WO2009002191A2 - Process and plant for production of biofuels - Google Patents

Process and plant for production of biofuels Download PDF

Info

Publication number
WO2009002191A2
WO2009002191A2 PCT/NO2008/000245 NO2008000245W WO2009002191A2 WO 2009002191 A2 WO2009002191 A2 WO 2009002191A2 NO 2008000245 W NO2008000245 W NO 2008000245W WO 2009002191 A2 WO2009002191 A2 WO 2009002191A2
Authority
WO
WIPO (PCT)
Prior art keywords
biosyngas
waste
air
biomass
raw
Prior art date
Application number
PCT/NO2008/000245
Other languages
French (fr)
Other versions
WO2009002191A3 (en
Inventor
Erik Tønseth
Original Assignee
Toenseth Erik
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Toenseth Erik filed Critical Toenseth Erik
Priority to US12/452,282 priority Critical patent/US20100216898A1/en
Priority to EP08779092.9A priority patent/EP2167613B1/en
Priority to DK08779092.9T priority patent/DK2167613T3/en
Publication of WO2009002191A2 publication Critical patent/WO2009002191A2/en
Publication of WO2009002191A3 publication Critical patent/WO2009002191A3/en

Links

Classifications

    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10BDESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/02Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10BDESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B49/00Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/02Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
    • C10B49/04Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING 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
    • C10G2/00Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02Fixed-bed gasification of lump fuel
    • C10J3/06Continuous processes
    • C10J3/08Continuous processes with ash-removal in liquid state
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02Fixed-bed gasification of lump fuel
    • C10J3/20Apparatus; Plants
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60Processes
    • C10J3/64Processes with decomposition of the distillation products
    • C10J3/66Processes with decomposition of the distillation products by introducing them into the gasification zone
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10KPURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00Purifying combustible gases containing carbon monoxide
    • C10K1/002Removal of contaminants
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10KPURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00Purifying combustible gases containing carbon monoxide
    • C10K1/002Removal of contaminants
    • C10K1/003Removal of contaminants of acid contaminants, e.g. acid gas removal
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10KPURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00Purifying combustible gases containing carbon monoxide
    • C10K1/002Removal of contaminants
    • C10K1/003Removal of contaminants of acid contaminants, e.g. acid gas removal
    • C10K1/004Sulfur containing contaminants, e.g. hydrogen sulfide
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10KPURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00Purifying combustible gases containing carbon monoxide
    • C10K1/02Dust removal
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10KPURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00Purifying combustible gases containing carbon monoxide
    • C10K1/02Dust removal
    • C10K1/024Dust removal by filtration
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10KPURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00Purifying combustible gases containing carbon monoxide
    • C10K1/02Dust removal
    • C10K1/028Dust removal by electrostatic precipitation
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10KPURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00Purifying combustible gases containing carbon monoxide
    • C10K1/08Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • C10K1/10Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
    • C10K1/101Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids with water only
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10KPURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00Purifying combustible gases containing carbon monoxide
    • C10K1/08Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • C10K1/10Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
    • C10K1/12Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors
    • C10K1/14Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors organic
    • C10K1/143Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors organic containing amino groups
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10KPURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00Purifying combustible gases containing carbon monoxide
    • C10K1/32Purifying combustible gases containing carbon monoxide with selectively adsorptive solids, e.g. active carbon
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10KPURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/02Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
    • C10K3/04Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment reducing the carbon monoxide content, e.g. water-gas shift [WGS]
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2200/00Details of gasification apparatus
    • C10J2200/15Details of feeding means
    • C10J2200/156Sluices, e.g. mechanical sluices for preventing escape of gas through the feed inlet
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/09Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913Carbonaceous raw material
    • C10J2300/0916Biomass
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/09Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913Carbonaceous raw material
    • C10J2300/0946Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/09Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953Gasifying agents
    • C10J2300/0956Air or oxygen enriched air
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/12Heating the gasifier
    • C10J2300/123Heating the gasifier by electromagnetic waves, e.g. microwaves
    • C10J2300/1238Heating the gasifier by electromagnetic waves, e.g. microwaves by plasma
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/16Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1625Integration of gasification processes with another plant or parts within the plant with solids treatment
    • C10J2300/1628Ash post-treatment
    • C10J2300/1634Ash vitrification
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/16Integration of gasification processes with another plant or parts within the plant
    • C10J2300/164Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1656Conversion of synthesis gas to chemicals
    • C10J2300/1659Conversion of synthesis gas to chemicals to liquid hydrocarbons
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/16Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1671Integration of gasification processes with another plant or parts within the plant with the production of electricity
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/16Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1671Integration of gasification processes with another plant or parts within the plant with the production of electricity
    • C10J2300/1675Integration of gasification processes with another plant or parts within the plant with the production of electricity making use of a steam turbine
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/18Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1846Partial oxidation, i.e. injection of air or oxygen only
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23GCREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00Pretreatment
    • F23G2201/40Gasification
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23GCREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2204/00Supplementary heating arrangements
    • F23G2204/20Supplementary heating arrangements using electric energy
    • F23G2204/201Plasma
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23GCREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2207/00Control
    • F23G2207/30Oxidant supply
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23GCREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2209/00Specific waste
    • F23G2209/26Biowaste
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23GCREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2900/00Special features of, or arrangements for incinerators
    • F23G2900/50208Biologic treatment before burning, e.g. biogas generation
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02EREDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00Technologies for the production of fuel of non-fossil origin
    • Y02E50/10Biofuels, e.g. bio-diesel
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02EREDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00Technologies for the production of fuel of non-fossil origin
    • Y02E50/30Fuel from waste, e.g. synthetic alcohol or diesel
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00Technologies relating to chemical industry
    • Y02P20/10Process efficiency
    • Y02P20/129Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00Technologies relating to chemical industry
    • Y02P20/141Feedstock
    • Y02P20/145Feedstock the feedstock being materials of biological origin

Definitions

  • the invention concerns a method and a plant for producing hydrocarbon based fuels from waste and biomass including wood and/or other cellulose containing biomass.
  • IPCC 4AR climate change
  • the transport sector which presently is almost fully run on derivatives of fossil oil.
  • the present transport sector utilises vehicles dependent on a chemical energy carrier able to be carried in the vehicles and delivering the energy to the engines of the vehicles, thus the problem of reducing greenhouse gas emissions from the transport sector becomes a question of finding another chemical energy carrier with sufficiently high energy density and which do not add net carbon to the earth carbon cycle.
  • Fuels made from waste and/or biomasses are very suited as replacement for fossil fuels such as gasoline and diesel. These fuels, e.g. bioethanol and biodiesel respectively, have a sufficient energy density suitable for present day transportation vehicles, they have similar chemical and physical properties such that they may be distributed and handled by present fuel distribution systems, and present day vehicles may be run on fossil fuels admixed with certain amounts of biofuels. Also, the technology for making engines run on pure biofuels is well developed, such that biofuels have capacity of eliminating greenhouse gas emissions from vehicles. Biofuels are presently made from agricultural leftovers and especially designated crops, so-called energy crops. However, the need for reserving arable land for food production and the large fuel volumes required by the transport sector calls for use of wood and other cellulose containing biomass as raw material in the future.
  • Conventional biomass gasifiers such as the widely used circulating fluidised bed (CFB) gasifiers which operates with air as gasification medium at near atmospheric pressure and about 850 °C, produces a raw biosyngas with typical compositions of 15-20 parts by volume of CO, H 2 , and CO 2 , 10-15 parts by volume H 2 O, about 40 parts by volume N 2 , about 5 parts by volume CH 4 , and smaller amounts of C 2 H 2 , C 2 H 4 , C 2 H 6 , benzene, toluene, xylenes and tars.
  • CFB circulating fluidised bed
  • inorganic impurities such as NH 3 , HCl, H 2 S, COS, CS 2 , HCN, HBr, dust, soot, and ash.
  • the syngas components H 2 and CO of the raw biosyngas will typically contain somewhat less than half of the chemical energy, while the rest are mainly contained by the CH 4 and the other hydrocarbons.
  • the Fischer-Tropsch synthesis is a catalytically conversion of CO and H 2 to hydrocarbons: 1 CO + 2 H 2 o -(CH 2 )- + H 2 O
  • the ratio in the feed gas is lower, it may be adjusted in a water-gas shift reaction:
  • WO 2007/000607 discloses a method for removing solid remnants termed "char" in the document from an off-gas produced by gasifying waste in a reactor at under- stochiometric conditions.
  • the char may include tarry compounds.
  • subjecting the off-gas including char to a plasma treatment unit in presence of oxygen and optionally steam, may overcome or at least mitigate the problem with char in the off-gas.
  • the main objective of this invention is to provide a method for production of biofuels by combined biomass gasification and Fischer-Tropsch synthesis which eliminate the problem with tar poisoning the catalysts in the Fischer-Tropsch synthesis.
  • Another objective is to provide a plant for performing the method according to the invention.
  • the invention is based on the realisation that a combination of a strong heating of a raw syngas exiting a gasif ⁇ er causing an atomisation of substantially all compounds of the raw syngas and thus destruction of all organic compounds in the raw syngas including tars, dioxins etc. and a subsequent rapid condensation of the atomised syngas in certain anaerobic conditions, will result in that practically all organic elements in the raw syngas will be converted to low-molecular anaerobic combustion products, primarily CO, CO 2 , H 2 O, and H 2 .
  • the invention is a method for producing biofuels and similar hydrocarbon products from waste and/or biomass, comprising:
  • the invention is a device for producing biofuels from waste and/or biomass, comprising:
  • a plasma reactor supplying a stream of inert gas heated to a temperature from 3000 to 5000 °C to the heating chamber where the heated inert gas is admixed with the mixture of raw biosyngas and air, - means for cooling the gas exiting the heat treatment chamber to a temperature in the range of 100 - 200 °C,
  • Eventual inorganic elements present in the raw syngas such as metals, sulphur, nitrogen etc. will form various oxides and hydrides, and should be substantially removed before entering the Fischer-Tropsch synthesis.
  • Other poisonous compounds may e.g. be compounds containing alkaline earth metals, and halogens.
  • the conditioning may also include removal of excess CO 2 by a conventional absorption process, by using water, amine or other known CO 2 -absorbents.
  • the conditioning may also include removal of some or all N 2 in the biosyngas.
  • biofuel as used herein includes any hydrocarbon based fuel and other hydrocarbon based products where the hydrocarbons are made by Fischer-Tropsch synthesis of gasified biomass and/or waste material.
  • the hydrocarbons may be more or less aliphatic single- or poly-branched hydrocarbon chains from 2 to more than 20 carbon atoms, and may also include a fraction of aromatic hydrocarbons. Hydrocarbons from 9 to 20 carbon atoms form the diesel fraction.
  • gasification means converting solid or liquid waste and/or biomass by evaporation and/or anaerobic decomposition to gas phase.
  • raw biosyngas as used herein means any gas exiting the gasification step of waste materials and/or biomass.
  • the term as used herein includes the case when the syngas is produced from gasification of only waste materials.
  • heat treated biosyngas as used herein means the gas mixture resulting from the atomisation and subsequent condensation of the raw biosyngas.
  • leaned biosyngas as used herein means the gas mixture resulting from removal of compounds poisonous for the catalysts in the Fischer-Tropsch synthesis from the heat treated biosyngas.
  • conditioned biosyngas means biosyngas where the H 2 :CO ratio has been adjusted by a water-shift reaction, and may also include removal of excess CO 2 .
  • anaerobic as used herein means a process in under- stochiometric amounts of oxygen, which is a reducing environment.
  • waste as used herein includes any carbon or hydrocarbon containing material waste or virgin material, including hazardous waste materials (not radioactive hazards).
  • the invention is not limited to any specific gasification process or gasification equipment, it may employ any known and conceivable method for forming a gaseous mixture comprising CO, CO 2 , H 2 O and H 2 from waste and/or biomass.
  • the gasification process will normally be a heating of the waste and/or biomass with regulated amounts of air as gasification medium to temperatures in the range of 500 to 1500 0 C, where the amount of air should be regulated to ensure under-stochiometric amounts of oxygen in the process such that the waste/biomass forms a gaseous mixture comprising CO, CO 2 , H 2 O and H 2 .
  • Both the biomass and waste contains inorganic compounds that results in liquid or solid remains in the lower part of the gasifier.
  • Biomass will generally contain less inorganic material than waste.
  • the gasifier should have means for taking out the inorganic residues accumulating in the lower lying section of the gasifier.
  • a proven and well known conventional technique for gasification of large volumes of biomass is the circulating fluid bed gasifier mentioned above operating with air as gasification medium at about atmospheric pressure and 850 °C, and which gives a raw biosyngas with typical compositions of 15-20 parts by volume of CO, H 2 , and CO 2 , 10-15 parts by volume H 2 O, about 40 parts by volume N 2 , about 5 parts by volume CH 4 , and smaller amounts of C 2 H 2 , C 2 H 4 , C 2 H 6 , benzene, toluene, xylenes and tars.
  • inorganic impurities such as NH 3 , HCl, H 2 S, COS, CS 2 , HCN, HBr, dust, soot, and ash.
  • a proven technology for gasification of solid waste materials is counter counter- current-flow shaft gasifiers known from the steel industry. These gasifiers are fed with solid waste material at the top, usually through a gas tight sluice at the top.
  • the waste is at the upper section heated to a temperature in the order of 300-500 0 C such that all volatile organic material and water is evaporated.
  • Pre-heated air is simultaneously injected in the bottom of the gasifier and the remaining carbon is gasified in the bottom at a temperature of about 1500°C.
  • the non-combustible materials like metals, ashes etc. are tapped of as a metal alloy and a non-leaching slag.
  • This type of shaft gasifier combines rugged design with low thermal losses and long lining life. It is fully sealed so that all material that leaves the gasifier is either treated at high temperature (melted) or sent to the plasma powered decomposition reactor for high temperature treatment.
  • the Fischer-Tropsch synthesis is well established conventional technology using iron-based catalysts or cobalt-based catalysts.
  • the FT-synthesis is well known to a person skilled in the art and need no further description.
  • the invention is not limited to the choice of Fischer-Tropsch reactor design and/or operation. Any known and conceivable Fischer-Tropsch reactor and synthesis process may be employed by the invention.
  • the catalysts of the Fischer-Tropsch synthesis are very sensitive towards poisoning by certain elements and solid particles in the feed gas.
  • the heat treated biosyngas according to the invention will contain small amounts of sulphur oxides/hydrides, nitrogen oxides/hydrides, halogen hydrides, and solid particles of alkaline metal oxides/hydrides that need to be lowered below the levels specified above.
  • sulphur oxides/hydrides nitrogen oxides/hydrides, halogen hydrides, and solid particles of alkaline metal oxides/hydrides that need to be lowered below the levels specified above.
  • cleaning technologies based on gas scrubbing and/or filtration available for removing all impurities in the heat treated biosyngas according to the invention.
  • the invention is not limited to a specific choice of cleaning method or device, any known and conceivable gas cleaning technology may be employed as long as the impurity levels reaches below the levels specified in the prior art section above. Such technologies are well known to a person skilled in the art and need no further
  • the invention is in principle not restricted to any specific choice of heat source for heat treating the raw biosyngas exiting the gasifier.
  • the heat-treatment should heat the entire stream of raw biosyngas exiting the gasifier to a temperature which ensures that practically all organic compounds including eventual halo- organic compounds in the gas stream are fully decomposed/atomised.
  • This requirement makes heating by use of electric arcs very suited, since these heat sources may readily provide very intense heat under conditions which makes it relatively easy to obtain an environment which is sufficiently reducing (oxygen depleted) to ensure that the organic constituents in the decomposed/atomised gas stream condenses to mainly low molecular combustion products such as CO, CO 2 , H 2 O and H 2 .
  • a heating the gas stream to a temperature of at least about 1250 °C, but preferably much higher, with a oxidation degree in the range of 0.2 ⁇ CO 2 /(CO+CO 2 ) ⁇ 0.4.
  • This degree of oxidation that is reducing environment will suppress formation of unwanted combustion products such as NO x and HCN to acceptable levels, and it will ensure that large organic and halo-organic compounds such as tars and dioxins, respectively cannot be formed.
  • the feature of heat treating the raw biosyngas to a temperature decomposing any tar and organic compound such as hydrocarbons in the raw biosyngas in a reducing environment ensuring conversion to low molecular combustion products eliminates the problem with tar poisoning the Fischer-Tropsch catalysts.
  • the conversion of tar and organic compounds in the raw biosyngas offer another advantage in that the energy content in those compounds are converted to syngas and thus made available for the Fischer-Tropsch synthesis.
  • the inventive method obtains a higher yield as measured by produced biofuels than prior art solutions.
  • a further advantage of the invention is that it will become possible to safely use any carbon or hydrocarbon containing materials including hazardous waste materials since all hazardous compounds are fully decomposed by the heat treatment and condensed to low molecular combustion products.
  • the inventive combination of a gasifier producing a raw syngas from biomass and/or waste materials, heating the raw syngas to at least about 1250 °C in an environment with a oxidation degree in the range of 0.2 ⁇ CO 2 /(CO+CO 2 ) ⁇ 0.4, removal of inorganic compounds from the heat treated syngas, eventual conditioning of the syngas before entering into a Fischer-Tropsch synthesis, provides a safe and cost-effective production method for biofuels from any hydrocarbon and carbon containing material such as municipal waste, industrial waste fractions, waste from food industry, waste from agriculture, fish processing industry, biomass from forestry etc. These material sources provide a cheap and abundant source allowing large scale production of biofuels and simultaneous reduction of waste problems.
  • the heat treated syngas exits the heat treatment with a temperature in the order of 1000-1500 °C and should be cooled to about 100-200 °C before cleaning.
  • This heat extraction may advantageously be utilised, for instance by a steam turbine to produce mechanical work or electricity.
  • the gasifier according to the example embodiment of the invention is a counter counter-current-flow shaft as shown in Figure 1.
  • This gasifier 1 comprises a waste/biomass inlet 10 with a two-port sluice system for introduction of waste/biomass 2 in the upper region 4 of the gasifier 1.
  • the temperature will typically be in the order of 200-500 °C such that all volatile organic material and water is evaporated.
  • the gasifier is sealed towards ambient atmosphere, and the introduction of fresh air is controlled to give an oxygen deficit in the gasifier.
  • the waste/biomass 2 descends down into the bulk zone 5 of the gasifier 1, it heats up in a reduced atmosphere and becomes gradually transformed to a low grade charcoal containing inorganic material.
  • these inorganic materials may be i.e. glass, metal and minerals, typically containing around 10 - 30 % of fix carbon.
  • Fix carbon means carbon that does not evaporate in the gasifier but remains down trough the carburisation zone. If the fix carbon in the waste becomes too low, biomass or other carbon source should be fed to the gasifier to provide the required temperature in the bottom of the gasifier.
  • the charcoal descending from the carbonization zone 5 into the partial oxidation and vitrification zone 6 is gasified by partly combustion with preheated air 3.
  • the partial combustion provides a temperature in the bottom of 1.450 — 1.550°C.
  • the inorganic materials melt into a slag and a metal alloy 8 accumulating in the lowest section 7 of the gasifier 1.
  • the accumulated liquid slag/metal alloy 8 should be tapped off at specific intervals.
  • waste materials contain enough silica to provide a glassy and leach resistant slag. Otherwise silica in the form of glass containing waste or a silica-containing mineral should be added.
  • the inorganic material in the waste/biomass melts in the gasifier and appears in the following manner:
  • Precious metals like gold, silver, copper, platinum, palladium etc., form a metal alloy that can be refined in a copper smelter.
  • Metals with higher affinity to oxygen than iron like Al, Ti, Mg, and Ca
  • iron like Al, Ti, Mg, and Ca
  • the slag fulfils the requirements to be used as construction material.
  • Part of the iron will be dissolved in the slag as iron oxide and part of it will be dissolved in the metal alloy.
  • By adding coal and limestone to the charge more iron will be reduced and dissolved in the metal.
  • Volatile metals like zinc, lead, cadmium and mercury are evaporated and leave the gasifier as part of the pyrolysis gas. These metals/metal oxides need to be removed from the syngas before entry into the Fischer-Tropsch synthesis. This may be obtained by acid scrubbing, cyclones, filtering or any other conventional technique known to remove solid particles of metals/metal oxides from a gas stream.
  • the temperature of the tapped slag and metal 8 is 1.450 - 1.550 °C, and during storage and cooling metal and slag separates due to the difference in specific weight. The freezing point is around 800 - 1.000 °C. After about one hour the slag on the top has frozen and the ladle is transported to a dedicated place for storage and cooling.
  • the ladle is tilted around and the slag and metal fall apart due to the different in thermal expansion.
  • the ladles are cone shaped and the metal and slag falls easily out of the ladles.
  • the slag is leach resistant and approved for use as fill material.
  • the gasifier is equipped with a rupture disc that bursts if the pressure in the gasifier exceeds 1.5 bar (a), and the pressure is relieved.
  • the relief will pass a pressure relief tank where particles from the gasifier will be captured.
  • the small amounts of gas leaked through the lock hopper system may be sucked off and recycled together with the secondary air to the plasma generator, thereby avoiding emissions to the environment.
  • a suited heat source for this invention is an arc discharge reactor which may heat a gaseous stream entering the discharge zone to many thousands degrees.
  • a plasma torch has also the advantage that the heat energy comes from electric energy, providing the possibility of atomising the gas compounds in an environment fully protected from the surrounding atmosphere and eliminating the need for introducing fuels or other forms of chemical energy carriers for providing the heat. This feature gives a plasma reactor the possibility of keeping an excellent control with the stochiometric conditions in the reaction zone (plasma/atomised gas zone) and subsequent condensation zone where the heat treated biosyngas is formed.
  • the gasified solid biomass/waste materials in outlet pipe 9 from the gasifier 1 is injected into zone 14 where it is mixed with the air jet discharged from the plasma torch 13 as shown in Figure 2.
  • Biomass/waste in the form of gas or liquid enters the air jet in the arc discharge zone 14.
  • the plasma torch 13 provides an air jet of high velocity and temperature (6 - 800 m/s and 3 - 5.000°C).
  • the air jet provides the necessary high temperature and immense dynamic power to completely decompose all hydrocarbons - even halogenated hydrocarbons like PAH, furans, and dioxins.
  • the plasma reactor gives the opportunity to dispose any liquid or gaseous waste/biomass materials by introducing them directly into the arc discharge zone 14. This is illustrated by reference number 12 on Figure 2.
  • the plasma torch may be placed in a T-junction on the outlet pipe 9 such as shown in Figure 3. Then the raw biosyngas exiting the gasifier 1 enters pipe 9 and where it is mixed with air to obtain the required oxidising conditions (the mixing means are not shown on the Figure). Then the mixed gas of air and biosyngas is admixed with hot gas exiting the plasma torch 13 before the heated gas mixture enters the decomposition reactor 15.
  • the plasma torch 13 may be configured as shown in Figure 4.
  • the torch is formed as a cylindrical tube with a set of apertures 23 for injection of air into an electric arc 21 running from annularly shaped electrodes 20.
  • the electric arc is rotated and controlled by annularly shaped magnets 22.
  • the tube forming the torch is sealed in one end and open in the other for allowing exit of the heated air.
  • the opening is directed into pipe 9, and the heated air exiting the torch has a temperature in the range of 3000 to 5000 °C.
  • the content of CO and CO 2 of the heat treated syngas is continuously recorded and controlled by regulating the fresh air injection 1 1 in order to maintain the following requirements: 0.2 ⁇ CO 2 /(CO 2 + CO) ⁇ 0.4. If the oxidation ratio becomes lower than 0.1 , HCN may be formed and if the oxidation ratio exceeds 0.5, the formation of NO x takes place. It is easy to operate the process between 0.2 and 0.4.
  • the heat treated syngas has a temperature of about 1250 °C when leaving the decomposition reactor 15. This temperature should be lowered to 150 °C before purification of the syngas.
  • the extracted heat should preferably be used for production of electric energy, by for example a steam turbine driven generator.
  • the gas cleaning system can be designed in different ways.
  • the two main alternatives are a wet or a combined dry and wet system.
  • a wet gas cleaning system can contain the following main equipment; a water quench precipitating dust and acid components, a two-stage scrubber cooling the gas and polishing the acid components including the sulphur and a wet electrostatic precipitator.
  • a combined dry and wet system will contain the following main equipment; a bag filter capturing the dust, a water quench precipitating the acid components and a two stage scrubber cooling the gas and polishing the acid components including the sulphur. If the waste contains mercury there might be necessary to have an activated carbon filter at the end of the gas cleaning system.
  • the inventive process decomposes chlorinated and halogenated hydrocarbons and dioxin, such that no special cleaning systems to capture these elements need to be included.
  • the plasma powered decomposition reactor decomposes all the tar components which is the main challenge to all gasification processes.
  • the NOx content in the fuel gas is less than 30 ppm.
  • the conditioning of the heat treated syngas and the following Fischer-Tropsch analysis are conventional technology known to a skilled person in the art. Any such process able to condition a syngas to meet the requirements of the Fischer-Tropsch synthesis may be employed. The same applies for and any conventional Fischer- Tropsch reactor and process.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Materials Engineering (AREA)
  • Dispersion Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The invention concerns a method and a plant for producing hydrocarbon based fuels from waste and biomass including wood and/or other cellulose containing biomass, where biomass and/or waste is gasified in anaerobic conditions, heating the formed syngas in for decomposition and subsequent condensation in anaerobic conditions, subjecting the heat treated biosyngas to cleaning measures for removing elements/compounds which are poisonous towards the catalysts of the Fischer-Tropsch synthesis, and passing the cleaned heat treated biosyngas through a Fischer-Tropsch synthesis for production of biofuels.

Description

Process and plant for production of biofuels
The invention concerns a method and a plant for producing hydrocarbon based fuels from waste and biomass including wood and/or other cellulose containing biomass.
Background The Intergovernmental Panel of Climate Change has recently released its fourth assessment report on climate change (IPCC 4AR), stating with very high confidence that human activities results in a climate forcing that may give dangerously strong climate changes in many regions of the world unless there is introduced substantial decreases in the emissions of greenhouse gases, especially carbon dioxide in the coming decades. The scientific discoveries and climate forcing knowledge expressed in IPCC 4AR is expected to result in both international agreements and national decisions for restrictions on emissions of carbon dioxide of fossil origin in the coming years.
One of the major contributing sectors of carbon dioxide emissions in developed countries is the transport sector, which presently is almost fully run on derivatives of fossil oil. The present transport sector utilises vehicles dependent on a chemical energy carrier able to be carried in the vehicles and delivering the energy to the engines of the vehicles, thus the problem of reducing greenhouse gas emissions from the transport sector becomes a question of finding another chemical energy carrier with sufficiently high energy density and which do not add net carbon to the earth carbon cycle.
Fuels made from waste and/or biomasses are very suited as replacement for fossil fuels such as gasoline and diesel. These fuels, e.g. bioethanol and biodiesel respectively, have a sufficient energy density suitable for present day transportation vehicles, they have similar chemical and physical properties such that they may be distributed and handled by present fuel distribution systems, and present day vehicles may be run on fossil fuels admixed with certain amounts of biofuels. Also, the technology for making engines run on pure biofuels is well developed, such that biofuels have capacity of eliminating greenhouse gas emissions from vehicles. Biofuels are presently made from agricultural leftovers and especially designated crops, so-called energy crops. However, the need for reserving arable land for food production and the large fuel volumes required by the transport sector calls for use of wood and other cellulose containing biomass as raw material in the future.
Prior art In a paper by Borriegter et al. presented at Pyrolysis and Gasification of Biomass and Waste, held at Strasbourg, France in 30 September - 1 October 2002, it is suggested using a biomass gasifϊer for producing a syngas from solid biomass and then feeding the syngas to a Fischer-Tropsch reactor for converting the syngas by the Fischer-Tropsch synthesis to biodiesel of high purity termed "green diesel" to distinguish this product from ordinary biodiesel made by esterfication of vegetable oils. An integrated biomass gasifier (BG) and Fischer-Tropsch (FT) plant may obtain large production volumes, and have an additional advantage in that the syngas after FT-synthesis contains sufficient rest energy to be employed in a combined cycle plant for production of electricity.
Conventional biomass gasifiers, such as the widely used circulating fluidised bed (CFB) gasifiers which operates with air as gasification medium at near atmospheric pressure and about 850 °C, produces a raw biosyngas with typical compositions of 15-20 parts by volume of CO, H2, and CO2, 10-15 parts by volume H2O, about 40 parts by volume N2, about 5 parts by volume CH4, and smaller amounts of C2H2, C2H4, C2H6, benzene, toluene, xylenes and tars. In addition there will be smaller amounts of inorganic impurities such as NH3, HCl, H2S, COS, CS2, HCN, HBr, dust, soot, and ash. The syngas components H2 and CO of the raw biosyngas will typically contain somewhat less than half of the chemical energy, while the rest are mainly contained by the CH4 and the other hydrocarbons.
The Fischer-Tropsch synthesis is a catalytically conversion of CO and H2 to hydrocarbons: 1 CO + 2 H2 o -(CH2)- + H2O
The synthesis consumes hydrogen and carbon monoxide in a ratio of H2:CO = 2. When the ratio in the feed gas is lower, it may be adjusted in a water-gas shift reaction:
2 CO + H2O <-> CO2 + H2 The catalysts of the FT-synthesis are sensitive towards poisoning from several of the compounds found in raw biosyngas. Thus the raw syngas needs to be purified before being used as feed gas in the FT-synthesis. Typical limits for safe levels of some compounds are:
H2S + COS + CS2 < 1 ppmV NH3 + HCN < 1 ppmV
HCl + HBr + HF < 10 ppbV alkaline metals, solids, tars < dew point class 2 tars < 1 ppmV
There are available conventional solutions for cleaning the feed gas for all compounds below the levels specified above, except for tars. Removal of tars remains a serious problem for production of biofuels from solid biomass by biomass gasification and Fischer-Tropsch synthesis of the gasified biomass, and has so far prevented commercial exploitation of this process route.
WO 2007/000607 discloses a method for removing solid remnants termed "char" in the document from an off-gas produced by gasifying waste in a reactor at under- stochiometric conditions. The char may include tarry compounds. The document teaches that subjecting the off-gas including char to a plasma treatment unit in presence of oxygen and optionally steam, may overcome or at least mitigate the problem with char in the off-gas.
Objective of the invention The main objective of this invention is to provide a method for production of biofuels by combined biomass gasification and Fischer-Tropsch synthesis which eliminate the problem with tar poisoning the catalysts in the Fischer-Tropsch synthesis.
It is also an objective of this invention to provide a method that may allow employing waste in combination with or as a substitute for biomass as raw material for the syngas fed to the Fischer-Tropsch synthesis.
Another objective is to provide a plant for performing the method according to the invention.
The objectives of the invention may be obtained by the features as set forth in the following description of the invention and/or in the appended claims.
Description of the invention
The invention is based on the realisation that a combination of a strong heating of a raw syngas exiting a gasifϊer causing an atomisation of substantially all compounds of the raw syngas and thus destruction of all organic compounds in the raw syngas including tars, dioxins etc. and a subsequent rapid condensation of the atomised syngas in certain anaerobic conditions, will result in that practically all organic elements in the raw syngas will be converted to low-molecular anaerobic combustion products, primarily CO, CO2, H2O, and H2. Thus the problem with tar in a raw syngas from gasifying biomass becomes practically eliminated. In a first aspect, the invention is a method for producing biofuels and similar hydrocarbon products from waste and/or biomass, comprising:
- gasification of the waste/biomass in anaerobic conditions to produce a raw biosyngas,
- admixing the raw biosyngas with air to obtain an oxidation degree in the range of 0.2 < CO2/(CO+CO2) < 0.4,
- contacting the raw biosyngas and air mixture with an air stream heated to a temperature in the range from 3000 to 5000 0C, elevating the temperature of the biosyngas to at least 1250°C,
- chilling the heat treated gas mixture to a temperature in the range of 100 - 200 0C to form a heat treated biosyngas,
- subjecting the heat treated biosyngas to cleaning measures for removing elements/compounds which are poisonous towards the catalysts of the Fischer- Tropsch synthesis to at least a tolerable level for the catalysts of the Fischer- Tropsch synthesis, and
- passing the cleaned heat treated biosyngas through a Fischer-Tropsch synthesis for production of biofuels. In a second aspect, the invention is a device for producing biofuels from waste and/or biomass, comprising:
- a gasifier forming a raw biosyngas from the waste/biomass,
- means for admixing a controlled amount of air into the raw biosyngas exiting the gasifier to obtain an oxidation degree in the range of 0.2 < CO2/(CO+CO2) < 0.4, - means for transporting the mixture of raw biosyngas and air to a heat treatment chamber,
- a plasma reactor supplying a stream of inert gas heated to a temperature from 3000 to 5000 °C to the heating chamber where the heated inert gas is admixed with the mixture of raw biosyngas and air, - means for cooling the gas exiting the heat treatment chamber to a temperature in the range of 100 - 200 °C,
- means for transporting the gas mixture from the cooling means to cleaning measures for removing compounds which are poisonous towards the catalysts of the Fischer-Tropsch synthesis to at least a tolerable level for the catalysts of the Fischer-Tropsch synthesis, and
- means for transporting the cleaned heat treated biosyngas to a Fischer-Tropsch synthesis reactor for production of biofuels.
Eventual inorganic elements present in the raw syngas such as metals, sulphur, nitrogen etc. will form various oxides and hydrides, and should be substantially removed before entering the Fischer-Tropsch synthesis. Other poisonous compounds may e.g. be compounds containing alkaline earth metals, and halogens.
The biosyngas may advantageously be conditioned before entering the Fischer- Tropsch synthesis, i.e. harmonising the ratio between hydrogen and carbon monoxide to H2:CO = 2, or at least increasing the ratio towards the harmonised level of 2 by performing a water-gas shift reaction of the heat treated biosyngas. The conditioning may also include removal of excess CO2 by a conventional absorption process, by using water, amine or other known CO2-absorbents. The conditioning may also include removal of some or all N2 in the biosyngas. The term "biofuel" as used herein includes any hydrocarbon based fuel and other hydrocarbon based products where the hydrocarbons are made by Fischer-Tropsch synthesis of gasified biomass and/or waste material. The hydrocarbons may be more or less aliphatic single- or poly-branched hydrocarbon chains from 2 to more than 20 carbon atoms, and may also include a fraction of aromatic hydrocarbons. Hydrocarbons from 9 to 20 carbon atoms form the diesel fraction.
The term "gasification" as used herein means converting solid or liquid waste and/or biomass by evaporation and/or anaerobic decomposition to gas phase. The term "raw biosyngas" as used herein means any gas exiting the gasification step of waste materials and/or biomass. The term as used herein includes the case when the syngas is produced from gasification of only waste materials. The term "heat treated biosyngas" as used herein means the gas mixture resulting from the atomisation and subsequent condensation of the raw biosyngas. The term "cleaned biosyngas" as used herein means the gas mixture resulting from removal of compounds poisonous for the catalysts in the Fischer-Tropsch synthesis from the heat treated biosyngas.
The term "conditioned biosyngas" as used herein means biosyngas where the H2:CO ratio has been adjusted by a water-shift reaction, and may also include removal of excess CO2. The term "anaerobic" as used herein means a process in under- stochiometric amounts of oxygen, which is a reducing environment. The term "waste" as used herein includes any carbon or hydrocarbon containing material waste or virgin material, including hazardous waste materials (not radioactive hazards).
The invention is not limited to any specific gasification process or gasification equipment, it may employ any known and conceivable method for forming a gaseous mixture comprising CO, CO2, H2O and H2 from waste and/or biomass. However, the gasification process will normally be a heating of the waste and/or biomass with regulated amounts of air as gasification medium to temperatures in the range of 500 to 1500 0C, where the amount of air should be regulated to ensure under-stochiometric amounts of oxygen in the process such that the waste/biomass forms a gaseous mixture comprising CO, CO2, H2O and H2. Both the biomass and waste contains inorganic compounds that results in liquid or solid remains in the lower part of the gasifier. Biomass will generally contain less inorganic material than waste. The gasifier should have means for taking out the inorganic residues accumulating in the lower lying section of the gasifier. A proven and well known conventional technique for gasification of large volumes of biomass is the circulating fluid bed gasifier mentioned above operating with air as gasification medium at about atmospheric pressure and 850 °C, and which gives a raw biosyngas with typical compositions of 15-20 parts by volume of CO, H2, and CO2, 10-15 parts by volume H2O, about 40 parts by volume N2, about 5 parts by volume CH4, and smaller amounts of C2H2, C2H4, C2H6, benzene, toluene, xylenes and tars. In addition there will be smaller amounts of inorganic impurities such as NH3, HCl, H2S, COS, CS2, HCN, HBr, dust, soot, and ash.
A proven technology for gasification of solid waste materials is counter counter- current-flow shaft gasifiers known from the steel industry. These gasifiers are fed with solid waste material at the top, usually through a gas tight sluice at the top.
The waste is at the upper section heated to a temperature in the order of 300-500 0C such that all volatile organic material and water is evaporated. Pre-heated air is simultaneously injected in the bottom of the gasifier and the remaining carbon is gasified in the bottom at a temperature of about 1500°C. The non-combustible materials like metals, ashes etc. are tapped of as a metal alloy and a non-leaching slag. This type of shaft gasifier combines rugged design with low thermal losses and long lining life. It is fully sealed so that all material that leaves the gasifier is either treated at high temperature (melted) or sent to the plasma powered decomposition reactor for high temperature treatment. The Fischer-Tropsch synthesis is well established conventional technology using iron-based catalysts or cobalt-based catalysts. The FT-synthesis is well known to a person skilled in the art and need no further description. The invention is not limited to the choice of Fischer-Tropsch reactor design and/or operation. Any known and conceivable Fischer-Tropsch reactor and synthesis process may be employed by the invention.
The catalysts of the Fischer-Tropsch synthesis are very sensitive towards poisoning by certain elements and solid particles in the feed gas. The heat treated biosyngas according to the invention will contain small amounts of sulphur oxides/hydrides, nitrogen oxides/hydrides, halogen hydrides, and solid particles of alkaline metal oxides/hydrides that need to be lowered below the levels specified above. There are well established conventional cleaning technologies based on gas scrubbing and/or filtration available for removing all impurities in the heat treated biosyngas according to the invention. Also, the invention is not limited to a specific choice of cleaning method or device, any known and conceivable gas cleaning technology may be employed as long as the impurity levels reaches below the levels specified in the prior art section above. Such technologies are well known to a person skilled in the art and need no further description.
The invention is in principle not restricted to any specific choice of heat source for heat treating the raw biosyngas exiting the gasifier. However, the heat-treatment should heat the entire stream of raw biosyngas exiting the gasifier to a temperature which ensures that practically all organic compounds including eventual halo- organic compounds in the gas stream are fully decomposed/atomised. This requirement makes heating by use of electric arcs very suited, since these heat sources may readily provide very intense heat under conditions which makes it relatively easy to obtain an environment which is sufficiently reducing (oxygen depleted) to ensure that the organic constituents in the decomposed/atomised gas stream condenses to mainly low molecular combustion products such as CO, CO2, H2O and H2. This requirement will be fulfilled by a heating the gas stream to a temperature of at least about 1250 °C, but preferably much higher, with a oxidation degree in the range of 0.2 < CO2/(CO+CO2) < 0.4. This degree of oxidation, that is reducing environment will suppress formation of unwanted combustion products such as NOx and HCN to acceptable levels, and it will ensure that large organic and halo-organic compounds such as tars and dioxins, respectively cannot be formed. The feature of heat treating the raw biosyngas to a temperature decomposing any tar and organic compound such as hydrocarbons in the raw biosyngas in a reducing environment ensuring conversion to low molecular combustion products eliminates the problem with tar poisoning the Fischer-Tropsch catalysts. The conversion of tar and organic compounds in the raw biosyngas offer another advantage in that the energy content in those compounds are converted to syngas and thus made available for the Fischer-Tropsch synthesis. Thus the inventive method obtains a higher yield as measured by produced biofuels than prior art solutions. A further advantage of the invention is that it will become possible to safely use any carbon or hydrocarbon containing materials including hazardous waste materials since all hazardous compounds are fully decomposed by the heat treatment and condensed to low molecular combustion products.
The inventive combination of a gasifier producing a raw syngas from biomass and/or waste materials, heating the raw syngas to at least about 1250 °C in an environment with a oxidation degree in the range of 0.2 < CO2/(CO+CO2) < 0.4, removal of inorganic compounds from the heat treated syngas, eventual conditioning of the syngas before entering into a Fischer-Tropsch synthesis, provides a safe and cost-effective production method for biofuels from any hydrocarbon and carbon containing material such as municipal waste, industrial waste fractions, waste from food industry, waste from agriculture, fish processing industry, biomass from forestry etc. These material sources provide a cheap and abundant source allowing large scale production of biofuels and simultaneous reduction of waste problems.
The heat treated syngas exits the heat treatment with a temperature in the order of 1000-1500 °C and should be cooled to about 100-200 °C before cleaning. This heat extraction may advantageously be utilised, for instance by a steam turbine to produce mechanical work or electricity.
Example of an embodiment of the invention
The invention will be verified and described in further detail by providing an example of an embodiment carrying out the method according to the invention. This embodiment should not be considered as a limitation of the general inventive idea of decomposition and subsequent condensation to convert all organic including halo-organic compounds in the syngas to low-molecular anaerobic combustion products. Any combination of gasifier, heat treatment device able to heat the raw syngas to at least 1250 °C and then rapidly condensate the atomised gas/plasma gas to low molecular anaerobic combustion products, and Fischer- Tropsch reactor are within the inventive scope of this invention.
The gasifier according to the example embodiment of the invention is a counter counter-current-flow shaft as shown in Figure 1. This gasifier 1 comprises a waste/biomass inlet 10 with a two-port sluice system for introduction of waste/biomass 2 in the upper region 4 of the gasifier 1. There the temperature will typically be in the order of 200-500 °C such that all volatile organic material and water is evaporated. The gasifier is sealed towards ambient atmosphere, and the introduction of fresh air is controlled to give an oxygen deficit in the gasifier. Thus, as the waste/biomass 2 descends down into the bulk zone 5 of the gasifier 1, it heats up in a reduced atmosphere and becomes gradually transformed to a low grade charcoal containing inorganic material. In the case of using waste materials, these inorganic materials may be i.e. glass, metal and minerals, typically containing around 10 - 30 % of fix carbon. Fix carbon means carbon that does not evaporate in the gasifier but remains down trough the carburisation zone. If the fix carbon in the waste becomes too low, biomass or other carbon source should be fed to the gasifier to provide the required temperature in the bottom of the gasifier.
The charcoal descending from the carbonization zone 5 into the partial oxidation and vitrification zone 6 is gasified by partly combustion with preheated air 3. The partial combustion provides a temperature in the bottom of 1.450 — 1.550°C. At this temperature the inorganic materials melt into a slag and a metal alloy 8 accumulating in the lowest section 7 of the gasifier 1. The accumulated liquid slag/metal alloy 8 should be tapped off at specific intervals. Normally, waste materials contain enough silica to provide a glassy and leach resistant slag. Otherwise silica in the form of glass containing waste or a silica-containing mineral should be added.
The inorganic material in the waste/biomass melts in the gasifier and appears in the following manner: Precious metals like gold, silver, copper, platinum, palladium etc., form a metal alloy that can be refined in a copper smelter. Metals with higher affinity to oxygen than iron (like Al, Ti, Mg, and Ca) oxidise and dissolve in the slag. The slag fulfils the requirements to be used as construction material. Part of the iron will be dissolved in the slag as iron oxide and part of it will be dissolved in the metal alloy. By adding coal and limestone to the charge more iron will be reduced and dissolved in the metal. Volatile metals like zinc, lead, cadmium and mercury are evaporated and leave the gasifier as part of the pyrolysis gas. These metals/metal oxides need to be removed from the syngas before entry into the Fischer-Tropsch synthesis. This may be obtained by acid scrubbing, cyclones, filtering or any other conventional technique known to remove solid particles of metals/metal oxides from a gas stream. The temperature of the tapped slag and metal 8 is 1.450 - 1.550 °C, and during storage and cooling metal and slag separates due to the difference in specific weight. The freezing point is around 800 - 1.000 °C. After about one hour the slag on the top has frozen and the ladle is transported to a dedicated place for storage and cooling. Twenty four hours after tapping the ladle is tilted around and the slag and metal fall apart due to the different in thermal expansion. The ladles are cone shaped and the metal and slag falls easily out of the ladles. The slag is leach resistant and approved for use as fill material.
For safety reasons, the gasifier is equipped with a rupture disc that bursts if the pressure in the gasifier exceeds 1.5 bar (a), and the pressure is relieved. The relief will pass a pressure relief tank where particles from the gasifier will be captured.
The small amounts of gas leaked through the lock hopper system may be sucked off and recycled together with the secondary air to the plasma generator, thereby avoiding emissions to the environment.
A suited heat source for this invention is an arc discharge reactor which may heat a gaseous stream entering the discharge zone to many thousands degrees. A plasma torch has also the advantage that the heat energy comes from electric energy, providing the possibility of atomising the gas compounds in an environment fully protected from the surrounding atmosphere and eliminating the need for introducing fuels or other forms of chemical energy carriers for providing the heat. This feature gives a plasma reactor the possibility of keeping an excellent control with the stochiometric conditions in the reaction zone (plasma/atomised gas zone) and subsequent condensation zone where the heat treated biosyngas is formed.
Thus, the gasified solid biomass/waste materials in outlet pipe 9 from the gasifier 1 is injected into zone 14 where it is mixed with the air jet discharged from the plasma torch 13 as shown in Figure 2. Biomass/waste in the form of gas or liquid enters the air jet in the arc discharge zone 14. The plasma torch 13 provides an air jet of high velocity and temperature (6 - 800 m/s and 3 - 5.000°C). The air jet provides the necessary high temperature and immense dynamic power to completely decompose all hydrocarbons - even halogenated hydrocarbons like PAH, furans, and dioxins. The plasma reactor gives the opportunity to dispose any liquid or gaseous waste/biomass materials by introducing them directly into the arc discharge zone 14. This is illustrated by reference number 12 on Figure 2. There may also be injected fresh air 11 into the arc discharge zone 14 in order to maintain the degree of oxidation within 0.2 < CO2/(CO+CO2) < 0.4. The decomposition of practically all larger molecules are ensured by injecting the plasma gas stream exiting zone 14 into a decomposition reactor 15 where the residence time of the gas is typically around 2 seconds and the temperature is maintained at about 1250 °C. Then the waste/biomass material is fully converted to a heat treated syngas exiting the decomposition reactor 15 through outlet pipe 16.
As an alternative, the plasma torch may be placed in a T-junction on the outlet pipe 9 such as shown in Figure 3. Then the raw biosyngas exiting the gasifier 1 enters pipe 9 and where it is mixed with air to obtain the required oxidising conditions (the mixing means are not shown on the Figure). Then the mixed gas of air and biosyngas is admixed with hot gas exiting the plasma torch 13 before the heated gas mixture enters the decomposition reactor 15.
The plasma torch 13 may be configured as shown in Figure 4. The torch is formed as a cylindrical tube with a set of apertures 23 for injection of air into an electric arc 21 running from annularly shaped electrodes 20. The electric arc is rotated and controlled by annularly shaped magnets 22. The tube forming the torch is sealed in one end and open in the other for allowing exit of the heated air. The opening is directed into pipe 9, and the heated air exiting the torch has a temperature in the range of 3000 to 5000 °C.
The content of CO and CO2 of the heat treated syngas is continuously recorded and controlled by regulating the fresh air injection 1 1 in order to maintain the following requirements: 0.2 < CO2/(CO2 + CO) < 0.4. If the oxidation ratio becomes lower than 0.1 , HCN may be formed and if the oxidation ratio exceeds 0.5, the formation of NOx takes place. It is easy to operate the process between 0.2 and 0.4.
The heat treated syngas has a temperature of about 1250 °C when leaving the decomposition reactor 15. This temperature should be lowered to 150 °C before purification of the syngas. The extracted heat should preferably be used for production of electric energy, by for example a steam turbine driven generator.
The gas cleaning system can be designed in different ways. The two main alternatives are a wet or a combined dry and wet system. A wet gas cleaning system can contain the following main equipment; a water quench precipitating dust and acid components, a two-stage scrubber cooling the gas and polishing the acid components including the sulphur and a wet electrostatic precipitator.
A combined dry and wet system will contain the following main equipment; a bag filter capturing the dust, a water quench precipitating the acid components and a two stage scrubber cooling the gas and polishing the acid components including the sulphur. If the waste contains mercury there might be necessary to have an activated carbon filter at the end of the gas cleaning system.
The inventive process decomposes chlorinated and halogenated hydrocarbons and dioxin, such that no special cleaning systems to capture these elements need to be included. The plasma powered decomposition reactor decomposes all the tar components which is the main challenge to all gasification processes. The NOx content in the fuel gas is less than 30 ppm.
The conditioning of the heat treated syngas and the following Fischer-Tropsch analysis are conventional technology known to a skilled person in the art. Any such process able to condition a syngas to meet the requirements of the Fischer-Tropsch synthesis may be employed. The same applies for and any conventional Fischer- Tropsch reactor and process.

Claims

1. Method for producing biofuels from waste and/or biomass, comprising:
- gasification of the waste/biomass in anaerobic conditions to produce a raw biosyngas, - admixing the raw biosyngas with air to obtain an oxidation degree in the range of 0.2 < CO2/(CO+CO2) < 0.4,
- contacting the raw biosyngas and air mixture with an air stream heated to a temperature in the range from 3000 to 5000 0C, elevating the temperature of the biosyngas to at least 1250 °C, - chilling the heat treated gas mixture to a temperature in the range of 100 -
200 °C to form a heat treated biosyngas,
- subjecting the heat treated biosyngas to cleaning measures for removing elements/compounds which are poisonous towards the catalysts of the Fischer- Tropsch synthesis to at least a tolerable level for the catalysts of the Fischer- Tropsch synthesis, and
- passing the cleaned heat treated biosyngas through a Fischer-Tropsch synthesis for production of biofuels.
2. Method according to claim 1 , characterised in that the poisonous compounds are one or more of the following: compounds containing alkaline earth metals, sulphur, halogens, and nitrogen.
3. Method according to claim 1, characterised in that the heat treatment is made by admixing the raw biosyngas exiting the gasifier with the gas stream exiting a plasma torch.
4. Method according to claim 3, characterised in that the raw biosyngas is injected into an arc discharge zone of an air stream from the plasma generator with velocity 6 - 800 m/s and temperature of 3 - 5.000 0C, and then enters a decomposition reactor where the temperature is in the range of 1200-1300 °C for about 2 seconds.
5. Method according to claim any of the preceding claims, characterised in that the heat treated biosyngas is conditioned by adjusting the
H2:CO ratio by a water shift reaction converting CO in the syngas to CO2 and H2 by reacting CO with water, before entry into the Fischer-Tropsch synthesis.
6. Method according to claim 5, characterised in that the conditioning of the heat treated biosyngas also comprises removal of at least a portion of the CO2 in the biosyngas.
7. Method according to claim 6, characterised in that the conditioning of the heat treated biosyngas also comprises removal of at least a portion of the N2 in the biosyngas.
8. Method according to claim 1, characterised in that the gasifier is fed with biomass.
9. Method according to claim 8, characterised in that the biomass comprises biomass containing cellulose.
10. Method according to claim 9, characterised in that waste comprises one or more of the following materials; municipal waste, industrial waste fractions, waste from food industry, and waste from agriculture and/or fish processing industry.
11. Device for producing biofuels from biomass, comprising:
- a gasifier forming a raw biosyngas from the waste/biomass,
- means for admixing a controlled amount of air into the raw biosyngas exiting the gasifier to obtain an oxidation degree in the range of 0.2 < CO2/(CO+CO2) <
0.4,
- means for transporting the mixture of raw biosyngas and air to a heat treatment chamber,
- a plasma reactor supplying a stream of inert gas heated to a temperature from 3000 to 5000 °C to the heating chamber where the heated inert gas is admixed with the mixture of raw biosyngas and air,
- means for cooling the gas exiting the heat treatment chamber to a temperature in the range of 100 - 200 °C,
- means for transporting the gas mixture from the cooling means to cleaning measures for removing compounds which are poisonous towards the catalysts of the Fischer-Tropsch synthesis to at least a tolerable level for the catalysts of the Fischer-Tropsch synthesis, and
- means for transporting the cleaned heat treated biosyngas to a Fischer-Tropsch synthesis reactor for production of biofuels.
12. Device according to claim 11 , characterised in that the cleaning measures are aimed at removing one or more of the following: compounds containing alkaline earth metals, sulphur, halogens, and nitrogen.
13. Device according to claim 1 1 or 12, characterised in that the gasifier 1 is a counter counter-current-flow shaft gasifier comprising:
- a waste/biomass inlet 10 with a two-port sluice system for introduction of waste/biomass 2 in the upper region 4 of the gasifier 1 , - a carbonization zone 5,
- a partial oxidation and vitrification zone 6,
- inlet 3 for injection of preheated air at the partial oxidation and vitrification zone 6, - a slag and metal alloy accumulating section 7,
- means 8 for tapping and collecting liquid slag and metal alloy, and
- means for regulating the injection of fresh air to maintain a temperature of 1.450 - 1.550°C in the slag and metal alloy accumulating section 7.
14. Device according to claim 13, characterised in that the decomposition reactor 15 comprises a plasma torch 13 placed in a T-junction on the outlet tube 9 providing an arc discharge zone 21 in which air is injected, and that the heated air exits the plasma torch 13 through zone 14 where it is admixed with raw biosyngas, and that the mixed gas then flows into a decomposition chamber 15.
15. Device according to claim 13, characterised in that
- the plasma torch 13 is formed as a cylindrical tube closed in one end and open in the other end and which is equipped with a set of apertures 23 for injection of air, - that an electric arc 21 is formed between two annularly shaped electrodes 20 and which is rotated and controlled by annularly shaped magnets 22, and
- the opening of the cylindrical tube is directed into tube 9 and thus forming a zone 14 where air heated by passing through apertures 23 and into arc 21 may pass into tube 9.
16. Device according to claim 15, characterised in that the plasma torch provides an air jet of flow velocity 6 - 800 m/s and a temperature of 3 - 5.000 °C in zone 14, and that the decomposition reactor is given a volume that ensures a residence time of about 2 seconds at a temperature of 1200-1300 °C before the gas exits as heat treated syngas through pipe 16.
17. Device according to claim 16, characterised in that the pipe 9 is equipped with means for regulating the injection of air 11 such that the oxidation degree in the zone 14 and decomposition reactor 15 is kept within 0.2 < CO2/(CO+CO2) < 0.4.
PCT/NO2008/000245 2007-06-27 2008-06-27 Process and plant for production of biofuels WO2009002191A2 (en)

Priority Applications (3)

Application Number Priority Date Filing Date Title
US12/452,282 US20100216898A1 (en) 2007-06-27 2008-06-27 Process and plant for production of biofuels
EP08779092.9A EP2167613B1 (en) 2007-06-27 2008-06-27 Process for production of biofuels
DK08779092.9T DK2167613T3 (en) 2007-06-27 2008-06-27 PROCEDURE FOR MANUFACTURING BIOLOGIES

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
NO20073321A NO330096B1 (en) 2007-06-27 2007-06-27 Process and facility for the production of biofuels from waste and / or biomass.
NO20073321 2007-06-27

Publications (2)

Publication Number Publication Date
WO2009002191A2 true WO2009002191A2 (en) 2008-12-31
WO2009002191A3 WO2009002191A3 (en) 2009-02-19

Family

ID=40091986

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/NO2008/000245 WO2009002191A2 (en) 2007-06-27 2008-06-27 Process and plant for production of biofuels

Country Status (5)

Country Link
US (1) US20100216898A1 (en)
EP (1) EP2167613B1 (en)
DK (1) DK2167613T3 (en)
NO (1) NO330096B1 (en)
WO (1) WO2009002191A2 (en)

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2011061484A3 (en) * 2009-11-18 2011-07-07 Gtl.F1 Ag Fischer-tropsch catalyst comprising supported cobalt and low levels of alkaline earth metals, its preparation method and use for producing hydrocarbons
WO2011100720A2 (en) * 2010-02-13 2011-08-18 Roy Eward Mcalister Carbon recyling and reinvestment using thermochemical regeneration
WO2011084301A3 (en) * 2010-01-06 2011-11-17 General Electric Company System for removing fine particulates from syngas produced by gasifier
WO2011100721A3 (en) * 2010-02-13 2012-01-05 Mcalister Roy E Oxygenated fuel
WO2012031587A1 (en) * 2010-09-10 2012-03-15 Ettenberger Gmbh & Co. Kg High-temperature carbon reactor htcr
US8318997B2 (en) 2010-02-13 2012-11-27 Mcalister Technologies, Llc Carbon-based durable goods and renewable fuel from biomass waste dissociation
WO2013025627A2 (en) * 2011-08-12 2013-02-21 Mcalister Technologies, Llc Recycling and reinvestment of carbon from agricultural processes for renewable fuel and materials using thermochemical regeneration
EP2690162A1 (en) * 2012-07-24 2014-01-29 Fundacion Tecnalia Research & Innovation Equipment for treating gases and use of said equipment for treating a synthesis gas contaminated with tars
CN103965965A (en) * 2013-01-24 2014-08-06 通用电气公司 System and method for gasification
US8916735B2 (en) 2011-08-13 2014-12-23 Mcalister Technologies, Llc Carbon-based durable goods and renewable fuel from biomass waste dissociation for transportation and storage
US8975458B2 (en) 2010-02-13 2015-03-10 Mcalister Technologies, Llc Carbon-based durable goods and renewable fuel from biomass waste dissociation
EP2952557A1 (en) * 2014-06-02 2015-12-09 PHG Energy, LLC Microwave induced plasma cleaning device and method for producer gas
US9284191B2 (en) 2013-03-15 2016-03-15 Mcalister Technologies, Llc Carbon-based manufacturing of fiber and graphene materials
US9416328B2 (en) 2010-01-06 2016-08-16 General Electric Company System and method for treatment of fine particulates separated from syngas produced by gasifier
US12077435B2 (en) 2011-09-27 2024-09-03 Thermochem Recovery International, Inc. Method of generating clean syngas

Families Citing this family (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8667706B2 (en) * 2008-08-25 2014-03-11 David N. Smith Rotary biomass dryer
US9115324B2 (en) 2011-02-10 2015-08-25 Expander Energy Inc. Enhancement of Fischer-Tropsch process for hydrocarbon fuel formulation
US9169443B2 (en) 2011-04-20 2015-10-27 Expander Energy Inc. Process for heavy oil and bitumen upgrading
US9156691B2 (en) 2011-04-20 2015-10-13 Expander Energy Inc. Process for co-producing commercially valuable products from byproducts of heavy oil and bitumen upgrading process
US9315452B2 (en) 2011-09-08 2016-04-19 Expander Energy Inc. Process for co-producing commercially valuable products from byproducts of fischer-tropsch process for hydrocarbon fuel formulation in a GTL environment
US8889746B2 (en) 2011-09-08 2014-11-18 Expander Energy Inc. Enhancement of Fischer-Tropsch process for hydrocarbon fuel formulation in a GTL environment
CN104024182A (en) 2011-09-08 2014-09-03 强能公司 Enhancement of fischer-tropsch process for hydrocarbon fuel formulation in a gtl environment
EP2583754B1 (en) * 2011-10-21 2015-05-13 Enefit Outotec Technology Oü Process and apparatus for winning oil from a vapor gas mixture
EP2583753B1 (en) * 2011-10-21 2015-05-13 Enefit Outotec Technology Oü Process and apparatus for dedusting a vapour gas mixture
CN102618330B (en) * 2011-12-29 2014-02-26 武汉凯迪工程技术研究总院有限公司 High temperature normal pressure biomass gasification island process
CA2776369C (en) 2012-05-09 2014-01-21 Steve Kresnyak Enhancement of fischer-tropsch process for hydrocarbon fuel formulation in a gtl environment
FI20125658L (en) * 2012-06-14 2013-12-15 Upm Kymmene Corp Method and system for producing liquid fuel from biomass
US9074151B2 (en) 2012-09-28 2015-07-07 Adaptivearc, Inc. Plasma assisted gasification system with an indirect vacuum system
US9266730B2 (en) 2013-03-13 2016-02-23 Expander Energy Inc. Partial upgrading process for heavy oil and bitumen
CA2818322C (en) 2013-05-24 2015-03-10 Expander Energy Inc. Refinery process for heavy oil and bitumen
CN103316899B (en) * 2013-07-08 2016-07-06 苑忠宝 One way of life garbage flash mineralization treater box
US20170101316A1 (en) * 2014-05-29 2017-04-13 Advanced Green Technologies, Llc System for production of carbon and net hydrogen liquid fuels
CN108296259A (en) * 2017-12-29 2018-07-20 中广核研究院有限公司 A kind of waste treatment apparatus and method
CN108191194A (en) * 2018-02-24 2018-06-22 航天慧能(江苏)环境工程有限公司 A kind of sludge of sewage treatment plant plasma processing method
CN109709122B (en) * 2019-01-11 2021-02-05 中国人民解放军国防科技大学 Collection test device of congealing looks combustion products in high temperature gas
CN111676033B (en) * 2020-03-23 2021-12-07 同济大学 Gas making system and gas making method by utilizing wastes

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2003018721A1 (en) * 2001-08-22 2003-03-06 Global Plasma Systems Group, Inc. Plasma pyrolysis, gasification and vitrification of organic material
KR100636853B1 (en) * 2002-05-08 2006-10-19 로우 에드먼드 킨 온 Hazardous waste treatment method and apparatus
CA2424805C (en) * 2003-04-04 2009-05-26 Pyrogenesis Inc. Two-stage plasma process for converting waste into fuel gas and apparatus therefor
US7658155B2 (en) * 2005-06-29 2010-02-09 Advanced Plasma Power Limited Waste treatment process and apparatus
FR2892127B1 (en) * 2005-10-14 2012-10-19 Commissariat Energie Atomique DEVICE FOR GASIFYING BIOMASS AND ORGANIC WASTE AT HIGH TEMPERATURE AND WITH EXTERNAL ENERGY DELIVERY FOR THE GENERATION OF A HIGH-QUALITY SYNTHESIS GAS
US8444725B2 (en) * 2006-09-11 2013-05-21 Purdue Research Foundation System and process for producing synthetic liquid hydrocarbon
US8100996B2 (en) * 2008-04-09 2012-01-24 Velocys, Inc. Process for upgrading a carbonaceous material using microchannel process technology

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
None

Cited By (27)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2011061484A3 (en) * 2009-11-18 2011-07-07 Gtl.F1 Ag Fischer-tropsch catalyst comprising supported cobalt and low levels of alkaline earth metals, its preparation method and use for producing hydrocarbons
CN102782099A (en) * 2010-01-06 2012-11-14 通用电气公司 System for removing fine particulates from syngas produced by gasifier
US9416328B2 (en) 2010-01-06 2016-08-16 General Electric Company System and method for treatment of fine particulates separated from syngas produced by gasifier
WO2011084301A3 (en) * 2010-01-06 2011-11-17 General Electric Company System for removing fine particulates from syngas produced by gasifier
US8975458B2 (en) 2010-02-13 2015-03-10 Mcalister Technologies, Llc Carbon-based durable goods and renewable fuel from biomass waste dissociation
US8912239B2 (en) 2010-02-13 2014-12-16 Mcalister Technologies, Llc Carbon recycling and reinvestment using thermochemical regeneration
WO2011100721A3 (en) * 2010-02-13 2012-01-05 Mcalister Roy E Oxygenated fuel
US8318997B2 (en) 2010-02-13 2012-11-27 Mcalister Technologies, Llc Carbon-based durable goods and renewable fuel from biomass waste dissociation
CN102844413A (en) * 2010-02-13 2012-12-26 麦卡利斯特技术有限责任公司 Carbon-based durable goods and renewable fuel from biomass waste dissociation
CN102869754A (en) * 2010-02-13 2013-01-09 麦卡利斯特技术有限责任公司 Oxygenated fuel
WO2011100720A2 (en) * 2010-02-13 2011-08-18 Roy Eward Mcalister Carbon recyling and reinvestment using thermochemical regeneration
US9297530B2 (en) 2010-02-13 2016-03-29 Mcalister Technologies, Llc Oxygenated fuel
US8784095B2 (en) 2010-02-13 2014-07-22 Mcalister Technologies, Llc Oxygenated fuel
WO2011100720A3 (en) * 2010-02-13 2011-12-22 Roy Eward Mcalister Carbon recyling and reinvestment using thermochemical regeneration
CN102869754B (en) * 2010-02-13 2014-10-22 麦卡利斯特技术有限责任公司 Oxygenated fuel
WO2012031587A1 (en) * 2010-09-10 2012-03-15 Ettenberger Gmbh & Co. Kg High-temperature carbon reactor htcr
WO2013025627A2 (en) * 2011-08-12 2013-02-21 Mcalister Technologies, Llc Recycling and reinvestment of carbon from agricultural processes for renewable fuel and materials using thermochemical regeneration
US9193925B2 (en) 2011-08-12 2015-11-24 Mcalister Technologies, Llc Recycling and reinvestment of carbon from agricultural processes for renewable fuel and materials using thermochemical regeneration
WO2013025627A3 (en) * 2011-08-12 2013-05-10 Mcalister Technologies, Llc Recycling and reinvestment of carbon from agricultural processes for renewable fuel and materials using thermochemical regeneration
US8916735B2 (en) 2011-08-13 2014-12-23 Mcalister Technologies, Llc Carbon-based durable goods and renewable fuel from biomass waste dissociation for transportation and storage
US12077435B2 (en) 2011-09-27 2024-09-03 Thermochem Recovery International, Inc. Method of generating clean syngas
EP2690162A1 (en) * 2012-07-24 2014-01-29 Fundacion Tecnalia Research & Innovation Equipment for treating gases and use of said equipment for treating a synthesis gas contaminated with tars
CN103965965A (en) * 2013-01-24 2014-08-06 通用电气公司 System and method for gasification
US9284191B2 (en) 2013-03-15 2016-03-15 Mcalister Technologies, Llc Carbon-based manufacturing of fiber and graphene materials
EP2952557A1 (en) * 2014-06-02 2015-12-09 PHG Energy, LLC Microwave induced plasma cleaning device and method for producer gas
EP3106505A1 (en) * 2014-06-02 2016-12-21 PHG Energy, LLC Microwave induced plasma cleaning device and method for producer gas
US9976095B2 (en) 2014-06-02 2018-05-22 Aries Gasification, Llc Method for cleaning producer gas using a microwave induced plasma cleaning device

Also Published As

Publication number Publication date
DK2167613T3 (en) 2020-02-17
EP2167613B1 (en) 2019-11-06
US20100216898A1 (en) 2010-08-26
NO330096B1 (en) 2011-02-21
NO20073321L (en) 2008-12-29
EP2167613A2 (en) 2010-03-31
WO2009002191A3 (en) 2009-02-19

Similar Documents

Publication Publication Date Title
EP2167613B1 (en) Process for production of biofuels
AU2009308404B2 (en) Process for decontaminating syngas
KR100452099B1 (en) Waste treatment method and apparatus through vaporization
RU2572998C2 (en) Synthetic gas produced by plasma arc gasification
US5980858A (en) Method for treating wastes by gasification
RU2471856C2 (en) Autothermal method of continuous gasification of substances with high content of carbon
KR101622801B1 (en) Two stage entrained gasification system and process
AU2008340650B2 (en) Method and device for reprocessing CO2-containing exhaust gases
JP3723061B2 (en) Complete resource recycling method for waste without chimney using oxygen-enriched gas
US20020048545A1 (en) Synthesis gas production and power generation with zero emissions
EP2015859A2 (en) A gas conditioning system
EP0979262B1 (en) Method and apparatus for treating wastes by gasification
JP2012107110A (en) Method for treating gas-treatment drainage, gasification apparatus of carbonaceous material, and method for treating carbonaceous material
US9079767B2 (en) Countercurrent gasification using synthesis gas as the working medium
JPH09241666A (en) Use of residue, waste and low-heating value fuel in terms of energy in steam power generating plant
JP4561779B2 (en) Swivel melting furnace and waste gasification method using swirl melting furnace
JPH1067992A (en) Composition of plastic waste into resource and apparatus for conversion into resource
JP3938981B2 (en) Gas recycling method for waste gasification
JP3883253B2 (en) High temperature oxidation furnace and oxidation treatment method
JP3941196B2 (en) Waste gasification method and apparatus
KR102608619B1 (en) System and method for producing hydrogen using waste
WO2023161407A1 (en) Plant, device and process
Dong et al. Formation characteristics of sulfur compounds and PCDDs/PCDFs from dried sewage sludge pyrolysis/combustion utilizing fluidized bed reactor

Legal Events

Date Code Title Description
NENP Non-entry into the national phase

Ref country code: DE

WWE Wipo information: entry into national phase

Ref document number: 2008779092

Country of ref document: EP

121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 08779092

Country of ref document: EP

Kind code of ref document: A2

WWE Wipo information: entry into national phase

Ref document number: 12452282

Country of ref document: US