite, X-type zeolite, mordenite, Faujasite, nano-crystalline zeolites, MCM mesoporous materials, SBA-15, a silica-alumino phosphate, a gallophosphate, a titanophosphate, ZSM-5 zeolite, RE-Y zeolite, RE-USY zeolite, and CREY zeolite.

12. The process according to any one of claims 9-11, wherein the one or more cracked hydrocarbon products is selected from ethylene, propylene, C4-C30 hydrocarbons, and C6-C30 aromatics, gasoline, LPG, diesel oil, heavy oil, dry gas, preferably wherein the hydrocarbon feed stream (H) is converted to cracked hydrocarbon products at a conversion of > 73.0 % at a catalyst to oil weight ratio of 4.5.

13. A system suitable for producing the hydrocarbon feed stream (H) as claimed in claims 1- 8, the system comprising:

14. A hydrocarbon feed stream (H) obtainable by the process according any one of claims 1- 8, preferably wherein the hydrocarbon feed stream (H) comprises:

(c) the oligomeric product (Ol) having a weight average molecular weight of > 1,000 g/mol and < 20,000 g/mol, > 1,000 g/mol and < 15,000 g/mol, preferably > 9,000 g/mol and < 18,000 g/mol, preferably > 12,000 g/mol and < 18,000 g/mol as determined with gel permeation chromatography.

15. Use of the hydrocarbon feed stream (H) as claimed in claim 14, as a feed for improving product conversion of a fluidized catalytic cracking process.