Description:FIELD OF INVENTION
[001] The present invention provides a process for production of mono-aromatics from clarified oil. More particularly, it relates to a process that includes aromatic extraction of the feedstock by contacting the feedstock with a solvent in an aromatic extraction unit followed by hydrocracking.

BACKGROUND OF THE INVENTION
[002] Background description includes information that may be useful in understanding the present invention. It is not an admission that any of the information provided herein is prior art or relevant to the presently claimed invention, or that any publication specifically or implicitly referenced is prior art.
[003] Clarified Oil (CLO) is produced from the bottom of Fluid catalytic cracking (FCC) unit. It is rich in poly-nuclear aromatics (PNA) and is a desirable feedstock for the production of premium-grade products such as needle coke or can be used as a cutter stock for marine fuel oil. However, due to high sulfur content and impurities present in it, its application for the desired purpose is limited. Owing to the strict IMO 2020 regulation for sulfur levels in marine fuels of 0.5% in the deep sea and up to 0.1% in the coastal areas, refiners have been investigating several strategies to meet the target.
[004] US10934494B2 describes a process for production of anisotropic coke from clarified oil feedstock. Clarified oil is parallelly routed to extraction and hydrotreating units and the effluent forms the delayed coker feedstock for the production of premium quality anisotropic coke.
[005] WO2000071639A1 discloses a process for hydroconversion of raffinate obtained from clarified oil extraction process. The process further includes solvent dewaxing and hydrofinishing to obtain lube base oil feedstock.
[006] IN202021017031 describes a process for production of light olefins and aromatics from residual hydrocarbon streams. High severity catalytic cracking process produces higher yields of lighter olefins and various boiling fractions, which are subjected to separation of C4 stream from gaseous product followed by metathesis and aromatization to form mono aromatics.
[007] US20130313159A1 relates to a process for improving aromaticity of Clarified slurry oil. The same is subjected to solvent extraction process for extraction of paraffinic rich oil using C2-C7 hydrocarbon and C3-C7 ketones as the solvent. The process claims that the extracted product can be used as a feed in FCC (fluid catalytic cracking), lube oil base stock and as thermic fluid.
[008] WO2016016748A1 discloses a process of separating valuable petroleum products from clarified slurry oil by vacuum distillation with gradual increase in temperature of the distillation column. Vacuum distillation products include diesel, cycle oil, rubber process oil, and petroleum pitch.
[009] IN Appl. No. 606/DEL/2009 relates to a process for production of improved quality feedstock for FCC and industrial carbon material from FCC bottom. In this process, clarified oil is subjected to solvent extraction unit to separate aromatic and paraffinic rich stream. Aromatic rich stream is routed to conventional carbon block manufacturing unit while the paraffinic rich stream is routed to FCC feedstock blending facility.
[0010] While several approaches have been tried in the past, none of the present approaches provide a desired solution as to effectively using the clarified oil, particularly, to obtain mono-aromatics therefrom in a high yield. Therefore, there is a long-standing need in the art of an improved process for production of mono-aromatics from clarified oil (CLO) feedstock.

OBJECTS OF THE INVENTION
[0011] The primary objective of the present invention is to provide a process for production of mono-aromatics from clarified oil.
[0012] Another objective of the present invention is to provide a process for processing CLO feedstock having a high content of polynuclear aromatics and sulfur to increase the mono-aromatic content and reduce the sulfur content.
[0013] It is an object of the present disclosure to provide an upgraded product which can be a potential feedstock to a petrochemical complex.
[0014] It is an object of the present disclosure to provide an aromatic extraction process that yields a Paraffin rich raffinate which can serve as a blend stock for lube refining.
[0015] Yet another object of the present disclosure is to provide a process for production of mono-aromatics from a clarified oil (CLO) feedstock that is facile, economical and industrially applicable.

SUMMARY
[0016] Various embodiments of present disclosure relate to a process for production of mono-aromatics from clarified oil. More particularly, it relates to a process that includes subjecting the feedstock to aromatic extraction by contacting the feedstock with a solvent in an aromatic extraction unit followed by hydrocracking to obtain mono-aromatics.
[0017] According to one aspect of the present disclosure, a process for production of mono-aromatics from Clarified Oil (CLO) is disclosed. The process comprises the following steps:
a. effecting aromatic extraction of the clarified oil (CLO) feedstock (1) to obtain an aromatic rich stream (7) and a paraffin rich raffinate stream (3), the aromatic extraction being effected by contacting the clarified oil (CLO) feedstock with a solvent in an aromatic extraction unit (2);
b. subjecting the aromatic rich stream (7) to a solvent separation unit (8) to recover the solvent (9) and to obtain a solvent free aromatic extract stream (10), said solvent (9) being recycled to the aromatic extraction unit (2);
c. subjecting the paraffin rich raffinate stream (3) to a solvent separation unit (4) to recover the solvent (5) and to obtain a solvent free paraffin rich stream (6), said solvent (5) being recycled to the aromatic extraction unit (2); and
d. hydrocracking the solvent free aromatic extract stream (10) in a hydrocracker (11) to obtain a stream (12) comprising the mono-aromatics.
[0018] In some embodiments, the stream (12) comprising the mono-aromatics is subjected to fractionation in a fractionator (13) to obtain a gaseous product stream (14), a liquid product stream (15) and an unconverted CLO stream (16).
[0019] In some embodiments, the unconverted CLO stream (16) is recycled, at least in part, to the hydrocracker (11).
[0020] In some embodiments, the solvent is selected from N-Methyl Pyrrolidone, Furfural, phenol, Dimethyl Formamide or mixtures there.
[0021] In some embodiments, the ratio between the solvent and the clarified oil (CLO) feedstock is in the range of 1:1 (wt/wt) to 10:1 (wt/wt). In some embodiments, the ratio between the solvent and the clarified oil (CLO) feedstock is in the range of 1:1 (wt/wt) to 2:1 (wt/wt).
[0022] In some embodiments, the step of aromatic extraction is effected at a temperature ranging from 20°C to 120°C for a time period ranging from 0.5h to 4h.
[0023] In some embodiments, the step of hydrocracking is effected at a temperature in the range of 370°C to 470°C, and at a pressure in the range of 40bar to 180bar, for a time period ranging from 2h to 6h.
[0024] In some embodiments, the step of hydrocracking is effected in presence of a hydrocracking catalyst, said hydroprocessing catalyst being a powdered catalyst, an oil soluble catalyst, a dispersed catalyst, a supported catalyst or a combination thereof. In some embodiments, the catalyst is present in an amount ranging from 0.5 wt% to 10 wt%.
[0025] In some embodiments, the catalyst comprises a metal selected from chromium, manganese, iron, cobalt, nickel, zirconium, niobium, molybdenum, tungsten, ruthenium, rhodium, tin, tantalum or combinations thereof.
[0026] In some embodiments, the liquid fraction obtained from the fractionator has high content of monoaromatics with a low sulfur content.
[0027] In some embodiments, the step of hydrocracking is effected in any of: a continuous stirred tank reactor, a fixed bed reactor, an ebullated bed reactor, or a slurry bubble column reactor.
[0028] In some embodiments, 0.01 to 30 wt% of water is used as antisolvent along with the solvent during solvent extraction step.
[0029] Various objects, features, aspects and advantages of the present disclosure will become more apparent from the following detailed description of preferred embodiments, along with the accompanying drawing figures in which like numerals represent like features.

BRIEF DESCRIPTION OF THE DRAWINGS
[0030] The accompanying drawing(s) are included to provide a further understanding of the present disclosure and are incorporated in and constitute a part of this specification. The drawings illustrate exemplary embodiments of the present disclosure and, together with the description, serve to explain the principles of the present disclosure. The diagrams are for illustration only, which thus is not a limitation of the present disclosure.
[0031] FIG. 1 illustrates an exemplary schematic flow diagram of a process for the production of mono-aromatics from clarified oil according to embodiments disclosed herein.

DETAILED DESCRIPTION OF THE INVENTION
[0032] The following is a detailed description of embodiments of the disclosure depicted in the accompanying drawing. The embodiments are in such detail as to clearly communicate the disclosure. However, the amount of detail offered is not intended to limit the anticipated variations of embodiments; on the contrary, the intention is to cover all modifications, equivalents, and alternatives falling within the scope of the present disclosure as defined by the appended claims.
[0033] In the following description, numerous specific details are set forth in order to provide a thorough understanding of embodiments of the present invention. It will be apparent to one skilled in the art that embodiments of the present invention may be practiced without some of these specific details.
[0034] 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.
[0035] The term “about” is defined as being close to as understood by one of ordinary skill in the art. In one non-limiting embodiment the terms are defined to be within 10%, preferably, within 5%, more preferably, within 1%, and most preferably, within 0.5%.
[0036] The terms “wt.%”, “vol.%” or “mol.%” refer to a weight, volume, or molar percentage of a component, respectively, based on the total weight, the total volume, or the total moles of material that includes the component. In a non-limiting example, 10 moles of component in 100 moles of the material is 10 mol. % of component.
[0037] The terms “comprise” and “comprising” are used in the inclusive, open sense, meaning that additional elements may be included. 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 element or steps but not the exclusion of any other element or step or group of element or steps.
[0038] The term “including” is used to mean “including but not limited to”. “Including” and “including but not limited to” are used interchangeably.
[0039] Ratios, concentrations, amounts, and other numerical data may be presented herein in a range format. It is to be understood that such range format is used merely for convenience and brevity and should be interpreted flexibly to include not only the numerical values explicitly recited as the limits of the range, but also to include all the individual numerical values or sub-ranges encompassed within that range as if each numerical value and sub-range is explicitly recited. For example, a temperature range of about 100°C to about 180°C should be interpreted to include not only the explicitly recited limits of about 100°C to about 180°C, but also to include sub-ranges, such as 125°C to 145°C, 130°C to 150°C, and so forth, as well as individual amounts, including fractional amounts, within the specified ranges, such as 122.2°C, 140.6°C, and 141.3°C, for example.
[0040] 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.
[0041] According to one aspect of the present disclosure, a process for production of mono-aromatics from Clarified Oil (CLO) is disclosed. The process comprises the following steps:
e. effecting aromatic extraction of the clarified oil (CLO) feedstock (1) to obtain an aromatic rich stream (7) and a paraffin rich raffinate stream (3), the aromatic extraction being effected by contacting the clarified oil (CLO) feedstock with a solvent in an aromatic extraction unit (2);
f. subjecting the aromatic rich stream (7) to a solvent separation unit (8) to recover the solvent (9) and to obtain a solvent free aromatic extract stream (10), said solvent (9) being recycled to the aromatic extraction unit (2);
g. subjecting the paraffin rich raffinate stream (3) to a solvent separation unit (4) to recover the solvent (5) and to obtain a solvent free paraffin rich stream (6), said solvent (5) being recycled to the aromatic extraction unit (2); and
h. hydrocracking the solvent free aromatic extract stream (10) in a hydrocracker (11) to obtain a stream (12) comprising the mono-aromatics.
[0042] In some embodiments, the stream (12) comprising the mono-aromatics is subjected to fractionation in a fractionator (13) to obtain a gaseous product stream (14), a liquid product stream (15) and an unconverted CLO stream (16).
[0043] In some embodiments, the unconverted CLO stream (16) is recycled, at least in part, to the hydrocracker (11).
[0044] In some embodiments, the solvent is selected from N-Methyl Pyrrolidone, Furfural, phenol, Dimethyl Formamide or mixtures there.
[0045] In some embodiments, the ratio between the solvent and the clarified oil (CLO) feedstock is in the range of 1:1 (wt/wt) to 10:1 (wt/wt). In some embodiments, the ratio between the solvent and the clarified oil (CLO) feedstock is in the range of 1:1 (wt/wt) to 2:1 (wt/wt).
[0046] In some embodiments, the step of aromatic extraction is effected at a temperature ranging from 20°C to 120°C for a time period ranging from 0.5h to 4h.
[0047] In some embodiments, the step of hydrocracking is effected at a temperature in the range of 370°C to 470°C, and at a pressure in the range of 40bar to 180bar, for a time period ranging from 2h to 6h.
[0048] In some embodiments, the step of hydrocracking is effected in presence of a hydrocracking catalyst, said hydroprocessing catalyst being a powdered catalyst, an oil soluble catalyst, a dispersed catalyst, a supported catalyst or a combination thereof. In some embodiments, the catalyst is present in an amount ranging from 0.5 wt% to 10 wt%.
[0049] In some embodiments, the catalyst comprises a metal selected from chromium, manganese, iron, cobalt, nickel, zirconium, niobium, molybdenum, tungsten, ruthenium, rhodium, tin, tantalum or combinations thereof.
[0050] In some embodiments, the liquid fraction obtained from a fractionator has high content of monoaromatics with a low sulfur content.
[0051] In some embodiments, the step of hydrocracking is effected in any of: a continuous stirred tank reactor, a fixed bed reactor, an ebullated bed reactor, or a slurry bubble column reactor.
[0052] In some embodiments, 0.01 to 30 wt% of water is used as antisolvent along with the solvent during solvent extraction step.
[0053] As would be appreciated by a person skilled in the art, various embodiments of the present disclosure pertain to upgradation of Clarified oil. As would be apparent to a person skilled in the art, clarified oil is a combination of hydrocarbons produced as the residual fraction from distillation of the products from a catalytic cracking process, which may consist of hydrocarbons having carbon numbers predominantly greater than C20 and boiling above approximately 350°C (662°F). According to some embodiments of the present disclosure, the clarified oil may have a boiling point in the range of 370°C to 540°C; Conradson carbon residue content in the range of 0.1% to 20wt%, poly-nuclear aromatics in the range of 10% to 90%, asphaltene content ranging from 0.1% to 3wt% and feed sulfur in the range of 2wt% to 8wt%.
[0054] Figure 1 illustrates an exemplary schematic flow diagram of a process for the production of mono-aromatics from clarified oil according to embodiments disclosed herein.
[0055] As it would be evident to a person skilled in the art from the process scheme, the CLO feed (preferably preheated) (1) is routed to aromatic extraction unit (2). In the presence of solvent, extraction is carried out until a chemical equilibrium is attained. Many operational parameters may be controlled during the disclosed process. For example, the process may be carried out at various temperature with varying time.
[0056] The extraction time for the CLO feed in the aromatic extraction unit may vary from 0.5hr-5hr, 0.5hr-4hr 0.5hr-3hr, 0.5hr-2hr. 1hr-5hr, 2hr-5hr or 3hr-5hr. In preferred embodiments, extraction time for the CLO feed in the aromatic extraction unit lies in the range of 0.5hr to 4hr. In more preferred embodiments, extraction time for the CLO feed in the aromatic extraction unit lies in the range of 2hr to 3 hr.
[0057] The extraction temperature for the CLO feed in the aromatic extraction unit may be in the range of 20°C to 120°C, or 30°C to 120°C, 40°C to 120°C, 50°C to 120°C, 60°C to 120°C, 70°C to 120°C, 20°C to 110°C, 20°C to 100°C, 20°C to 90°C, 20°C to 80°C, 20°C to 70°C. In preferred embodiments, the extraction temperature is in the range of 50°C to 70°C.
[0058] Various polar solvents such, dimethylformamide (DMF), dimethylsulfoxide (DMSO), NMP, phenols, etc may be used in the present extraction process. Examples of solvents that may be suitable for use in the present process include but not limited to N-Methyl Pyrrolidone, Furfural, phenol or Dimethyl Formamide or a mixture of any of these.
[0059] Various antisolvents may be used along with the solvent in the solvent extraction process. In preferred embodiments, 0.01 to 30 wt% of water is used as antisolvent along with the solvent during solvent extraction step.
[0060] The solvent to feed CLO ratio may be in the range of 1:1 (wt/wt) to 10:1 (wt/wt) or 1:1 (wt/wt) to 8:1 (wt/wt), or 1:1 (wt/wt) to 7:1 (wt/wt), or 1:1 (wt/wt) to 6:1 (wt/wt), or 1:1 (wt/wt) to 4:1 (wt/wt), or 1:1 (wt/wt) to 3:1 (wt/wt). In preferred embodiment of the present disclosure the solvent to feed CLO ratio may be in the range of 1:1 (wt/wt) to 5:1 (wt/wt). In a more preferred embodiment, the solvent to feed CLO ratio may be in the range of 1:1 (wt/wt) to 2:1 (wt/wt).
[0061] Paraffin rich raffinate stream (3) from the extraction unit (2) is routed to paraffin rich stream solvent recovery unit (4). Recycled solvent (5) is sent back to the extraction unit (2). The solvent free paraffin rich stream (6) may be routed to lube processing unit. The aromatic rich stream (7) from the extraction unit (2) is routed to the aromatic rich stream solvent recovery unit (8). Recovered solvent (9) is recycled back to the extraction unit (2). The solvent free aromatic rich stream (10) is routed to catalytic hydrocracking unit (11).
[0062] The catalytic hydrocracking unit (11) may be operated at various combinations of pressure and temperature. In preferred embodiments, the hydrocracking unit is operated at a temperature in the range of 370°C to 470°C, hydrogen pressure in the range of 40bar to 180bar, catalyst concentration in the range of 0.5 to 10wt% and reaction time in the range of 2hr to 6hr. In some embodiment the hydrocracking unit is operated at a temperature in the range of 400°C to 440°C, hydrogen pressure in the range of 60bar to 150bar, catalyst concentration in the range of 1 to 5wt% and reaction time in the range of 4hr to 6hr.
[0063] The hydrocracked product (12) is routed to the fractionator (13) for separation of gas (14), liquid fraction (15) and unconverted CLO (16). Liquid fraction obtained has high content of monoaromatics with a low sulfur content. The unconverted CLO stream (16) is recycled, at least in part, to the hydrocracker. In some embodiments, as high as 80% of unconverted CLO (16) is recycled back to the hydrocracking unit (11). In some embodiments 20% of this fraction is purged.
[0064] Hydroprocessing catalyst may be advantageously employed in the hydrocracker. As it may be readily determined by those skilled in the art hydroprocessing catalyst may be in the form of powder, oil soluble catalyst, dispersed catalyst or supported catalyst or any combination of these catalysts. In some embodiments hydroprocessing catalyst supports can include but not limited to zeolites, preferably H-ZSM and H-Beta zeolites.
[0065] In preferred embodiments, said metal may be selected from selected from a group consisting of chromium, manganese, iron, cobalt, nickel, zirconium, niobium, molybdenum, tungsten, ruthenium, rhodium, tin, tantalum or the like.
[0066] Hydrocracking reactions can be carried out in any hydrocracking reactor, including but not limited to continuous stirred tank reactors, fixed bed reactors, ebullated bed reactors and slurry bubble column.
EXAMPLES
[0067] The following examples are given to illustrate the present invention and do not limit the scope of the invention.
[0068] Feed CLO used for the examples has the properties given in Table-1

Table-1
Properties Value
Density, g/cc 1.0765
Sulfur, wt% 5.2
KV, mm2/S @40°C 989.1
MCRT, wt% 5.4
SARA fraction, wt%
Saturates 12.4
Aromatics 80.5
Resins 6.6
Asphaltenes 0.5
Aromatic Distribution, wt%
Mono 7.0
Di 19.5
Poly-nuclear 53.7
Boiling fraction, wt%
IBP – 180°C 0.1
180 – 250°C 0
250 – 370°C 0.1
370°C + 89.6

[0069] The said feedstock was subjected to solvent extraction for separating the aromatic-rich and paraffin-rich phase from the CLO. 200g of CLO was employed for the extraction with 400g of NMP as solvent at 60°C for 2hr. Aromatic-rich phase (extract) was separated along with NMP solvent from paraffin-rich phase (raffinate). NMP solvent was separated from the aromatic-rich phase under 20mbar vacuum at 120°C using rotavapor. The total weight percentage of aromatic (extract) and paraffin (raffinate) rich phase obtained was 80% and 20% respectively.
[0070] The extracted aromatic-rich phase was further subjected to hydrocracking using different catalysts.
Example 1
[0071] 160g of aromatic rich CLO was produced from 200g of CLO after solvent extraction and the same was subjected to hydrocracking in the presence of 5 wt% of powdered catalyst (Catalyst 1) and 5 wt% of supported catalyst (Catalyst 2) under the operating conditions of 430°C, 150 bar H2 pressure, and 4hr reaction time. The properties for the product of catalytic hydrocracking of aromatic extracted CLO are given in Table-2.

Table-2
Properties Catalyst 1 Catalyst 2
Mono-aromatics, % 31.1 32.9
Di+ conversion, % 65 59
PNA conversion, % 70 67
Dry Gas + LPG + H2S, % 8.4 9.4
Distillates, % 42.9 39.2
Lube blend stock, % 20.0 20.0
Unconverted CLO, % 27.1 30.7
Coke, % 1.6 0.7
Overall hydrocracking conversion, % 65 62
HDS, % 88 77
Hydrogen Consumption, % 1.6 1.0

[0072] It can be seen from the above example that in the process scheme of present disclosure, the mono-aromatics yield is increased from 7wt% to approximately 31-33% with CLO conversion and HDS activity being in the range of 62 to 65% and 77 to 88%, respectively.
Example 2
[0073] 160g of aromatic rich CLO was produced from 200g of CLO after solvent extraction and the same was subjected to hydrocracking in the presence of 1 wt% of oil soluble catalyst (Catalyst 3) and 5 wt% of supported catalyst (Catalyst 2) under the operating conditions of 440°C, 150bar H2 pressure, and 6hr reaction time. The properties for the product of catalytic hydrocracking of aromatic extracted CLO are given in Table-3.

Table-3
Properties Catalyst 3 Catalyst 2
Mono-aromatics, % 19.9 15.1
Di+ conversion, % 64 59
PNA conversion, % 82 76
Dry Gas + LPG + H2S, % 19.2 18.6
Distillates, % 49.2 43.9
Lube base stock, % 20.0 20.0
Unconverted CLO, % 10.5 17.4
Coke, % 1.1 0.1
Overall hydrocracking conversion, % 86 80
HDS, % 94 94
Hydrogen Consumption, % 1.3 0.3

[0074] It can be seen from the above example that in the process scheme of present disclosure, the mono-aromatics yield is increased from 7wt% to approximately 15-20% with CLO conversion and HDS activity being in the range of 80 to 86% and 94% respectively.

ADVANTAGES OF THE INVENTION
[0075] The proposed invention provides a process for production of mono-aromatics from clarified oil.
[0076] The proposed invention provides a process for processing CLO feedstock having a high content of polynuclear aromatics and sulfur to increase the mono-aromatic content and reduce the sulfur content.
[0077] The proposed invention provides an upgraded product which can be a potential feedstock to a petrochemical complex.
[0078] The proposed invention provides an aromatic extraction process that yields a Paraffin rich raffinate which can serve as a blend stock for lube refining.
[0079] Although the present invention has been described with reference to preferred embodiments, it is submitted that various modifications can be made to the exemplary embodiments without departing from the spirit and scope of the invention.
, Claims:1. A process for production of mono-aromatics from a clarified oil (CLO) feedstock, said process comprising the steps of:
a. Effecting aromatic extraction of the clarified oil (CLO) feedstock (1) to obtain an aromatic rich stream (7) and a paraffin rich raffinate stream (3), the aromatic extraction being effected by contacting the clarified oil (CLO) feedstock with a solvent in an aromatic extraction unit (2);
b. Subjecting the aromatic rich stream (7) to a solvent separation unit (8) to recover the solvent (9) and to obtain a solvent free aromatic extract stream (10), said solvent (9) being recycled to the aromatic extraction unit (2);
c. Subjecting the paraffin rich raffinate stream (3) to a solvent separation unit (4) to recover the solvent (5) and to obtain a solvent free paraffin rich stream (6), said solvent (5) being recycled to the aromatic extraction unit (2); and
d. hydrocracking the solvent free aromatic extract stream (10) in a hydrocracker (11) to obtain a stream (12) comprising the mono-aromatics.
2. The process as claimed in claim 1, wherein stream (12) comprising the mono-aromatics is subjected to fractionation in a fractionator (13) to obtain a gaseous product stream (14), a liquid product stream (15) and an unconverted CLO stream (16).
3. The process as claimed in claim 2, wherein the unconverted CLO stream (16) is recycled, at least in part, to the hydrocracker (11).
4. The process as claimed in claim 1, wherein the solvent is selected from N-Methyl Pyrrolidone, Furfural, phenol, Dimethyl Formamide or mixtures thereof.
5. The process as claimed in claim 1, wherein ratio between the solvent and the clarified oil (CLO) feedstock is in the range of 1:1 (wt/wt) to 10:1 (wt/wt).
6. The process as claimed in claim 1, wherein ratio between the solvent and the clarified oil (CLO) feedstock is in the range of preferably 1:1 (wt/wt) to 2:1 (wt/wt).
7. The process as claimed in claim 1, wherein the step of aromatic extraction is effected at a temperature ranging from 20°C to 120°C for a time period ranging from 0.5h to 4h.
8. The process as claimed in claim 1, wherein the step of hydrocracking is effected at a temperature in the range of 370°C to 470°C and at a pressure in the range of 40bar to 180bar for a time period ranging from 2h to 6h.
9. The process as claimed in claim 1, wherein the step of hydrocracking is effected in presence of a hydrocracking catalyst, said hydroprocessing catalyst being a powdered catalyst, an oil soluble catalyst, a dispersed catalyst, a supported catalyst or a combination thereof.
10. The process as claimed in claim 9, wherein the catalyst is present in an amount ranging from 0.5 wt% to 10 wt%.
11. The process as claimed in claim 9, wherein the catalyst comprises a metal selected from selected from a group consisting of chromium, manganese, iron, cobalt, nickel, zirconium, niobium, molybdenum, tungsten, ruthenium, rhodium, tin, tantalum or combinations thereof.
12. The process as claimed in claim 1, wherein the step of hydrocracking is effected in any of: a continuous stirred tank reactor, a fixed bed reactor, an ebullated bed reactor, or a slurry bubble column reactor.
13. The process as claimed in claim 1, wherein 0.01 to 30 wt% of water is used as antisolvent along with the solvent during solvent extraction step.