Description:TECHNICAL FIELD:

[001] The present invention generally relates to the field of Environmental Science and Chemical Engineering. Particularly the present disclosure relates to stream separation, thermal cracking, steam cracking, and selective mild hydrocracking techniques to convert waste tyre-derived pyrolysis oil into high-value chemicals, enabling resource recovery and sustainable waste management.

BACKGROUND:

[002] Waste oil is recognized as a significant environmental hazard, with potential consequences for water pollution. The U.S. Environmental Protection Agency (EPA) states that a single gallon of waste oil can contaminate up to one million gallons of water. Consequently, the proper handling and treatment of waste oil are crucial to mitigate its detrimental effects on the environment. Conventional methods such as regeneration and incineration have drawbacks due to high disposal costs and potential environmental impacts. Therefore, there is a pressing need for a flexible and efficient technique that can effectively eliminate harmful components in waste oil while producing valuable products, all while prioritizing environmental protection.

[003] Annually, an estimated 1.5 billion end-of-life tyres are discarded worldwide, leading to significant environmental and health concerns. Improper disposal of these tyres, including landfilling or burning, contributes to pollution and poses a threat to ecosystems and human well-being. In India alone, approximately 1 million tons of waste tyres are generated each year, further exacerbating the problem.

[004] One of the primary challenges associated with waste tyres is the presence of tyre-derived oil, a byproduct obtained through pyrolysis. This oil, if not effectively managed, can become a source of pollution itself. Traditional disposal methods for waste tyre oil, such as sending it to industrial landfills or incinerators, come with high costs and adverse environmental impacts. Therefore, finding sustainable and economically viable alternatives for waste tyre oil management is crucial.

[005] GB 2024245A discloses a process for producing gaseous and liquid fuels from waste rubber products by dissolving/suspending the scrap rubber in crude oil residues and subjecting to a temperature of 450-580oC and at a pressure of 0.5-11 atm. Liquefaction of scrap rubber is carried out by dissolving in a hot solvent prior to subjecting to Coking process.

[006] US 20210230486A1 discloses a process for converting waste rubber to fuel by pyrolysis followed by condensation to produce pyrolytic oil which is subjected to vacuum steam stripping to produce hydrocarbon fuel.

[007] The present disclosure deals with the need of converting waste tyre oil into valuable chemicals, thereby tackling both the issue of waste tyre disposal and the production of high-value products. By developing a novel process, the invention aims to extract the maximum value from waste tyre oil, transforming it into useful chemicals that can be utilized in various industries. More particularly, this approach not only reduces the environmental impact of waste tyre disposal but also creates economic opportunities by turning waste into a valuable resource. By addressing the challenges associated with waste tyre oil management, the present disclosure contributes to the establishment of a circular economy, where waste is minimized, and resources are efficiently utilized.

OBJECTIVE:
[008] An objective of the present invention is to convert waste tyre oil into value-added chemicals, optimizing resource utilization.

[009] An objective of the present invention is to provide an eco-friendly solution for waste tyre oil disposal, reducing pollution and environmental impact.

[0010] Another objective of the present invention is to offer an alternative feedstock for refineries, promoting resource diversification and sustainable production of specialty chemicals.

SUMMARY:

[0011] This summary is provided to introduce a selection of concepts, in a simplified format, that are further described in the detailed description of the disclosure. This summary is neither intended to identify key or essential inventive concepts of the disclosure and nor is it intended for determining the scope of the disclosure.

[0012] The invention pertains to a novel process which involves the utilization of Tyre Derived Fuel obtained from waste tire pyrolysis as a feedstock. The process employs Mild Hydrocracking catalysts, specifically Nickel-Molybdenum, Cobalt-Molybdenum, or a mixture thereof, supported on Silica-alumina or Zeolite. The overall process comprises three main units: Mild Thermal Cracking, Delayed Coker Unit, and Selective Hydrocracking Unit.

[0013] In the Mild Thermal Cracking unit, waste tire oil undergoes separation in the 1st Separator, resulting in streams with different boiling ranges. Stream (5), with a boiling range of 250°C+, is subjected to mild thermal cracking in the Furnace (6), followed by residence time in the Soaker Vessel (8), resulting in cracked effluent (9). Quenching with Stream (3) halts cracking reactions, and the mixture is sent to a Hydrocyclone (10) for separation into cracked effluent (11) and Coke (12). Stream (11) is further separated in the 2nd Separator (13), yielding various product streams.

[0014] In the Selective Hydrocracking Unit, Stream (17) (boiling range 190-300°C) is mixed with fresh Hydrogen Stream (19) and Recycle Hydrogen stream (25) and heated in furnace (20). The heated stream (21) undergoes mild hydrocracking in the Mild Hydrocracking Reactor (22), leading to the separation of Hydrogen stream (25) and Product stream (26). The latter is subjected to further separation in the 4th Separator (27), resulting in light gas (28), Light Naphtha Stream (29), Heavy Naphtha Stream (30) and stream boiling above 180oC (31). The 190-300°C boiling range stream (17) is recycled and mixed with fresh Hydrogen Stream (19) for reuse.

[0015] Overall, the process described in the invention allows for the conversion of waste tyre-derived pyrolysis oil into valuable chemicals through a series of fractionation, cracking, and separation steps. It employs various reactors, separators, and catalysts to achieve the desired conversions and maximize the utilization of the waste tyre oil.

BRIEF DESCRIPTION OF DRAWINGS:

[0016] These and other features, aspects, and advantages of the present disclosure will become better understood when the following description is read with reference to the accompanying drawings in which like characters represent like parts throughout the drawings wherein:

[0017] Figure 1 illustrates schematic process flow diagram of waste tyre oil conversion to valuable chemicals using thermal cracking and hydrocracking.

[0018] Figure 2 illustrates schematic process flow diagram of waste tyre oil co-conversion with refinery feed stock.

DETAILED DESCRIPTION:

[0019] Those skilled in the art will be aware that the present disclosure is subject to variations and modifications other than those specifically described herein. It is to be understood that the present disclosure includes all such variations and modifications. The disclosure also includes all such features of the invention, and steps of the process that are referred to or indicated in this specification, individually or collectively, and any and all combinations of any or more of such features or steps.

[0020] The articles “a”, “an” and “the” are used to refer to one or to more than one (i.e., to at least one) of the grammatical object of the article. The terms “comprise” and “comprising” are used in the inclusive, open sense, meaning that additional elements may be included. It is not intended to be construed as “consists of only”. Throughout this specification, unless the context requires otherwise, the word “comprise”, and variations such as “comprises” and “comprising”, will be understood to imply the inclusion of a stated element or step or group of elements or steps but not the exclusion of any other element or step or group of elements or steps.

[0021] Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this disclosure belongs. Although any methods and materials similar or equivalent to those described herein can be used in the practice or testing of the disclosure, the preferred methods, and materials are now described. All publications mentioned herein are incorporated herein by reference. The present disclosure is not to be limited in scope by the specific examples described herein, which are intended for the purposes of exemplification only. Functionally equivalent products and methods are clearly within the scope of the disclosure, as described herein.

[0022] The present disclosure provides for the process comprised of liquid hydrocarbon derived from waste tyres, commonly known as Tyre Derived Oils or Tyre Derived Fuel. These oils are obtained through the pyrolysis of discarded tyres, which consist of various materials, including synthetic rubber and natural rubber. The use of these tyre derived oils as a feedstock enables the transformation of waste materials into valuable products.

[0023] In some embodiments of the present disclosure, to facilitate the selective hydrocracking process, mild hydrocracking catalysts are employed. These catalysts, which may include Nickel-Molybdenum, Cobalt-Molybdenum, or a combination thereof, are supported by Silica-alumina or Zeolite. The catalysts play a vital role in promoting the desired chemical reactions and enhancing the efficiency of the hydrocracking process.

[0024] Process conditions:

Mild Thermal Cracking
Furnace Coil Outlet Temperature (COT) to be maintained in the range of ~410-470oC. Residence time inside the Soaker reactor is kept in the range of 10-120 minutes at an operating pressure range of 1-20 Kg/cm2 (g).

Delayed Coker Unit
Furnace Coil Outlet Temperature to be maintained in the range of ~470-520oC. Coke drum overhead temperature may be maintained around 430-460oC. Operating pressure may be maintained in the range of 1-10 Kg/cm2 (g). Hydrocarbon residence time in the drums is kept in the range of 10 to 48 hrs.

Selective Hydrocracking Unit
Hydrocracking occurs in a reactor or series of reactors operated in the temperature range of 350-400oC and pressure of 50-100 bar (g). Liquid Hourly Space Velocity (LHSV) to be maintained in the range of 0.5-2.5 hr-1 & H2/HC ratio of 900-2500 Nm3/m3.

[0025] In some embodiments of the present disclosure, waste tyre oil is initially directed to a 1st Separator, where it undergoes separation into three streams based on their boiling ranges: 190oC- range, 190oC-250oC range, and 250oC+ range (Figure 1). The stream in the 250oC+ range is then heated in a Mild Thermal Cracking Furnace to a mild cracking temperature, resulting in a heated stream. This heated stream is further processed in a Soaker Vessel, allowing for sufficient residence time to undergo thermal cracking and generating an effluent stream. The 190oC- range stream acts as a quench medium to halt cracking reactions. It is mixed with the effluent stream and sent to a Hydrocyclone, where the cracked effluent stream is separated from the coke residue. The cracked effluent stream proceeds to a 2nd Separator, where it is separated into various streams including light gases, a C5-170oC boiling range stream, a 170-190oC boiling range stream, a 190-300oC boiling range stream, and a 300oC+ boiling range stream. The 300oC+ boiling range stream is recycled and combined with the 250oC+ range stream for further processing in the Mild Thermal Cracking Furnace. The 190-300oC boiling range stream is mixed with fresh Hydrogen Stream, heated in a furnace, and directed to a Mild Hydrocracking Reactor. In this reactor, the molecules undergo mild hydrocracking reactions. The resulting product stream is then sent to a 3rd Separator, which separates a Hydrogen stream (recycled and mixed with the 190-300oC boiling range stream) and a Product stream. The Product stream is routed to a 4th Separator, yielding a light gas stream and a Light Naphtha Stream that is directed to the Steam Cracker section. Additionally, a Heavy Naphtha Stream containing aromatic chemicals is mixed with the stream from the 2nd Separator. The 190oC-250oC boiling range stream from the 1st Separator is routed to the Steam Cracker section, where it is subjected to severe thermal cracking temperatures and transformed into light olefins and aromatics. A light boiling fraction with a preferred gasoline boiling range is sent to a 5th Separator, which separates it into a stream with a boiling range of 160oC- and a stream of 190oC+ range. The 160oC-190oC stream is directed to the 2nd Separator, while the light olefins and the stream with a boiling range of 200oC+ are obtained as additional products from the process.

[0026] In some embodiments of the present disclosure, the feedstock used is Tyre Derived Fuel, obtained from pyrolysis of waste tyres, which contains liquid hydrocarbon compounds derived from synthetic rubber, natural rubber, and other tyre components. The selective hydrocracking reactions are facilitated by mild hydrocracking catalysts, including Nickel-Molybdenum, Cobalt-Molybdenum, or a mixture thereof supported by Silica-alumina or Zeolite.

[0027] In some embodiments of the present disclosure, in the mild thermal cracking unit, the furnace coil outlet temperature is maintained within the range of ~410-470oC. The residence time in the Soaker reactor is set between 10-120 minutes, operating at a pressure range of 1-20 Kg/cm2 (g). In the Delayed Coker Unit, the furnace coil outlet temperature is kept in the range of ~470-520oC, with a coke drum overhead temperature around 430-460oC. The operating pressure is maintained between 1-10 Kg/cm2 (g), and the hydrocarbon residence time in the drums ranges from 10 to 48 hours.

[0028] In some embodiments of the present disclosure, for the Selective Hydrocracking Unit, the reactions take place in a reactor or a series of reactors operating at temperatures between 350-400oC and a pressure of 50-100 bar (g). The Liquid Hourly Space Velocity (LHSV) is maintained within the range of 0.5-2.5 hr-1, and the H2/HC ratio is in the range of 900-2500 Nm3/m3.

[0029] In some embodiments of the present disclosure, the process initiates with the acquisition of waste tire-derived pyrolysis oil, which is subsequently fractionated in a primary separator into three distinct streams: Stream (3) with a boiling range below 190°C, Stream (4) with a boiling range between 190-250°C, and Stream (5) with a boiling range exceeding 250°C.

[0030] In some embodiments of the present disclosure, following the fractionation, Stream (5) is directed to a Mild Thermal Cracking Furnace (6), where it undergoes mild thermal cracking reactions, resulting in the generation of a heated stream (7). This heated stream is then routed to a Thermal Cracking reactor (8), providing sufficient residence time for mild thermal cracking reactions, leading to the production of a Thermal Cracking reactor effluent stream (9).

[0031] In some embodiments of the present disclosure, to quench the Thermal Cracking reactor effluent stream (9), Stream (3) with a boiling range below 190°C is combined with the effluent stream and subsequently sent to a hydrocyclone for the separation of vapors and residue.

[0032] In some embodiments of the present disclosure, the process incorporates a second separator (13) that isolates gases (14), a stream boiling in the range of IBP-170°C (15), a stream boiling in the range of 170-190°C (16), a stream boiling in the range of 190-300°C (17), and a 300°C+ boiling range stream (18). The 300°C+ stream (18) is recycled and mixed with Stream (5) for routing to the Mild Thermal Cracking Furnace.

[0033] In some embodiments of the present disclosure, the stream boiling in the range of 190-300°C (17) from the second separator is blended with a fresh hydrogen stream (19), heated in a furnace, and the furnace effluent (21) is directed to a Mild Hydrocracking reactor (22). In this reactor, molecules undergo mild hydrocracking reactions, resulting in a reactor effluent stream (23) that is separated into a hydrogen stream (25), which is recycled and mixed with Stream (17) and stream (19).

[0034] In some embodiments of the present disclosure, the effluent stream from the third separator (24) is directed to a fourth separator (27), which separates gases (28), Light Naphtha Stream (29), Heavy Naphtha Stream (30), and a stream boiling above 180°C (31). The Heavy Naphtha Stream (30) is recycled and routed to the second separator (13).

[0035] In some embodiments of the present disclosure, the Light Naphtha stream (29) from the fourth separator is mixed with Stream (4) boiling in the range of 190-250°C and sent to a Steam Cracker and Product Recovery Section (32) for steam cracking. This process yields C9- chemicals (38), Pyrolysis Fuel Oil (39), and a stream boiling in the range of C9-200°C (33).

[0036] In some embodiments of the present disclosure, the stream boiling in the range of C9-200°C (33) is directed to a fifth separator (34), separating it into 160°C- (35), 160-190°C (36), and 190°C+ (37), wherein the stream boiling in the range of 160-190°C (36) is recycled and routed to the second separator (13).

[0037] In one embodiment of the present invention, the method involves subjecting a mixture of 250°C + (5) fraction of waste tyre derived Pyrolysis Oil (1) and 300oC+ fraction (18) from the 2nd Separator (13) to mild thermal cracking. This is carried out in a specially designed Mild Thermal Cracking Furnace (6), where the temperature is maintained within the range of 410°C to 470°C. The residence time in the Thermal Cracking reactor (8) is controlled within the range of 10-120 minutes. This step facilitates the conversion of the mentioned feedstock into valuable products.

[0038] In another embodiment, the Pyrolysis oil stream (1) is directed towards a Delayed Coker Section. Here, it is co-processed with a residual oil feedstock, which can range from 0.01-20 wt%. This co-processing step enhances the overall efficiency and versatility of the system by allowing the integration of different feedstocks, leading to the production of a diverse range of valuable products.

[0039] Yet another embodiment, process involves the utilization of the 190oC- stream (3) as a quench medium for the Thermal Cracking reactor effluent stream (9). This quenching process helps to control the temperature of the effluent, stabilize the reaction products, and facilitate further downstream processing.

[0040] In embodiment of present disclosure, the mixture of streams (3) and (9), Heavy Naphtha Stream (30), and 160-190oC boiling range stream (36) is directed to a 2nd Separator (13). In this embodiment, the separation process yields gases (14), an Aromatic enriched stream with a boiling range of C5-170oC (15), a Limonene-containing stream boiling in the range of 170-190oC (16), 190-300oC stream (17), and 300oC+ stream (18).

[0041] Building on the previous embodiment, the Aromatic enriched stream (15) is further routed to the Aromatic recovery section of a Steam Cracker and Product recovery section. Additionally, the stream boiling in the range of 190-300oC (17) from the 2nd Separator (13) is subjected to hydrocracking in a Mild Hydrocracking Reactor. This reactor operates at a temperature in the range of 350-400°C and a pressure of 50-100 bar (g). The hydrocracking step enhances the quality and value of the final products obtained from this fraction of the process.

[0042] In some embodiments of the present disclosure, alternatively, the pyrolysis oil stream (1) is directed to a Delayed Coker Section for co-processing with residual oil feedstock in the range of 0.01-20 wt%.

[0043] In some embodiments of the present disclosure, the aromatic-enriched stream (15) obtained from the second separator (13) is routed to the Aromatic Recovery section of the Steam Cracker and Product Recovery section.

[0044] In some embodiments of the present disclosure, the stream boiling in the range of 190-300°C (17) from the second separator (13) undergoes mild hydrocracking in a Mild Hydrocracking Reactor operating at a temperature in the range of 350-400°C and a pressure of 50-100 bar (g).

[0045] In some embodiments of the present disclosure, waste Tyre Oil stream (55) is split into 2 parts; Stream (1) and Stream (56). Stream (56) is mixed with a residual oil stream (40) to form stream (41) which is routed to a Main Fractionator (42). After mixing with an internal recycle, Secondary feed stream (43) from the Main Fractionator (42) is routed to a furnace (44) for heating to thermal cracking temperature. Furnace Outlet stream (45) is routed through (46) or (47) to either of the coke drums (48) or (49) for providing residence time for thermal cracking reactions inside the coke drums. While coke forms inside the Coke drums, Coke drum effluent stream (50) is routed to the Main fractionator (42) for separation into gases (51), Naphtha (52), Gasoil (53) and Fuel oil (54)(Figure 2).

Examples:

[0046] Example 1:
Waste tyre oil sample having property as described in Table-1 was subjected to fractionation into 190oC- (Fraction no. 1) & 190oC+ (Fraction no. 2) boiling fractions. 190oC- fraction was analyzed and analysis of the same is provided in Table-2.

Property Value
C/H/N/S 78.5/10.1/0.94/0.6
P+N/O/A/H2 12.0/38.8/49.2/9.6
Metals, Ni/V <4/<4
5/10/30/50/70/90/95/FBP 139/164/236/307/374/449/474/512
Ash/Moisture/VMC/FC 0.01/12.4/86.2/1.3

Table-1: Property of Waste Tyre Oil

Analysis Fraction no.1
Distillation, wt% vs oC
5 65
10 78
30 112
50 121
70 138
90 166
95 176
Molecular identification, wt%
C6 Cycloalkenes 16.1
Limonene 10.9
Benzene Derivatives 42
Benzene Derivatives
Ethyl Benzene 8.9
m-Xylene 18.6
Substituted Benzene 14.5

Table-2: Property of 190- fraction of Waste Tyre Oil
From Table-2, it can be observed that Limonene content of ~11 wt% and Benzene derivatives ~42 wt% are present in 190- fraction of Waste Tyre Oil.

[0047] Example 2:

Waste tyre oil sample was subjected to mild thermal cracking in a batch reactor as per operating conditions provided in Table-3. Thereafter, gas, liquid and coke products were measured and product yield is provided in Table-3. Liquid product was collected and subjected to fractionation into 190oC- (Fraction no. 3) and 190oC+ fractions (Fraction no. 4). Fraction no. 3 was analyzed and analysis of the same is provided in Table-4.

Parameter Value
Feed Waste tyre oil
Feed weight, gm 300
Temperature, oC 460
Pressure, Kg/cm2 (g) 1
Residence time, hrs 1.5
Yield, wt%
Gas 3.4
Liquid 84.9
Coke 11.7

Table-3: Operating Conditions & Product Yield of Mild Thermal Cracking
Analysis Fraction no.3
Distillation, wt% vs oC
5 74
10 84
30 112
50 117
70 136
90 163
95 176
Molecular identification by Mass Spectroscopy, wt%
C6 Cycloalkenes 10.8
Limonene 13.9
Benzene Derivatives 48
Benzene Derivatives
Ethyl Benzene 12.8
m-Xylene 19.1
Substituted Benzene 16.1

Table-4: Property of 190- fraction of Thermal Cracking Liquid product
It can be observed from Table-2 and 4 that there is an increase in the concentration of Limonene and Benzene derivatives in the Mild Thermal Cracking product of Waste Tyre Oil.
[0048] Example3:

Waste tyre oil sample was subjected to fractionation into 250oC- (Fraction no. 5) and 250oC+ (Fraction no. 6). Fraction no.6 was subjected to mild thermal cracking in a batch reactor as per operating conditions provided in Table-5. Thereafter, gas, liquid and coke products were measured and product yield is provided in Table-5. Liquid product was collected and subjected to fractionation into 190oC- (Fraction no. 7) and 190oC+ fractions (Fraction no.8). Fraction no. 7 was analyzed and analysis of the same is provided in Table-6.

Parameter Value
Feed 250+ fraction of Waste tyre oil
Feed weight, gm 300
Temperature, oC 460
Pressure, Kg/cm2 (g) 1
Residence time, hrs 1.5
Yield, wt%
Gas 2
Liquid 85.2
Coke 12.8

Table-5: Operating Conditions & Product Yield of Mild Thermal Cracking

Analysis Fraction no.7
Distillation, wt% vs oC
5 94
10 107
30 125
50 139
70 159
90 180
95 201
Molecular identification by Mass Spectroscopy, wt%
C6 Cycloalkenes 4
Limonene 10
Benzene Derivatives 47
Benzene Derivatives
Ethyl Benzene 10
m-Xylene 10
Substituted Benzene 27

Table-6: Property of 190- fraction of Thermal Cracking Liquid product
[0049] Example 4:

In a preferred feature of the present invention, waste tyre oil with property as described in Table-1 was processed as per multiple steps described in the embodiment 1 of current invention and the product yield obtained is provided in Table-7.

Component Wt%
Gas 5
Limonene 3
BTX + Ethyl Benzene + Xylene + Substituted Benzenes 22.2
Ethylene 6
Propylene 4
Others (C4 olefins) 6
C5-190 fraction 25.4
180+ fraction 1.4
Py-gas + PGO/PFO 1
Coke 8.5
Recycle 17.5

Table-7: Product yield from the invention.
, Claims:1. A process for converting waste tire-derived pyrolysis oil into valuable chemicals, comprising:
? fractionating the waste tire derived pyrolysis oil (1) in a first separator (2) into three streams boiling in the range of 190°C- (3), 190-250°C (4) and 250°C + (5);
? routing stream (5) to a Mild thermal cracking furnace (6) to obtain a heated stream (7);
? routing the heated stream (7) to a Thermal Cracking reactor (8) to provide sufficient residence time to undergo mild thermal cracking reactions to obtain a Thermal Cracking reactor effluent stream (9)
? Mixing the stream having boiling range 190oC- (3) for quenching the Thermal Cracking reactor effluent stream (9) and routing the mixed stream to a hydrocyclone (10) for separating the vapors (11) and residue (12)
? Routing stream (11) to a 2nd Separator (13) for separation into gases (14), stream boiling in the range of IBP-170oC (15), stream boiling in the range of 170-190 oC (16), stream boiling in the range of 190-300oC (17) and 300oC+ boiling range stream (18) which is recycled and mixed with stream (5) for routing to Mild thermal cracking furnace (6)
? Stream boiling in the range of 190-300oC (17) is mixed with fresh Hydrogen stream (19) and heated in a furnace (20) and furnace effluent (21) is routed to a Mild Hydrocracking reactor (22) wherein molecules is stream (21) undergo mild hydrocracking reactions and the reactor effluent stream (23) is routed to a 3rd Separator (24) to separate Hydrogen stream (25) which is recycled and mixed with stream (17) and stream (19)
? Effluent stream from 3rd Separator (24) is routed to a 4th Separator (27) for separation into gases (28), Light Naphtha Stream (29), Heavy Naphtha Stream (30) and stream boiling above 180oC (31) wherein Heavy Naphtha Stream (30) is routed to the 2nd Separator (13)
? Light Naphtha stream (29) from 4th Separator is mixed with stream boiling in the range of 190-250oC (4) from 1st Separator (2) and routed to a Steam Cracker and Product recovery section (32) for steam cracking to obtain C9- chemicals (38), Pyrolysis Fuel Oil (39) and stream boiling in the range of C9-200oC (33)
? Stream boiling in the range of C9-200 (33) is routed to a 5th Separator (34) for separation into 160oC- (35), 160-190oC (36) and 190oC+ (37) wherein stream boiling in the range of 160-190oC (36) is routed to the 2nd Separator (13).

2. The process as claimed in claim 1, wherein the Pyrolysis Oil stream (1) is obtained from tyres containing natural rubber, synthetic rubber, waste plastic or mixtures thereof.

3. The process as claimed in claim 1-2, wherein stream (4) after mixing with Light Naphtha Stream (29) is directed to a Steam Cracker and Product Recovery Section wherein it is subjected to Steam Cracking in the temperature range of 800-900oC.

4. The process as claimed in claim 1-3, wherein the mixture of 250°C + (5) fraction of waste tyre derived Pyrolysis Oil (1) and 300oC+ fraction (18) from 2nd Separator (13) is subjected to mild thermal cracking at temperature in the range of 410°C to 470°C in a Mild Thermal Cracking Furnace (6) and residence time in the range of 10-120 mins in a Thermal Cracking reactor (8).

5. The process as claimed in claim 1-4, wherein Pyrolysis oil stream (1) is routed to a Delayed Coker Section for co-processing with residual oil feed stock in the range of 0.01-20 wt%.

6. The process as claimed in claim 1-2, wherein the 190oC- stream (3) is used as a quench medium for quenching the Thermal Cracking reactor effluent stream (9).

7. The process as claimed in claim 1-6, wherein the mixture of stream (3) and stream (9), Heavy Naphtha Stream (30) and 160-190oC boiling range stream (36) is routed to a 2nd Separator (13) for Separation into gases (14), Aromatic enriched stream having boiling range of C5-170oC (15), Limonene containing stream boiling in the range of 170-190oC (16), 190-300oC (17) and 300oC+ stream (18).

8. The process as claimed in claim 1-7, wherein aromatic enriched stream (15) is routed to the Aromatic recovery section of Steam Cracker and Product recovery section.

9. The process as claimed in claim 1-8, wherein the stream boiling in the range of 190-300oC (17) from 2nd Separator (13) is hydrocracked in a Mild Hydrocracking Reactor operating at a temperature in the range of 350-400°C and a Pressure of 50-100 bar (g).