WO2010025525A1 - Procédé de fabrication de carburants de synthèse à partir de déchets et d'autres matières - Google Patents

Procédé de fabrication de carburants de synthèse à partir de déchets et d'autres matières Download PDF

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Publication number
WO2010025525A1
WO2010025525A1 PCT/AU2009/001170 AU2009001170W WO2010025525A1 WO 2010025525 A1 WO2010025525 A1 WO 2010025525A1 AU 2009001170 W AU2009001170 W AU 2009001170W WO 2010025525 A1 WO2010025525 A1 WO 2010025525A1
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Prior art keywords
feedstock
gas
stream
reaction vessel
oxygenates
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PCT/AU2009/001170
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English (en)
Inventor
Peter Vernon Lansell
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Sheima Pty Ltd.
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Publication date
Priority claimed from AU2008904621A external-priority patent/AU2008904621A0/en
Application filed by Sheima Pty Ltd. filed Critical Sheima Pty Ltd.
Publication of WO2010025525A1 publication Critical patent/WO2010025525A1/fr

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    • 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
    • C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
    • C10G1/065—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation in the presence of a solvent
    • 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
    • C08J11/14—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 treatment with steam or water
    • 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
    • C08J11/16—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 treatment with inorganic material
    • 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
    • C08J11/18—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 treatment with organic material
    • C08J11/20—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 treatment with organic material by treatment with hydrocarbons or halogenated hydrocarbons
    • 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
    • C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
    • 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
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1003—Waste materials
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1011—Biomass
    • C10G2300/1014—Biomass of vegetal origin
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4006—Temperature
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4012—Pressure
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4081—Recycling aspects
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/04—Diesel oil
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/54—Improvements relating to the production of bulk chemicals using solvents, e.g. supercritical solvents or ionic liquids
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00—Technologies for solid waste management
    • Y02W30/50—Reuse, recycling or recovery technologies
    • Y02W30/62—Plastics recycling; Rubber recycling

Definitions

  • the present invention relates to a process of producing synthetic hydrocarbon and oxygenated fuels of substantially the same functionality and purity as commercial diesel or petrol or other petroleum fractions from a variety of feedstock materials including solids, liquids, gases and combinations thereof.
  • Biodiesel as an alternative diesel fuel from edible/non-edible oils and animal fats have shown promise as alternative diesel fuels.
  • transesterification is the preferred route for biodiesel synthesis.
  • the current techniques for transesterification of the oils to biodiesel are based on acid/alkali catalysis. However, these methods are not cost effective for oils with high free fatty acid content and also require an additional downstream step for separation of glycerine and soap from the product.
  • Much of the process complexity originates from contaminants in the feedstock, such as water and free fatty acids, or impurities in the final product, such as methanol, free glycerol, and soap.
  • transesterified biodiesel comprises a mix of mono-alkyl esters of long chain fatty acids.
  • the most common form uses methanol (commonly converted to sodium methoxide) to produce methyl esters as it is the cheapest alcohol available, though ethanol can be used to produce an ethyl ester biodiesel and higher alcohols such as isopropanol and butanol have also been used.
  • ethanol can be used to produce an ethyl ester biodiesel and higher alcohols such as isopropanol and butanol have also been used.
  • Using alcohols of higher molecular weights reduces the cold flow properties of the resulting ester, at the cost of a less efficient transesterification reaction.
  • a by-product of the transesterification process is the production of glycerol. For every 1 tonne of biodiesel that is manufactured, from 100 kg to 300kg of glycerol are produced. Usually this crude glycerol has to be purified, typically by performing vacuum distillation. This is rather energy intensive. The refined glycerol (98%+ purity) can then be utilised directly, or converted into other products.
  • transesterification of vegetable oils or animal fats can be done in an unsophisticated process, the process conditions must be carefully controlled and or modified to achieve maximum yield at the lowest temperature and reaction time.
  • the process of transesterification is affected by the mode of reaction condition, molar ratio of alcohol to oil, type of alcohol, type and amount of catalysts, reaction time and temperature and purity of reactants.
  • feedstock low in fatty acid content to help minimise effect of saponification.
  • Food crops such as corn and soy are known to have a relatively low fatty acid content and have been grown and harvested as a biodiesel feedstock material.
  • waste material such as plastics, biomass, household rubbish, cellulose, municipal solid waste (MSW), agricultural residues, farm waste and other biodegradable waste.
  • MSW municipal solid waste
  • Fisher-Tropsch has been the method conventionally used to utilise waste material to produce alternative fuels to reduce the use of fossil fuels, reduce greenhouse gas emissions and reduce pollution and waste management problems.
  • feedstock has to be scrupulously cleaned of sulphur, chlorine and various other poisons to avoid catalyst degradation. Once the catalyst is depleted, consumed or poisoned, it may not be able to be regenerated, and the catalyst itself then represents a toxic waste problem.
  • a further drawback is that the feedstock requires gasification.
  • a method for producing hydrocarbons or oxygenates for use as a synthetic fuel source from suitable material including: providing a feedstock stream comprising solid and/or liquid and/or gaseous material under pressure to a mixing vessel at a predetermined feed rate; injecting a stream of a reactant gas capable of dissolving in the feedstock into the feedstock stream for mixing; transferring a stream of feedstock and gas reactant mixture to a reaction vessel downstream therefrom; subjecting the feedstock and gas mixture in the reaction vessel to at or near supercritical conditions; wherein the solubilised material is broken down in the reaction vessel into a distribution of molecular weight fractions, and wherein the reactant gas selectively adds or subtracts from the molecular weight fractions to provide a hydrocarbon or oxygenateof predetermined chain length suitable as an alternative fuel.
  • the present invention represents a significant advance over the prior art since the instant process does not require conversion of solids, liquids or gaseous material as in the Fisher-Tropsch process.
  • the present invention is also not limited by requiring quality feedstock material. Indeed the process of the invention can be used to produce a synthetic fuel from any suitable material including coal, waste material including domestic waste, commercial municipal waste, agricultural waste, chemical waste, plastics and biomass such as cellulose.
  • the reactant gas can be selected from a range of gases including hydrocarbons, carbon dioxide, carbon monoxide, nitrogen or steam.
  • the reactant gas stream comprises methane.
  • the source of methane can be derived from decomposition of the waste material, flare gas or town gas.
  • the reaction occurring in the reaction vessel can be exothermic, and in which case the heat of reaction can be collected by a heat exchanger downstream from the reaction vessel and the heat redirected to the reaction vessel to help maintain reaction conditions.
  • the reaction occurring in the reaction vessel can be endothermic, and in which case the heat for the reaction can be supplied by a heat exchanger upstream from the reaction vessel.
  • a method of producing hydrocarbons for use as a synthetic fuel source including: providing a feedstock stream comprising solid, liquid or gaseous material; mixing a stream of a reactant gas with the feedstock stream; transferring the feedstock and gas mixture to a reaction vessel; subjecting the feedstock and gas mixture in the reaction vessel to sub- or supercritical temperature and pressure, wherein the gas is at least partially dissolved in the feedstock material; wherein the feedstock material is selectively changed into a predetermined quantifiable fraction and wherein the solubilised hydrocarbon gas selectively substitutes on the fraction to provide a hydrocarbon or oxygenate liquid fuel of predetermined chain length suitable as an alternative fuel.
  • the feedstock stream is pumped under pressure of about 6 bar by a pumping means prior to entering a mixing station upstream from the pumping means.
  • the mixing station can include a feed tank with a stirring means or static mixer.
  • the gas can be introduced into the feedstock stream at the mixing station by means of gas injection.
  • the mixing station includes a static mixer.
  • the process includes a gas separating means.
  • the process can be continuous.
  • the feedstock and gas mixture is subjected to compression at sub- or supercritical pressures and temperatures.
  • the feedstock and gas mixture is preferably preheated following compression before being transferred to the reaction vessel.
  • the process includes a heat exchanger which is adapted to transfer heat from the reaction vessel and redirected upstream of the reaction vessel so as to preheat the reactants before input to the reaction vessel.
  • heat generated by reaction of the feedstock and gas mixture can be recovered and redirected to use for preheating combined gas and feedstock mixture before entering the reaction vessel. This represents a clear energy savings.
  • the process can also include providing a catalyst.
  • the catalyst can be present in varying quantities and are selected from either of two categories being:
  • the reactant can be water.
  • water as with other supercritical fluids can readily solubilise the waste material and exposes relatively high molecular weight hydrocarbons in the waste material to cleavage to form a majority of low molecular weight short chain hydrocarbons.
  • waste material feedstock to a gas at elevated pressure and temperature causes the waste feedstock to solubilise and break down into lower chain molecules and in some instances their constituent atoms.
  • the lower chain molecules then combine with methane or its alkyl derivative to form hydrocarbon liquids suitable for use as alternative fuels.
  • a process for producing synthetic fuel from a feedstock material selected from fats, oils, greases, cellulose, organic waste, plastics and the like including: cleaning and preheating the feedstock material; providing a source of a short chain hydrocarbon including an alcohol; providing a source of methane gas at a pressure and temperature effective to dissolve the feedstock and the hydrocarbon; combining the preheated feedstock material into a mixing chamber with a stream of methane from the source of methane at a predetermined rate to dissolve the feedstock material; and reacting the feedstock material with the gas or alcohol wherein the gas or the alcohol is provided at a predetermined rate into the mixing chamber.
  • the above process represents a departure from prior art processes.
  • the process of the invention allows production of synthetic diesel fuel from a range of waste material including solids, liquids, gases and combinations thereof.
  • the methane gas is provided at supercritical temperature and pressure.
  • the use of methane in the process at supercritical conditions surprisingly becomes an excellent solvent and dissolves into the feedstock so that the reactants are in close proximity of each other and therefore react readily. This represents an advance over conventional, base-catalysed transesterification which does not work efficiently on the high free fatty acid (FFA) content typical of cheaper, lower-quality feedstocks.
  • FFA free fatty acid
  • methane has low solubility in the products at ambient temperature separation can easily be achieved by reduction of pressure.
  • Figure 1 shows a schematic flow diagram of a process for producing hydrocarbon as a synthetic fuel source in accordance with the present invention
  • Figure 2 shows a flow diagram of an industrial process for producing a hydrocarbon as a synthetic fuel in accordance with the present invention.
  • FIG. 1 and 2 there is shown a schematic representation of a process for producing a synthetic fuel from a suitable material wherein the material can be selected from commercial, domestic and other waste materials typically solids waste including domestic waste such as paper, plastic, cellulosic matter, food wastes otherwise sent to landfill.
  • the material can be selected from commercial, domestic and other waste materials typically solids waste including domestic waste such as paper, plastic, cellulosic matter, food wastes otherwise sent to landfill.
  • FIG. 1 shows a feedstock stream 3 indicating directional flow of a feedstock such as cellulose from a waste feed station towards a mixing chamber 1.
  • the mixing station is fitted with a stirring mechanism 40 such as a static mixer 2.
  • the feedstock stream 3 is supplied to the mixing chamber at a first predetermined temperature and feed rate and subjected to stirring.
  • a reactant gas stream 4 which is shown as methane in this example, is injected into the mixer and mixed with the waste material.
  • the reactant gas stream is delivered to the mixing chamber at a predetermined pressure and rate to suit the feedstock characteristic and feed rate.
  • the process further includes a high pressure pump 5 located downstream from the mixing chamber, which receives the combined feedstock and reactant gas from the mixing chamber.
  • the pump 5 increases the pressure of the combined feedstock and gas reactant mixture to a desired level at sub- or supercritical temperatures and pressure of the reactant gas. Referring to Table 1, the supercritical conditions for a range of reactant gases is shown.
  • a pressure control valve 6 is located proximal to the pump 5 and regulates the back-pressure.
  • the feedstock and gas reactant having been subjected to high pressure, are transferred to a supercritical reaction vessel 20 downstream from the pump 5.
  • the feedstock and gas reactant are subjected to the sub- or supercritical temperatures of the gas reactant (46 bar and 190.6 K).
  • the schematic representation shows an exothermic process.
  • the process can be endothermic or exothermic depending on the oxidation/reduction capabilities of the feedstock and reactant gas.
  • the reactant gas can be steam.
  • heat of reaction 21 in the case of an exothermic reaction is recovered and used to preheat the reactant stream before entering the reaction vessel.
  • a final product stream 22 exits the reactor.
  • the final product stream is passed through a separating means such as a chromatograph 23, which provides a qualitative analysis of end product.
  • the feedstock material is primarily a cellulose material, which apart from being a cheap and abundant source of waste feedstock, provides a source of oxygen.
  • the reactant gas is methane but can be a hydrocarbon such as methane, ethane, propane or the like. The process is shown using methane gas as this can be readily and cost effectively obtained from the waste feedstock or derived from flare gas or even domestic gas supply.
  • methane has relatively low solubility in the products at ambient temperature separation can easily be achieved by reduction of pressure.
  • the process produces levulinic acid and or methyl or ethyl levulinate having a cetane rating of about 52, which provides a direct replacement for high quality diesel.
  • the formation of levulinic acid and its derivitives provides a useful precursor for PET plastics as well as many other feedstock chemicals.
  • a combined reaction vessel and heat exchanger 20 At least part of the heat provided for reaction is provided by a furnace chamber 8, which uses heating oil or molten salt to transfer heat to the reaction vessel.
  • reaction process is exothermic, and the heat produced can be received and redirected back to the input stream 9 prior to entry to the reaction vessel by the heat exchanger.
  • a clear advantage is achieved in minimising heating costs by using the heat of reaction.
  • the process as shown in figure 2 further includes a fire-safe valve 10, which acts as a safety means to allow escape of material to a water-filled dump tank 15 in the event of a reactor leakage. Additional safety is provided by a pressurised water tank 16, which deluges the process space in the event of a fire. Downstream from the reactor there is provided a gas separator 11 , which serves to remove water vapour and any residual gas from the end product 22.
  • a fire-safe valve 10 acts as a safety means to allow escape of material to a water-filled dump tank 15 in the event of a reactor leakage. Additional safety is provided by a pressurised water tank 16, which deluges the process space in the event of a fire.
  • a gas separator 11 Downstream from the reactor there is provided a gas separator 11 , which serves to remove water vapour and any residual gas from the end product 22.

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

Abstract

L'invention porte sur un procédé de fabrication d'hydrocarbures ou de composés oxygénés destinés à être utilisés en tant que source de carburant de synthèse à partir de matières appropriées, le procédé consistant : à utiliser un courant de charge d'alimentation comportant une matière solide et/ou liquide et/ou gazeuse sous pression dans une cuve de mélange à un débit d'alimentation prédéfini ; à injecter un courant d'un réactif gazeux pouvant se dissoudre dans la charge d'alimentation en un courant de charge d'alimentation pour mélange ; à transférer un courant de mélange de charge d'alimentation et de réactif gazeux vers une cuve de réaction en aval de celle-ci ; à soumettre le mélange de charge d'alimentation et de gaz dans la cuve de réaction à des conditions supercritiques ou proches de celles-ci ; la matière solubilisée étant décomposée dans la cuve de réaction en une distribution de fractions de masse moléculaire, le réactif gazeux s'ajoutant ou se soustrayant sélectivement des fractions de masse moléculaire pour fournir un hydrocarbure ou un composé oxygéné, de longueur de chaîne prédéterminée, approprié en tant que carburant de remplacement.
PCT/AU2009/001170 2008-09-05 2009-09-07 Procédé de fabrication de carburants de synthèse à partir de déchets et d'autres matières WO2010025525A1 (fr)

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AU2008904621 2008-09-05
AU2008904621A AU2008904621A0 (en) 2008-09-05 A Method of Producing Hydrocarbon as an Alternative Fuel from Waste Material

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WO2010025525A1 true WO2010025525A1 (fr) 2010-03-11

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3080232A4 (fr) * 2013-12-11 2017-08-09 Biogts OY Procédé et système de production de biocarburant liquide provenant d'huiles et/ou de graisses à base biologique
CN108251146A (zh) * 2018-02-11 2018-07-06 宁波普前环保科技有限公司 一种废塑料和纤维素共处理的方法
EP2612900B1 (fr) * 2012-01-05 2020-05-06 Korea Institute of Science and Technology Procédé de production de combustible renouvelable utilisant un fluide supercritique

Citations (3)

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Publication number Priority date Publication date Assignee Title
US4396786A (en) * 1980-10-27 1983-08-02 Johnson Matthey Public Limited Company Method for producing fuel oil from cellulosic materials
US6504068B1 (en) * 1996-06-06 2003-01-07 Mitsubishi Jukogyo Kabushiki Kaisha Method for converting a plastic waste into oil in a stainless steel reactor
US20030221361A1 (en) * 2000-03-23 2003-12-04 Russell Richard W Method of converting agricultural waste to liquid fuel cell and associated apparatus

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4396786A (en) * 1980-10-27 1983-08-02 Johnson Matthey Public Limited Company Method for producing fuel oil from cellulosic materials
US6504068B1 (en) * 1996-06-06 2003-01-07 Mitsubishi Jukogyo Kabushiki Kaisha Method for converting a plastic waste into oil in a stainless steel reactor
US20030221361A1 (en) * 2000-03-23 2003-12-04 Russell Richard W Method of converting agricultural waste to liquid fuel cell and associated apparatus

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2612900B1 (fr) * 2012-01-05 2020-05-06 Korea Institute of Science and Technology Procédé de production de combustible renouvelable utilisant un fluide supercritique
EP3080232A4 (fr) * 2013-12-11 2017-08-09 Biogts OY Procédé et système de production de biocarburant liquide provenant d'huiles et/ou de graisses à base biologique
CN108251146A (zh) * 2018-02-11 2018-07-06 宁波普前环保科技有限公司 一种废塑料和纤维素共处理的方法
CN108251146B (zh) * 2018-02-11 2019-09-17 北京石油化工学院 一种废塑料和纤维素共处理的方法

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