FIELD OF THE INVENTION

[0001] The present invention generally relates to aprocess for preparing hydrocarbons and chemicals from waste plastics and biomass. Specifically, the present invention relates to a solvothermal process for producing high quality fuels and chemicals from a feedstock comprising combination of waste plastics and biomass using lignin containing bioliquor as a solvent for hydrothermal liquefaction with transition metal catalyst. The lignin containing bioliquor of the present invention isproduced as a waste stream from 2G-ethanol manufacturing plants.

BACKGROUND OF THE INVENTION

[0002] 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.

[0003] India is a growing consumer of plastics and also produces agricultural residues in billion tons. Both waste plastic and agricultural residues can be converted into energy source as part of circular economy and approach towards renewable fuels and energy independence.

[0004] Owing to the convenience of moulding into different shapes and sizes, low cost, and durability, plastics like polyethylene, polypropylene, teflon, nylon, polyester, polyvinyl chloride, thermoplastic polyurethane, etc., have emerged as the most fundamental commodity for human-life. Plastic waste is produced each year and being non-biodegradable, this plastic wastes are a huge threat to the environment in addition to the already existing pollution. Hence, there is a need to reduce the amount of plastic waste.

[0005] Hydrothermal liquefaction (or solvothermal synthesis in presence of liquor solvent) offers the advantage of pyrolyzing the waste plastics at low temperatures (may be 120 deg C to 400 deg C), and the convenience of using wet waste to form plastic crudeoil, that can be conveniently used as fuel blend with simple upgradation processes.

[0006] Biofuel, Bioprod. Bioref. 9:630-638 (2015) discloses hydrothermal liquefaction (HTL) of sugarcane bagasse using ethanol and black liquor as solvents. However, the oil yield is less and HTL does not utilize a catalyst. [0007] Although there are various studies of hydrothermal liquefaction that emphasis on oil yields and products from various plastic materials at a few isolated hydrothermal liquefaction conditions, still there requires an optimisation on hydrothermal liquefaction temperatures. Recent studies has focused on polyolefins and much less is known about hydrothermal liquefaction of other materials such as polypropylenes, polyethylene Terephthalate (PET), polyestersand so on.

[0008] Municipal solid waste (MSW) mainly consist of mixed plastic waste and some amount of biomass/ bio waste, segregating the plastic and having dedicated process of conversion for each component of MSW will be expensive. Hence, there is a need for a process for converting mixed plastic and biomass waste. India also has significant amount of agricultural residues like wheat straw, rice husk and rice starw etc available which can be converted to energy source.

[0009] Therefore, there is a need to provide a method of producing high quality fuels and chemical from mixedbiomass and waste plastics feedstock which results in ease of conversion, energy recovery, and oil compositions, for different applications.

OBJECTS OF THE INVENTION

[0010] An object of the present invention is to provide a method of solvothermal process for producing high quality fuels and chemicals from a feedstock comprising of combination of biomass and waste plastics using lignin containing bio-liquor as a solvent for liquefaction.

[0011] Another object of the present invention is to provide a method of solvothermal process for producing high quality fuels and chemicals from a feedstock comprising of combination of biomass and waste plastics using lignin containing bioliquor as a solvent for liquefaction wherein the lignin containting liquor is formed from the acid/base pre-treatment of 2G-ethanol plant waste stream.

[0012] Another object of the present invention is to provide a method of solvothermal process for producing high quality fuels and chemicals from a feedstock comprising of combination of biomass and waste plastics using lignin containing bioliquor as a solvent for liquefaction yielding very good oil yieldwith assistance of transisition metal catalyst.

SUMMARY OF THE INVENTION

[0013] The present invention relates to a solvothermal process for producing high quality fuels and chemicals from a feedstock comprising combination of waste plastics and biomass using lignin containing liquor as a solvent for liquefaction. The lignin containing liquor of the present invention is produced as a waste stream from 2G-ethanol manufacturing plants. [0014] In one aspect, the present invention relates to a method of producing fuels and chemicals from a feedstock comprising combination of biomass and waste plastics comprising the steps of:

(a) processing a lignocellulose biomass in a biomass treatment unit to obtain a processed biomass and bio liquor stream and further fermenting the processed biomass in a fermenter to obtain ethanol;

(b) treating the bioliquor stream with acid/base treatments to obtain a processed bioliquor stream;

(c) mixing a feedstock comprising of waste plastics and biomass in a feedstock vessel and introducing the mixed feedstock into a hydrothermal liquefaction reactor;

(d) introducing the bioliquor stream into the hydrothermal liquefaction reactor comprising the mixed feedstock to obtain a mixture,

(e) subjecting the mixuture to hydrothermal liquefaction by adding a transition-metal catalyst to obtain a liquefied product;

(f) collecting the liquefied product in a collection vessel and separating the liquefied product into a gaseous product and a gas-free product stream;

(g) separating the gas-free product stream into oil stream comprising fuels and chemicals, a solid phase and an aqueous phase;

(h) optionally purifying the oil stream to obtain purified oil stream; and

(i) optionally updgrading the purified oil stream to obtain fuels and chemicals.

[0015] In anembodiment of the present invention, the waste plastic is selected from low density polyethylene (LDPE), high density polyethylene (HDPE), linear LDPE, polypropylene (PP), Teflon, nylon, polyester, polyvinyl chloride, thermoplastic polyurethane and combination thereof.

[0016] In another embdoiment of the present invention, the biomass is selected from rice straw, rice husk, saw dust, corn stover and combination thereof.

[0017] In another embodiment of the present invention, the acid is selected from organic acid or inorganic acids, like H2SO4, HC1, oxalic acid at different dilutions; base is selected from sodium hydroxide, KOH and C5-C6 sugar is xylose, arabinose, glucose, fructose and lignin.

[0018] In another embodiment of the present invention, the bioliquor stream comprises of sodium hydroxide and lignin.

[0019] In another embodiment of the present invention, the hydrothermal liquefaction is carried out at a temperature in the range of 120 deg C to 400 deg C. [0020] In another embodiment of the present invention, the hydrothermal liquefaction is carried out at an initial pressure of batch reactor is in the range of 0.1 -0.5 MPa and an in-situ pressure generated is in the range of 10-30 MPa.

[0021] In another embodiment of the present invention, the hydrothermal liquefaction is carried out at a temperature in the range of 180 deg C to 350 deg C.

[0022] In another embodimentof the present invention, the hydrothermal liquefaction is carried out in a time ranging from 5 minutes to 120 minutes.

[0023] In another embodiment of the present invention, the gaseous product obtained from the liquefied product is routed for heat integration with feedstock heating.

[0024] In another embodiment of the present invention, the separating gas-free product stream comprises separating of bleed stream and make-up liquid which is connected with the bio-liquor for further processing.

[0025] In another aspect, the present invention relates to a purification of solid phase obtained from the gas-free product stream comprising the step of:

(a) purifying the solid phase to obtain purified solid product; and

(b) sending the purified solid product to solid char upgradation unit to obtain a final product

[0026] In another aspect, the present invention relates to amethod of upgradation oil stream obtained from the method of claim 1, wherein the upgradation methods are selected from:

(a) mixing the oil stream with petroleum fractions in co-processing unit to obtain the hydrocarbons;

(b) hydrotreating the oil stream in a hydrotreating unit to obtain diesel or jet range fuels;

(c) cracking the oil stream using a fluid catalytic cracking unit in present of a catalyst in presence of a catalysts to obtain light olefins and gasoline additive compounds; and

(d) cracking the oil stream using a steam cracking unit to ethylene and propyleneand aromatics.

[0027] In another embodiment of the present invention, the catalyst used in the fluid catalytic cracking unit is selected from ZSM-5, beta zeolite, y- zeolite or combination thereof. [0028] Various objects, features, aspects and advantages of the inventive subject matter will become more apparent from the following detailed description of preferred embodiments. BRIEF DESCRIPTION OF THE FIGURES

[0029] Figure 1 represents process flow for the catalytic hydrothermal liquefaction of feedstock comprising combination of biomass and waste plastics.

[0030] Figure 2 represents process flow for upgradation of oil stream to valuable chemicals.

[0031] Figure 3 shows the comparative oil yield for the comparative examples and examples 1-2 of the present invention.

DETAILED DESCRIPTION OF THE INVENTION

[0032] The following is a detailed description of embodiments of the disclosure. 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 spirit and scope of the present disclosure as defined by the appended claims.

[0033] Unless the context requires otherwise, throughout the specification which follow, the word “comprise” and variations thereof, such as, “comprises” and “comprising” are to be construed in an open, inclusive sense that is as “including, but not limited to.”

[0034] Reference throughout this specification to “one embodiment” or “an embodiment” means that a particular feature, structure or characteristic described in connection with the embodiment is included in at least one embodiment. Thus, the appearances of the phrases “in one embodiment” or “in an embodiment” in various places throughout this specification are not necessarily all referring to the same embodiment. Furthermore, the particular features, structures, or characteristics may be combined in any suitable manner in one or more embodiments.

[0035] As used in this specification and the appended claims, the singular forms “a,” “an,” and “the” include plural referents unless the content clearly dictates otherwise. It should also be noted that the term “or” is generally employed in its sense including “and/or” unless the content clearly dictates otherwise.

[0036] In some embodiments, the numbers expressing quantities of ingredients, properties such as concentration, reaction conditions, and so forth, used to describe and claim certain embodiments of the invention are to be understood as being modified in some instances by the term “about.” Accordingly, in some embodiments, the numerical parameters set forth in the written description are approximations that can vary depending upon the desired properties sought to be obtained by a particular embodiment. In some embodiments, the numerical parameters should be construed in light of the number of reported significant digits and by applying ordinary rounding techniques. Notwithstanding that the numerical ranges and parameters setting forth the broad scope of some embodiments of the invention are approximations, the numerical values set forth in the specific examples are reported as precisely as practicable.

[0037] The recitation of ranges of values herein is merely intended to serve as a shorthand method of referring individually to each separate value falling within the range. Unless otherwise indicated herein, each individual value is incorporated into the specification as if it were individually recited herein.

[0038] All processes described herein can be performed in any suitable order unless otherwise indicated herein or otherwise clearly contradicted by context. The use of any and all examples, or exemplary language (e.g. “such as”) provided with respect to certain embodiments herein is intended merely to better illuminate the invention and does not pose a limitation on the scope of the invention otherwise claimed. No language in the specification should be construed as indicating any non-claimed element essential to the practice of the invention.

[0039] The headings and abstract of the invention provided herein are for convenience only and do not interpret the scope or meaning of the embodiments.

[0040] The following discussion provides many example embodiments of the inventive subject matter. Although each embodiment represents a single combination of inventive elements, the inventive subject matter is considered to include all possible combinations of the disclosed elements. Thus if one embodiment comprises elements A, B, and C, and a second embodiment comprises elements B and D, then the inventive subject matter is also considered to include other remaining combinations of A, B, C, or D, even if not explicitly disclosed.

[0041] All publications herein are incorporated by reference to the same extent as if each individual publication or patent application were specifically and individually indicated to be incorporated by reference. Where a definition or use of a term in an incorporated reference is inconsistent or contrary to the definition of that term provided herein, the definition of that term provided herein applies and the definition of that term in the reference does not apply.

[0042] Groupings of alternative elements or embodiments of the invention disclosed herein are not to be construed as limitations. Each group member can be referred to and claimed individually or in any combination with other members of the group or other elements found herein. One or more members of a group can be included in, or deleted from, a group for reasons of convenience and/or patentability. When any such inclusion or deletion occurs, the specification is herein deemed to contain the group as modified thus fulfilling the written description that follows, and the embodiments described herein, is provided by way of illustration of an example, or examples, of particular embodiments of the principles and aspects of the present disclosure. These examples are provided for the purposes of explanation, and not of limitation, of those principles and of the disclosure.

[0043] It should also be appreciated that the present invention can be implemented in numerous ways, including as a system, a method or a device. In this specification, these implementations, or any other form that the invention may take, may be referred to as processes. In general, the order of the steps of the disclosed processes may be altered within the scope of the invention.

[0044] Various terms as used herein are shown below. To the extent a term used in a claim is not defined below, it should be given the broadest definition persons in the pertinent art have given that term as reflected in printed publications and issued patents at the time of filing.

[0045] The term, “hydrothermal liquefaction reactor” as used herein refers to a reactor in which a solvent is used at its super critical conditions for hydrothermal liquefaction to convert any organic substance to crude oil and chemicals at moderate temperature and pressure. Generally, the hydrothermal liquefaction process is conducted in a batch type autoclave reactor, that can sustain temperatures upto 500 deg C and pressures upto 32MPa, fitted with an electrically heated furnace, high temperature thermocouple, stirrer, and pressure gauge. The reactor material can be stainless steel (SS3316) and the volume of reactor is anywhere between 0.5 to 1.2 L. The reactor used in this study was a 0.5 L high temperature and high pressure stirred reactor (Parr 4575) with Parr 4848B reactor controller obtained from Parr Instrument Co., Moline, IL, US.

[0046] The term “transition metal catalyst” as used herein refers to a catalyst as prepared in the the patent applications, US20210339235A1 and WO2018235094A1. The transition metal catalyst can be oil soluble catalyst or water soluble catalyst and in the form of powder.

[0047] Typically, the liquefaction of polyolefins begins with the depolymerization reactions that involve the cleavage of C-C or C-H bonds to form oligomers that undego P- scission reactions to give rise to olefins, which on cyclization form cyclic hydrocarbons. These cyclics, on dehydrogenation further give rise to aromatics. There is a possibility of some aromatics undergoing undesirable reactions to form polycyclic aromatic hydrocarbons that are the major precursors for solid char. The biomass liquefaction in the presence of transition-metal catalyst gave more phenolics, and aromatics. Unexpectedly, the coliquefaction of feedstock comprising combination of waste plastic and biomass resulted in high olefins and naphthenes in the present invention.

[0048] In first embodiment, the present invention relates to a method of producing fuels and chemicals from a feedstock comprising combination of biomass and waste plastics comprising the steps of:

(a) processing a lignocellulose biomass in a biomass treatment unit to obtain a processed biomass and bio liquor stream and further fermenting the processed biomass in a fermenter to obtain ethanol;

(b) treating the bioliquor stream with acid/base treatments to obtain a processed bioliquor stream;

(c) mixing a feedstock comprising of waste plastics and biomass in a feedstock vessel and introducing the mixed feedstock into a hydrothermal liquefaction reactor;

(d) introducing the bioliquor stream into the hydrothermal liquefaction reactor comprising the mixed feedstock to obtain a mixture,

(e) subjecting the mixuture to hydrothermal liquefaction by adding a transition-metal catalyst to obtain a liquefied product;

(f) collecting the liquefied product in a collection vessel and separating the liquefied product into a gaseous product and a gas-free product stream;

(g) separating the gas-free product stream into oil stream comprising fuels and chemicals, a solid phase and an aqueous phase;

(h) optionally purifying the oil stream to obtain purified oil stream; and

(i) optionally updgrading the purified oil stream to obtain fuels and chemicals.

[0049] In another embodiment of the present invention, the figure 1 shows the flow scheme for the catalytic hydrothermal liquefaction of waste plastic and biomass in the presence of solvent and a transition metal catalyst to valuable chemicals and fuels in accordance with the present disclosure. According to the present invention, the feedstock comprising combination of biomass and waste plastic is stored or mixed in the feed hopper combined with feeder(3) which is introduced into the hydrothermal liquefaction reactor (HTL) reactor (4). The lignocellulosic biomass is initially processed in the biomass pretreatment unit (1) where acid/base pre-treatment occurs and then, the C5-C6 sugars (b), constituting cellulose and hemicellulose are sent into a fermenter (2), where the ethanol (c) is the main product along with a lignin containing liquor stream (d). This bio-liquor (d) is composed of sodium hydroxide and lignin and is passed to the hydrothermal liquefaction reactor (HTL) reactor (4) comprising of mixed feedstock. A transition-metal catalyst (e) is added in to the HTL reactor. The liquefaction takes place at a temperature in the range of 120 deg C to 400 deg C and at a pressure in the range of 120-300 bar, and for a residence time 5 min to 120 min to obtain a liquefied product (mixture of solid char, aqueous phase and oil phase) (f). This liquefied product (f), obtained during the hydrothermal liquefaction is sent into a product collector vessel (5), where the gaseous product (g) may be collected, may be sent to vent, may be routed for heat integration with feedstock heating. The gas -free product stream (i) is sent into a liquid- solid separator (6), where there may be a single stage or multistage separation procedures. The mixed plastic and biomass crude stream (j) is separated from the solid phase (n) and the aqueous phase (k). A bleed stream (1) and make-up liquid (h) are also separated.

[0050] In another embodiment of the present invention, the oil phase (j) can be purified or processed in (7) and final oil (m) can be sent for upgradation or blending into drop in fuel/ co-processed in refinery units like fluid catalytic cracking or hydrocracking/ hydrotreater.

[0051] In another embodiment of the present invention, the solid phase (n) is sent into a purification unit (8), where the solid phases is purified and the raw char stream(o) is sent into solid char upgradation unit (9) to obtain a final product which can be used as a catalyst support (p) or for bio-remediation aid(q). The solid char upgradation unit can use steam, KOH or any other activation agent for improving surface area and physical propertirs of raw char stream.

[0052] In an embodiment of the present invention, the waste plastics can be selected from be low density polyethylene (LDPE), high density polyethylene (HD PE) linear LDPE, polypropylene (PP), polyethylene terephthalate (PET), Teflon, nylon, polystyrene, polyester, polyvinyl chloride, thermoplastic polyurethane or combination thereof. Preferably, the feedstock of waste plastics can be polypropylene (PP), Polyethylene Terephthalate (PET), Teflon, nylon, polyester, polyvinyl chloride or combination thereof.

[0053] In an embodiment of the present invention, the biomass for feedstock is selected from any of the different kinds of lignocellulosic biomass categories - hardwood, softwood, grasses and agricultural wastes. Examples of such biomass are poplar, oak, eucalyptus, pine, douglas fir, spruce, wheat straw, barley hull, barley straw, rice straw, rice husks, oat straw, ray straw, corn cobs, corn stalks, sugarcane bagasse, sorghum straw, grass, switch grass and so on or combination thereof. Preferably, the biomass for feedstock is selected from rice straw, rice husk, saw dust, com stover, wheat straw, com cobs, bagasse, municipal solid waste and combination thereof. [0054] In an embodiment of the present invention, the bioliquor streamcan be formed from the acid/base pre-treatment of 2G-ethanol plant waste stream, as a solvent for the process, that aids in improving the plastic crude oil yield, and also producing alcohols, olefins, naphthenes and paraffins in ranges that are useful for being used for lube oil preparation, bitumen blending, surfactants, detergents, fuels and petrochemical feedstock and so on.

[0055] In an embodiment of the present invention, the the transition metal based oilsoluble catalyst or powdered catalyst is in the concentration of 1-20 wt% of solids loading for enhancing the quality of the crude towards fuel oils and lubricating oils.

[0056] In another embodiment of the present invention, the bio-liquor stream comprises of 1% to 10 wt % sodium hydroxide (NaOH) and lignin about 2 to 30 wt% and can be associated with lignin concentration step using multi effect evaporation.

[0057] In an embodiment of the present invention, the liquefaction takes place at a temperature in the range of 120 deg C to 400 deg C. Preferably, at a temperature in the range of 180 deg C to 350 deg C. More preferably, at a temperature in the range of 300 deg C to 350 deg C.

[0058] In an embodiment of the present invention, the liquefaction takes place at apressure in the range of 2 to 30 MPa. Preferably, at a pressure in the range of 15 to 25MPa. More preferably, at apressure in the range of 20 to 25MPa.

[0059] In another embodiment of the present invention, the reacting bio-liquor stream in the hydrothermal liquefaction reactor is carried out in a time ranging from 5 minutes to 120 minutes. Preferably, in a time ranging from 10 minutes to 60 minutes. More preferably, in a time ranging from 10 minutes to 20 minutes.

[0060] In an embodiment of the present invention, the catalyst used in the liquefaction can be present in the concentration range of 0.1-10 wt% of solids loading for enhancing the quality of the plastic crude towards fuel oils and lubricating oils.

[0061] According to the present invention, the method of converting of mixed feedstock of biomass to fuels and chemicals provides oil stream in range of 65% to 75% yield.

[0062] In an embodiment of the present invention, the method of converting of mixed feedstock of biomass to fuels and chemicals produces valuable fuel compounds, olefins and aromatics.

[0063] In an embodiment of the present invention, the fuels and chemicals are selected from the aromatic, alcohol, alkane, alkene, cycloalkane, phenols and ketonic. [0064] In an embodiment of the present invention, the method of converting of mixed feedstock to fuels and chemicals produces olefins, and naphthenes that are useful for lube oil preparation, bitumen blending, surfactants, detergents, fuels and petrochemical feedstock and the like.

[0065] In an embodiment of the present invention, the method of converting of mixed feedstock to fuels and chemicals produces valuable chemicals in significantly higher quantity. [0066] In antoher aspect, the present invention relates to a method of upgrading the crude oil stream, wherein the upgradation methods are selected from:

(a) mixing the oil stream with petroleum fractions in co-processing unit to obtain the hydrocarbons;

(b) hydrotreating the oil stream in a hydrotreating unit to obtain diesel or jet range fuels;

(c) cracking the oil stream using a fluid catalytic cracking unit in present of a catalyst in presence of a catalysts to obtain light olefins and gasoline additive compounds; and

(d) cracking the oil stream using a steam cracking unit to ethylene and propylene.

[0067] According to the present invention, figure 2 shows the flow scheme of upgradation techniques for the products obtained from the solvothermal synthesis of waste plastics in the presence of bio-liquor solvent. The oil stream (j) can be purified or processed in unit (2a) . Unit (2a) can be a coprocessing unit, where the oil stream mixed with petroleum fractions like vacuum gas oil and heavy gas oil and processed to obtain the upgraded fuels or chemicals. Also, unit (2a) can be a hydrotreating unit for converting crude oil stream into diesel/jet range fuels. Unit (2a) can also be a fluid catalytic cracking unit, where crude oil streamcan be cracked in presence of catalysts like zeolites (ZSM-5, beta zeolite, y- zeolite etc) to light olefins and gasoline additive compounds. Unit (2a) can also be a steam cracking unit, where crude oil stream can be steam cracked to produce ethylene and propylene

[0068] In an embodiment of the present invention, the updgradation of oil stream (j) comprising the step of purifiying oil stream (j) in unit (2a) to obtain purified oil stream.

[0069] In an embodiment of the present invention, the updgradation of oil stream (j) comprising the steps of:

(a) purifiying oil stream (j) in unit (2a) to obtain purified oil stream; and

(b) carrying out paraffins purification in unit (5a) to obtain paraffin stream (el).

[0070] While the foregoing describes various embodiments of the disclosure, other and further embodiments of the disclosure may be devised without departing from the basic scope thereof. The scope of the invention is determined by the claims that follow. The invention is not limited to the described embodiments, versions or examples, which are included to enable a person having ordinary skill in the art to make and use the invention when combined with information and knowledge available to the person having ordinary skill in the art.

EXAMPLES

[0071] The present invention is further explained in the form of following examples. However, it is to be understood that the following examples are merely illustrative and are not to be taken as limitations upon the scope of the invention.

[0072] The biomass used in the present invention is procured from the local animal feed market in Devangonthy, Bengaluru.

[0073] Preparation 1 - Feedstock Prepration

[0074] Biomass waste used is secured from the agriculture fields in the neighboring rural areas of the city. The agriculture waste (usually consists of rice husk, or rice straw etc.) is used directly in the experimentations without any pre-treatment or pre-processing stages.

[0075] Bio-liquor is produced as a waste stream from the 2G-ethanol plants. This is further sent for acid pre-treatment so as to concentrate the lignin content in the stream.

[0076] Sulfuric acid (2 g) is taken for about 200 ml of untreated bioliquor. This solution is made up to 600 ml using water. Around 150 g biomass is added to this solution and is soaked for 30min to 1 hour. The soaked liquor is then cooked in a reactor for 15 to 30 min at a temperature of 200 deg C. Later, after it cools down, residue is squeezed manually, and the waste liquor of about 400 ml is produced which is disposed. Now, the solid residue which is containing about 200 ml liquor is taken, and to this, about 2% sodium hydroxide solution is added. For 1 eq of the solid residue, an equal amount of sodium hydroxide solution is added and left for some time. Further, the process of manual squeezing is done so as to neutralize the solid residue, and bring down its moisture content to below 100g. Now, a 3% solution is prepared and 300 ml sodium hydroxide is added to it. This solution is then cooked for 1 hour at a temperature of 200 deg C to get a final bio-liquor solution.

[0077] The bio-liquor solution obtinaed is used as a low cost fuel, but, in this innovation, it is being used as a solvent for the hydrothermal liquefaction of biomass, as the linin content in the liquor aids in forming very useful bio-crude oil, that can be further used as a diesel or gasoline blend.

[0078] Preparation 2 - Synthesis of transition-metal catalyst

[0079] For the metal precursor, about 100g molybdic acid is taken and a solution is prepared. To this, 100g of 2-ethyl hexanoic acid (first additive) solution was added and refluxed at 180 °C for 4 hours to obtain the dark black color salt. The salt obtained was cooled and re-dissolved in 150 g of 2-ethyl hexanol (second additive) and heated with reflux at 180 °C for 12 hours to obtain the Mo(O), (2-ethyl hexanoate)2-ethyl hexanolate). About 340g was produced with the Mo percentage around 14 %.

[0080] Preparation 3 - Synthesis of transition-metal catalyst

[0081] To a solution of iron (III) nitrate (1 eq.) in water and hexane (1:2 ratio; 5 ml per 1 mmol of Fe salt), sodium 2-ethyl hexanoate (3 eq.) in water (solution of 1 mmol in ImL water) was added drop wise at 70 °C and the solution was refluxed for 3 h at 80 °C. The resulting reaction mixture was cooled and fractionated between water/hexane layers. The organic layer was washed with the water. The organic phase was dried (Na2NOs), concentrated in vacuo to afford the catalyst, iron ethyl-hexanoate as a gummy solid.

[0082] Example 1:

[0083] Solvothermal liquefaction of polyproylene (PP) plastics, agri residue rice straw and lignin containing liquor solventas feed and molybdenum oil-soluble catalyst were performed in a high pressure high temperature 500 mL autoclave (Parr 4848B model, USA) equipped with a pressure sensor, J-type thermocouple and an external electric furnace, where the heating system is controlled by a PID controller.

10g of Waste polypropylene (solid to solvent ratio of 1:4) and 10g of rice straw is mixed with lignin containing bio-liquor solvent (80g) obtained from rice strawin feedstock vessel. Molybdenum oil-soluble catalyst (0.2g) and the feedstock from feedstock vessesl are loaded into the reactor. The reactor was purged with nitrogen gas to maintain an inert homogeneous atmosphere. A pressure test was carried out to ensure the reactors and lines are securely sealed and no leak was observed. Initial pressure of the reactor was kept at atmospheric pressure, and stirrer speed was adjusted to 350 rpm. Reactor was then allowed to reach the desired reaction temperature of 593 deg K with increments of 10 deg K/min. Once the temperature is reached, the reactor is kept at the desired temperature for residence time of 15 minutesat the pressures of 23-25 MPa. On the completion of the reaction, the autoclave is immediately cooled to room temperature with an external cooling bath. After the gas samples were collected for analysis using gas bags, the pressure was released from the reactor through vent. For the separation process, the contents of the reactor and the stirrer are washed thoroughly with a solvent dichloromethane for three times. The mixture was filtered with the help of buchner filter funnel, to remove the solids from the liquid phase. Two layers are observed in the separating funnel, where the oil stream is separated from the aqueous stream. Oil stream is extracted from the liquid samples by separating the solvent in a rotary vacuum evaporator (Buchi Rotavapor). The compounds obtained in the oil stream is given in the table 1 below.

Table 1: List of all major compounds

Table la: List of all major chemical group compounds

[0084] The following examples were produced using the above experimental procedures with appropriate conditions, and starting material as given in the table below with non-critical variations.

[0085] Example 2: [0086] Biomass (rice husk (RH)); Waste plastic (polypropylene (PP)); Solvent

(Bioliquor) and Mo oil solubleCatalyst

Table 2: List of all major compound Table 2a: List of all major chemical group compounds

[0087] Comparative example -1 (CE-1):

[0088] Biomass (rice husk (RH)); Waste plastic (polypropylene (PP)); Solvent (water) and No Catalyst

Table 3: List of all major compounds

Table 3a: List of all major chemical group compounds

[0089] Comparative example -2 (CE-2): [0090] Biomass (rice straw (RS)); Waste plastic (polypropylene (PP)); Solvent (water) and No Catalyst

Table 4: List of all major compounds

Table 4a: List of all major chemical group compounds

[0091] Results :The yield of the oil stream obtained from the method of the present invention is provided in the table 5 and figures 3. The yields of the solid residue and oil formed were calculated from the below reactions:

XSR % = (Weight of Solid Residue x 100) / Weight of feedstock — (1)

XOIL %= (Weight of Oil x 100) / Weight of feedstock - (2)

[0092] The results clearly demonstrated that the process of present invention provides high yield of the oil stream when compared to the comparative examples. Furhter, the final product may have organic compounds which may have dissolved in aquoues phase which resulted in low oil yield in the comparative examples.

Table 5: Comparative table

T-Temperature, P-Pressure [0093] A skilled artisan will appreciate that the quantity and type of each ingredient ingredients can be used in different combinations or singly. All such variations and combinations would be falling within the scope of present disclosure

[0094] The foregoing examples are merely illustrative and are not to be taken as limitations upon the scope of the invention. Various changes and modifications to the disclosed embodiments will be apparent to those skilled in the art. Such changes and modifications may be made without departing from the scope of the invention.

ADVANTAGES OF THE PRESENT INVENTION

[0095] The present invention provides a method of converting of mixed feedstock of biomass to fuels and chemicals which gives high yield of oil stream. [0096] The present invention provides a method of converting of mixed feedstock of biomass to fuels and chemicalswhich gives high yield of olefins and naphthenes. [0097] The method of present invention shows synergestic effect and results in high yield of oil compared to when biomass and plastics are treated independently.

[0098] The method present invention can be utilized for conversion of MSW which is hard to seggreagte from plastics.