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WO2025062423A1 - Valorisation de matières plastiques en carburants et produits chimiques à valeur ajoutée - Google Patents

Valorisation de matières plastiques en carburants et produits chimiques à valeur ajoutée Download PDF

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Publication number
WO2025062423A1
WO2025062423A1 PCT/IN2024/051779 IN2024051779W WO2025062423A1 WO 2025062423 A1 WO2025062423 A1 WO 2025062423A1 IN 2024051779 W IN2024051779 W IN 2024051779W WO 2025062423 A1 WO2025062423 A1 WO 2025062423A1
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WO
WIPO (PCT)
Prior art keywords
kiln
hydrocarbons
receptacle
condenser
lighter
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PCT/IN2024/051779
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English (en)
Inventor
B.V. Satish Kumar
B. Sheela
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Individual
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Publication of WO2025062423A1 publication Critical patent/WO2025062423A1/fr
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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J11/00—Recovery or working-up of waste materials
    • C08J11/04—Recovery or working-up of waste materials of polymers
    • C08J11/10—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation
    • C08J11/12—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation by dry-heat treatment only
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
    • C10B47/02—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with stationary charge
    • C10B47/06—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with stationary charge in retorts
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/07—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of solid raw materials consisting of synthetic polymeric materials, e.g. tyres
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/006—General arrangement of incineration plant, e.g. flow sheets
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/44—Details; Accessories
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/12—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of plastics, e.g. rubber
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B2101/00—Type of solid waste
    • B09B2101/75—Plastic waste
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • B09B3/40—Destroying solid waste or transforming solid waste into something useful or harmless involving thermal treatment, e.g. evaporation
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J2323/00—Characterised by the use of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond; Derivatives of such polymers
    • C08J2323/02—Characterised by the use of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond; Derivatives of such polymers not modified by chemical after treatment
    • C08J2323/04—Homopolymers or copolymers of ethene
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/40—Gasification
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2209/00—Specific waste
    • F23G2209/28—Plastics or rubber like materials

Definitions

  • the present invention relates to a process for the upcycling of plastics including industrial plastics and municipal plastic wastes, into fuels and value-added chemicals.
  • Plastics formed by the polymerization of multiple molecules are decomposed into small molecular hydrocarbon compounds through pyrolysis carried out at high temperatures.
  • the plastic wastes are contained in a reaction container and thermal energy is provided to heat the reaction container, so that the plastic wastes in the reaction container are melted and then gasified and pyrolyzed into a variety of small hydrocarbon compounds.
  • the temperature and pressure of the reaction container are required to be accurately controlled, wherein the temperature of the reaction container, too high or too low, will adversely affect the reacting plastic and the efficiency of the whole process.
  • US 11518940 relates to a plastic recycling system and method that provides a plastic recycling system and method adapted for thermal decomposition process, such as pyrolysis, for plastic material and it can be precisely controlled throughout the process.
  • US10717934B2 relates to a mixed plastic waste recycling apparatus for conversion of mixed plastic waste into a liquid hydrocarbon product, wherein the recycling apparatus comprises a fluidized bed pyrolysis reactor configured to contain a fluidized bed of particulate material, a condenser to form a liquid fraction and a gas fraction, a monitor for measuring heat of combustion, a controller for maintaining the temperature of fluidized bed pyrolysis reactor so as to maintain the liquid fraction within a certain range.
  • the mixed plastic waste recycling apparatus is configured to treat from 5,000 to 20,000 tonnes per year of mixed plastic waste.
  • US 10975313 B2 relates to the production of aromatic hydrocarbons from mixed plastics via processes which include pyrolysis, hydroprocessing, reforming, and disproportionation and alkylation, wherein benzene and xylenes are the preferred products.
  • It relates to a process for producing benzene and xylenes comprising (a) converting a plastic waste to a hydrocarbon liquid stream and a pyrolysis gas stream in a pyrolysis unit, contacting the hydrocarbon liquid stream with a hydroprocessing catalyst in the presence of hydrogen to yield a hydrocarbon product and a first gas stream, wherein the hydrocarbon product comprises C5+ hydrocarbons, feeding the saturated hydrocarbons stream to a reforming unit to produce a reforming unit product, a second gas stream, and a hydrogen stream, wherein the reforming unit comprises a reforming catalyst, introducing the reforming unit product to a second aromatics separating unit to produce a non-aromatics recycle stream and a second aromatics stream, comprising C6+ aromatic hydrocarbons, recycling a portion of the non- aromatics recycle stream to the reforming unit, introducing the first and/or the second aromatics stream to a third aromatics separating unit to produce a first C6 aromatics stream comprising benzene, a C
  • the primary object of the present invention is to provide a plastic recycling system and method, which can provide a safe and reliable environment for thermal decomposition and pyrolysis of plastic.
  • Another object of the present invention is to provide a plastic recycling system and method, which can generate value added chemicals through thermal decomposition and pyrolysis of waste plastics.
  • Yet another object of the present invention is to provide a plastic recycling system and method, in which waste plastic material of any type such as Polyethylene (PE), Polypropylene (PP), Polyethylene Terephthalate (PET), Low Density Polyethylene (LDPE), and High Density Polyethylene (HDPE), can be used as the feed, for the generation of value added chemicals.
  • waste plastic material of any type such as Polyethylene (PE), Polypropylene (PP), Polyethylene Terephthalate (PET), Low Density Polyethylene (LDPE), and High Density Polyethylene (HDPE)
  • Still another object of the present invention is to provide a plastic recycling system and method, in which plastic material used as feed can be of any type, i.e., rigid or flexible plastic, for the generation of value added chemicals.
  • Another object of the present invention is to convert plastic wastes into hydrocarbons that can be used for specific applications. Further, yet another object of the present invention is to convert plastic wastes into hydrocarbons that can be further treated and converted into chemicals, depending on market requirements.
  • Figure 1 illustrates the schematic representation of system for pre-processing of plastic material and subsequent conversion of the pre-processed plastic material to hydrocarbons and chemicals.
  • Figure 2 illustrates a chromatogram from the gas chromatographic analysis of sample obtained from receptacle AB.
  • Figure 4 illustrates a chromatogram from the gas chromatographic analysis of sample obtained from receptacle AX.
  • the present invention is related to a single-step reaction process for the conversion of plastic material into value-added fuel oils and chemicals through de -polymerization.
  • Said plastic materials may include, but are not limited to, polyethylene (PE), polypropylene (PP), low-density polyethylene (LDPE), high-density polyethylene (HDPE), polyethylene terephthalate (PET), polyvinyl, or mixtures thereof.
  • the raw materials for conversion into chemicals may also include light petroleum distillates (LDP), heavy petroleum distillates (HDP), and the like, or a mixture thereof.
  • Aromatics are important chemicals, with applications ranging from chemical intermediates to solvents.
  • Benzene occurs in crude oil and is used for manufacturing chemicals such as ethylbenzene, cumene, cyclohexane, nitrobenzene, and alkylbenzenes.
  • Benzene has a high octane number, and is an important component of gasoline.
  • Benzene can also be used in the manufacture of rubbers, lubricants, dyes, detergents, drugs, explosives, and pesticides.
  • xylenes occur in small concentrations in crude oil, xylenes are produced mainly as part of the BTX aromatics (benzene, toluene, and xylenes).
  • Xylenes are primarily used as solvents in various applications, such as in printing, rubber, and leather industries, and are common components of ink, rubber, adhesives, thinning paints, varnishes, and cleaning agents (e.g., for steel, silicon wafers, integrated circuits).
  • Xylene is also used as a building block for producing Terephthalic acid (TPA) from which Polyethylene Terephthalate (PET) which is one of the most widely used plastic types in the world, is manufactured.
  • TPA Terephthalic acid
  • PET Polyethylene Terephthalate
  • Plastic waste is posing a big threat to humans and animals and therefore, research on the conversion of plastics into fuels and value-added products is also in progress.
  • the present invention is related to a system and a method for the direct conversion of crude plastic wastes into high value chemicals.
  • the pre-processing of plastic material comprises loading different types of plastic materials procured from various sources, into a plastic shredding machine, wherein the plastic material is ground into powder form or chips, and manually fed into a reactor kiln. Melting and gasification of said ground plastic material is performed in the same reactor kiln (C) wherein the de -polymerization takes place,
  • the present invention relates to a single-step reaction process for the conversion of raw, unsorted, contaminated plastic waste materials to generate fuel oils and chemicals.
  • the type of contaminants could be of inorganic, organic or biological origin and concentration of these contaminants may vary which will have an effect on the recovery percentage or yield of chemicals.
  • the invention also relates to a system for plastic waste conversion comprising a series of kilns, hot condensers, cool condensers, gas distributors and receptacles.
  • the process for plastic waste conversion comprises a de -polymerization process, wherein said plastic waste material is loaded in a de -polymerization reactor also called Kiln (C) equipped with a special heating system wherein de -polymerization takes place at a temperature of 90°C to 550°C under atmospheric pressure for 18 to 28 hours, said depolymerization process further comprising a humidity removal process, wherein said reactor kiln (C) is heated to remove the moisture present in said plastic material at a temperature of 90°C to 140°C.
  • a self-purging process for the removal of oxygen from said reactor kiln (C) wherein said purging activity is performed at 140°C to 220°C, using a temperature controller and thermal management algorithm operated and controlled through the Control Panel (A).
  • the materials then undergo a plastic material melting process, wherein said plastic material is melted at a temperature of 220°C to 290°C in said kiln (C), a gasification and cracking process, wherein said plastic melt solution is heated in said kiln (C) to effect gasification at a temperature of 290°C to 320°C, which is subsequently raised to 350°C and maintained at this temperature for a duration of 3 hours. Due to this heat transformation, the plastic material slowly melts and changes its state into a liquid. The temperature is then slowly increased from 350°C to 400°C in a phased manner and is maintained for 8 hours.
  • the lighter fraction containing hydrocarbons below C20 flows through said intermediate cracker (D) into the collection receptacles from where it travels to the condensation and distillation module for condensation and subsequent distillation into various liquid condensates.
  • Heavier fraction which turns into liquids in said intermediate cracker (D) is subjected to further heating in said intermediate cracker (D) where it undergoes further cracking into lighter hydrocarbon fractions below C20.
  • the lighter gases rise and flow into the condensation and distillation module.
  • Hydrocarbon fractions in the range of C14-C20 travel through the connecting pipe from said intermediate cracker (D), condense and settle down as liquids in the receptacle (G). From said receptacle (G), the fraction lighter than C14 flows to the hot condenser (E) where the gases are allowed to expand and cool down to realize two hydrocarbon fractions ranging between C7 - CIO and CIO - C 14 which condense and settle into the receptacles (H) and (I) respectively.
  • the hydrocarbon fraction lighter than C7 flows into the cool condenser (F) where it is subjected to external cooling using a compressor (K), thereby realizing a liquid condensate fraction of hydrocarbons fraction in the range of C5 - C « which is collected into receptacle (J).
  • the uncondensed hydrocarbon fraction with gases lighter than C5 moves further into the gas distributor (M) in which uncondensed gases lighter than C5 from within the systems is further passed through a gas bubbler (L) to a dual fuel diesel generator for co-combustion in its Internal combustion (IC) engine to generate electric power.
  • This power is used in the premises for various purposes as ancillary power or is fed back into the system as a secondary power source.
  • the C14-C20 hydrocarbon condensate collected in said receptacle (G) is further passed into another kiln (P) in which the hydrocarbons are further cracked by subjecting the condensate to desired temperature settings.
  • P kiln
  • This is achieved by using an advanced thermal algorithm, wherein the liquid condensate is transformed into gaseous state.
  • the gases rise through said kiln (P) to condense and settle as the heavier hydrocarbon fraction of C20 in the receptacle (Q), while the lighter fractions proceed into the hot condenser (U) for further expansion and condensation into two hydrocarbon fractions, Cis and Ci6, into the receptacles (R) and (S) respectively.
  • the hydrocarbon fraction lighter than Ci6 moves further into cool condenser (V) and is externally cooled by a compressor (W) where said lighter hydrocarbon fraction expands, loses heat, and condenses as a liquid condensate consisting of C14 hydrocarbons in receptacle (T).
  • Said C14 hydrocarbon condensate fraction realized from further cracking of heavier liquid condensates derived from plastic waste can directly be used as chemicals or fuels as desired. Alternately, they can be subjected to further synthesis downstream to produce value-added chemicals.
  • the uncondensed hydrocarbon fractions that are lighter than C14 pass through the gas bubbler (X) into the gas separator (Y) from where it moves to another kiln (Z).
  • Said kiln (Z) receives two inputs including an input of gases lighter than C14 from said kiln (P) as well as the liquid hydrocarbon condensate from a collection receptacle (H).
  • a thermal algorithm is applied in said receptacle (H) to heat up the received inputs, further cracking them into lighter fractions to produce lighter fractions of C14 which rise through said kiln (Z) and condense into the receptacle (AA), while C13 and C12 containing hydrocarbon fraction passes through the hot condenser (AE) where it condenses into the receptacles (AB) and (AC) respectively.
  • the lighter fractions pass through into the cool condenser (AF) where the gases are allowed to expand and cool through external cooling using the compressor (AG), allowing the gases to condense into a receptacle (AD).
  • This liquid condensate consists of a C 10 hydrocarbon fraction.
  • Said kiln (AJ) receives two hydrocarbon fractions containing a fraction less than C10 from said kiln (Z), and the liquid condensate comprising of hydrocarbon fractions in the range of C7 to C10 collected in the receptacle (I) wherein the mixture of hydrocarbons is heated in said kiln (AJ) thus subjecting the same to further cracking into lighter hydrocarbon fractions.
  • hydrocarbon fraction containing CIO hydrocarbons rises up through said kiln (AJ), expands and condenses into the receptacle (AK) while lighter gases pass beyond said receptacle (AK) into a hot condenser (AO) allowing further expansion and condensation, before being collected as liquid condensates of hydrocarbon fractions of C9 and Cs into receptacles (AL) and (AM) respectively.
  • Hydrocarbon fractions lighter than Cs flow into the (AP) where they are further expanded and cooled with a compressor (AQ) thereby condensing into a liquid condensate consisting of C7 hydrocarbons.
  • the hydrocarbon gases lighter than C7 pass onto the bubbler (AR) and through the gas separator (AS) into a kiln (AT).
  • Said kiln (AT) receives an input of gases lighter than C7 from the kiln (AJ) as well as the liquid condensate hydrocarbon fractions in the range of C5 to C8 from the receptacle (J).
  • This stream may contain benzene and small quantities of toluene and xylenes.
  • the hydrocarbons from receptacle (J) which consist primarily of hydrocarbons in the range of C5 to C8 also consists of commercially viable molecules such as ortho-xylene, meta-xylene and para-xylene. These , heated in the kiln (AT) to further crack the same into lighter hydrocarbon fractions ranging between C5 to C8, which will be collected in various receptacles and these commercially viable hydrocarbon molecules can be recovered using distillation.
  • the mixture of hydrocarbons heated in said kiln (AT) is subjected to temperatures designed for cracking and subsequent separation occurs at pressure not more than the ambient pressure, thereby realizing separation of commercially viable molecules such as benzene based compounds and xylenes.
  • the percentage of xylenes in the resultant liquids can be as high as ⁇ 27 %.
  • the uncondensed gases pass through the cool condenser (AZ) and into a bubbler (BB) and onto a gas separator (BC) and move to a gas distributor (M) from where it reaches the diesel generator (O) through a bubbler (N) to undergo co-combustion along with diesel in the IC engine of the diesel generator to produce electricity which is used as ancillary power within the process or outside in the accompanying facility.
  • All said kilns (C), (P), (Z), (AJ), and (AT), and the intermediate cracker (D) are cooled by said tower cooler (B) which is a heat cooling system.
  • This process is unique for its ability to process plastic waste, and generate desired hydrocarbon fractions which can be used as specialty chemicals, plastic intermediates or fuels or blend for fuels without using a catalyst or applying any pressure higher than the ambient pressure thereby making it cost-effective, while also being environmentally friendly.
  • the residual solid carbon upon the completion of the reaction can be added to the soil or converted into carbon bricks. Due to the low thermal co-efficient, the carbon bricks when used in the construction of enclosed spaces, help maintain the temperature contained in the enclosed space, thus contributing to energy savings.
  • the system for conversion of plastic waste to chemicals has also been designed for operation with solar energy. While the process operates directly with solar energy during day time when the sun is shining, the plant is run at night times with the help of batteries that store the power during day time. The system may also draw power from the grid during the night time, if required. Similar approach may be followed when the source of energy is wind.
  • the objects of the present invention are achieved through a system and method where conversion of plastics into chemical intermediates is achieved through de -polymerization.
  • Plastic wastes such as polyethylene (PE), polypropylene (PP), low-density polyethylene (LDPE), high-density polyethylene (HDPE), polyethylene terephthalate (PET), polyvinyl, or mixtures thereof are passed through a series of kilns, hot condensers, cool condensers, gas distributors and receptacles. Waste plastics are first freed of moisture and oxygen, and then melted, and the molten solution is slowly heated upto 400°C.
  • the initial fraction containing hydrocarbons below C20 is subjected to condensation and distillation.
  • the resulting hydrocarbon fraction of C14 to C20 is then cracked.
  • the hydrocarbon fraction lighter than C14 is further cracked and C7 to C10 hydrocarbon containing fraction is collected.
  • C7 to C10 hydrocarbon stream is further separated into C9 and C « containing hydrocarbon streams.
  • Lighter hydrocarbons of C5 to C7 are further collected.
  • the absolute concentration of xylene in the stream may be as high as 26%.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Materials Engineering (AREA)
  • Health & Medical Sciences (AREA)
  • Sustainable Development (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Thermal Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Environmental & Geological Engineering (AREA)
  • Combustion & Propulsion (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

La présente invention concerne un système et un procédé de conversion de matières plastiques en hydrocarbures dans un procédé en une seule étape. Les matières plastiques peuvent comprendre des matières plastiques industrielles ou des déchets plastiques municipaux. Le système comprend une série de fours, de condenseurs chauds, de condenseurs froids, de distributeurs de gaz et de réceptacles. Les déchets plastiques débarrassés de l'humidité et de l'oxygène sont chauffés lentement jusqu'à 400°C. Initialement, la fraction contenant des hydrocarbures en dessous de C20 est séparée. La fraction hydrocarbonée de C14 à C20 est ensuite craquée pour obtenir des fractions C7-C10 et C10-C14. La fraction hydrocarbonée plus légère que C14 est en outre craquée et la fraction hydrocarbonée C7 à C10 est collectée. Le flux d'hydrocarbures C10 est ensuite séparé en hydrocarbures C9 et C8. Des hydrocarbures plus légers de C5 à C7 sont en outre collectés. Ce système n'utilise pas de catalyseur et aucune pression induite n'est utilisée au-delà de la pression ambiante.
PCT/IN2024/051779 2023-09-19 2024-09-18 Valorisation de matières plastiques en carburants et produits chimiques à valeur ajoutée Pending WO2025062423A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
IN202341062901 2023-09-19
IN202341062901 2023-09-19

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WO2025062423A1 true WO2025062423A1 (fr) 2025-03-27

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Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2021171313A1 (fr) * 2020-02-26 2021-09-02 Satish Kumar B V Procédé de conversion de matière plastique en carburants

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2021171313A1 (fr) * 2020-02-26 2021-09-02 Satish Kumar B V Procédé de conversion de matière plastique en carburants

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