US20120117879A1 - Method for utilizing distillation fractions obtained from distillation of tall oil in btl or cellulose factory - Google Patents

Method for utilizing distillation fractions obtained from distillation of tall oil in btl or cellulose factory Download PDF

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US20120117879A1
US20120117879A1 US13/241,688 US201113241688A US2012117879A1 US 20120117879 A1 US20120117879 A1 US 20120117879A1 US 201113241688 A US201113241688 A US 201113241688A US 2012117879 A1 US2012117879 A1 US 2012117879A1
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Prior art keywords
tall oil
btl
plant
fraction
distillation column
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English (en)
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Jani MÄKELÄ
Mika TIMONEN
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Vapo Oy
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Vapo Oy
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
    • C11B13/00—Recovery of fats, fatty oils or fatty acids from waste materials
    • C11B13/005—Recovery of fats, fatty oils or fatty acids from waste materials of residues of the fabrication of wood-cellulose (in particular tall-oil)
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1011—Biomass
    • C10G2300/1014—Biomass of vegetal origin
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4025—Yield
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983—Additives
    • C10J2300/0989—Hydrocarbons as additives to gasifying agents to improve caloric properties
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
    • C10J2300/1606—Combustion processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1656—Conversion of synthesis gas to chemicals
    • C10J2300/1659—Conversion of synthesis gas to chemicals to liquid hydrocarbons
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1678—Integration of gasification processes with another plant or parts within the plant with air separation
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00—Technologies for solid waste management
    • Y02W30/50—Reuse, recycling or recovery technologies
    • Y02W30/74—Recovery of fats, fatty oils, fatty acids or other fatty substances, e.g. lanolin or waxes

Definitions

  • the invention relates to a method in accordance with the preamble of claim 1 for utilizing distillation fractions obtained from distillation of tall oil in a BtL or, when necessary, in a cellulose factory.
  • the invention also relates to a use in accordance with claim 8 .
  • Low-temperature gasifiers typically operate at a temperature of 1000° C. maximum and are implemented as either fixed-bed reactors (power rating less than 20 MW) or as fluidized-bed reactors (power rating above 20 MW). Fuel is fed into these reactors generally as a mass of solid, comminuted particles. Respectively, gasification takes place either above a fixed-bed distributor or in a fluidized bed. Use of liquid or gaseous raw materials in these gasifier types is difficult.
  • High-temperature gasifiers are operated at a temperature of about 1400° C. and carry out processes often requiring fuel comminuted to a fine particle size for firing a burner that serves as the gasifier unit.
  • This kind of embodiment is characterized by allowing the burner to be relatively easily fired also with liquid and gaseous raw materials whose combustion in low-temperature gasifiers is complicated.
  • high-temperature gasifiers are operated as pressurized reactions using oxygen or a mixture of oxygen and steam and/or carbon dioxide as the gasification agent.
  • a high-temperature gasifier is the gasification technology typically chosen for producing maximally pure syngas, e.g., for the needs of chemical or oil-refining industries.
  • the Fischer-Tropsch method abbreviated as the FT method, which is based on a catalyzed chemical reaction wherein synthesis gas containing only carbon monoxide and hydrogen is converted into various paraffinic hydrocarbons that at room temperature generally are waxy compounds. Typically, iron and cobalt catalysts are used.
  • the principal target of the method is to produce synthetic oil compounds for use as synthetic fuel or lubricant.
  • the processing of syngas obtained after cleaning the product gas of biomass gasification in an FT reactor and postprocessing of FT products as an entity is called a Biomass-to-Liquids process, abbreviated as a BtL process.
  • a Fisher-Tropsch reactor typically gives two end products: a heavier FT wax often denoted as Heavy Fischer-Tropsch Liquid (HFTL) with hydrocarbon chains of about 15 to 100 carbon atoms, and lighter liquid product called Light Fischer-Tropsch Liquid (LFTL) with hydrocarbon chains of 5 to 30 carbon atoms.
  • HFTL Heavy Fischer-Tropsch Liquid
  • LFTL Light Fischer-Tropsch Liquid
  • the FT products are taken to a refining unit designed to be compatible with the FT technique and catalyst used in the reactor.
  • the refining unit comprises plural different unit processes.
  • the term hydrogenation unit also known as a hydrotreater, primarily refers to a reactor wherein hydrogen is added to the reactive (unsaturated) bonds of a molecule. In other words, when a hydrogenated bond becomes saturated thereby losing its reactivity, the process is called hydrogenation or hydrogen bonding.
  • the term cracking simply means the conversion of large hydrocarbon molecules into a smaller size, whereby this process unit is also known a hydrocracker (hydrogen addition cracking unit). Isomerization refers to a process wherein hydrocarbon chains are branched to obtain better fuel qualities for use in engines (i.a., modification of fuel cloud point). In the final distillation step, the different fuel fractions are separated from each other to obtain end product fractions such as diesel fuel, kerosene and naphtha.
  • a BtL plant may be particularly advantageously designed to utilize the byproducts of forest industry plants such as those of the pulp/paper plants. Especially the use of byproducts obtained from a sulfate cellulose plant in a BtL plant may bring up mutual benefits.
  • tall oil by an average amount of 35 kg per ton of cellulose.
  • the tall oil composition varies by wood species, growth location and annual season of felling, whereby it contains about 35-70% fatty acids, 20-50% resin acids, while the remaining portion consists of 5-30% of neutral components.
  • Today, a very minor amount of crude tall oil is used in unprocessed form.
  • the major portion of crude tall oil is distilled into products that are consumed in, e.g., paint and adhesive manufacturing plants and production of tall oil soap.
  • tall oil as a fuel is very close to fuel oil with a heat value of about 38 MJ/kg, which is greater than 90% of the heat value of fuel oil.
  • tall oil is readily combustible or gasifiable in a modified oil burner.
  • cellulose plants Concurrently, cellulose plants generally sell tall oil due to its very high energy content for use as an industrial raw material outside their own processes. While the use of tall oil as a raw material for biofuel has been investigated, implementing such a refinery unit in conjunction with cellulose plants would make it too small in size and, hence, an unprofitable investment. Besides the need for pressurized processing, one additional limitation is the need for pure hydrogen that elevates the operating costs of the process excessively. A further problem is that heavy-fuel-oil-like character of tall oil requires its storage temperature to be kept in excess of 60° C., whereby its shipping also dictates special actions such as transport in insulated containers.
  • tall oil can be used as feedstock for a gasifier with the provision that the gasifier has a burner-type gasifier unit.
  • this alternative bypasses the already recognized high refining potential of tall oil and exploits only the energy content of this byproduct. Additionally such an infeed to a low-temperature gasifier is difficult to arrange as these gasifiers generally are fixed-bed or fluidized-bed reactors.
  • a distillation column is erected for processing tall oil.
  • distillation means separation of the feedstock components from each other by evaporation.
  • the separate components condense at different temperature ranges, they can be recovered in the distillation process as separate fractions, i.e., separate distillates, so that one fraction may contain one or more components.
  • the light fractions are recovered as a distillate whose hydrocarbon chains are closely similar to the HFTL liquid generated in an FT reactor thereby principally comprising different kinds of fatty acids.
  • the heavy and low-quality fractions not directly usable as vehicle fuel obtained from the distillation process are gasified in the gasification process of the BtL plant whereby this process most advantageously is a high-temperature pressurized oxygen gasifier.
  • These fractions typically are comprised of resin acids.
  • the amount of hydrocarbons is thus increased, more syngas can be processed that in turn improves the product yield of FT products and the overall productivity of the entire plant.
  • the light, gaseous fractions of the distillation process are combined with the other gaseous process products of the BtL plant, whereby they are utilized as a hydrogen or energy source in the BtL plant processes or boilers of a power plant.
  • An essential feature of the arrangement according to the invention is to utilize tall oil in a BtL plant, most advantageously in a BtL plant directly integrated with a cellulose plant.
  • the essential features of the invention are crucial to the disclosed method and its use as specified in the appended claims. More specifically, the invention is characterized by what is stated in the claims.
  • the essential goal of the invention is to utilize tall oil in the process steps of a BtL plant in such a fashion that the end product is a high-quality biofuel.
  • FIGS. 1-3 in which drawings:
  • FIGS. 1-3 show some process diagrams of arrangements for implementing the method according to the invention.
  • the process described below is related to a method depicted in FIGS. 1-3 for utilizing tall oil in a BtL plant.
  • An essential feature of the invention is that a BtL plant using the method can utilize tall oil in its different processes.
  • An advantageous alternative is to run the process integrated in particular with a sulfate cellulose plant in such a fashion that the BtL plant uses crude tall oil obtained from the sulfate cellulose plant, whereby the crude tall oil is passed along a pipeline to a distillation column integrated with the refinery unit of the BtL plant.
  • FIG. 1 illustrates the stages of a BtL process.
  • Solid biomass 19 is first taken to a biomass preprocessing step 1 , wherein the biomass particle size and moisture content are homogenized.
  • the preprocessed biomass is fed to a high-temperature gasification step 2 , whereto oxygen is passed from an oxygen plant 3 .
  • the gasification step may comprise a pregasification step, wherein the biomass is coked or torrefied, whereupon the pyrolysis gases released by the biomass are taken to a high-temperature oxygen gasifier and resulting product is milled and either passed to the burners of the high-temperature oxygen gasifier or the coke can be subjected to so-called chemical gas quenching, whereby the hydrogen content of the syngas increases and, due to endothermic reactions, the syngas is cooled.
  • the water required in the reaction comes to the process along with the biomass or water may be injected separately into the gasifier.
  • the gas generated in the gasifier is cooled in a heat exchanger 4 and cleaned free from solid impurities in step 5 .
  • the syngas pressure is elevated to the operating pressure of the refinery unit with the help of a compressor 6 .
  • the syngas hydrogen-carbon monoxide ratio is adjusted in step 7 and other components except for hydrogen and carbon monoxide are removed from the syngas in steps 8 , whereupon the syngas can be fed to a Fischer-Tropsch reactor 9 .
  • the FT fractions exiting the FT reactor are refined in the refinery unit 10 of the plant and thereupon distilled in distillation column 11 into end products 13 .
  • tall oil 18 from tall oil 18 are separated those hydrocarbon fractions 14 a / 14 b that due to their distillation properties and other qualities are close to the HFTL fraction processed in the FT reactor 9 from the syngas 8 .
  • the nonliquified light hydrocarbon fraction 17 are separated and used in energy generation, for instance.
  • the fatty oil distillates can be fed either via unit 14 a to the hydrocracking process of the refinery unit or via unit 14 b to end-product distillation.
  • unit 14 a to the hydrocracking process of the refinery unit
  • unit 14 b to end-product distillation.
  • FIGS. 2 and 3 The difference between these alternatives is illustrated in FIGS. 2 and 3 .
  • the refinery unit 10 of the BtL plant can be designed for an oversize capacity, whereby it can also process tall oil 18 received from plural sources. If a need in the process arises thereto, the hydrocracker unit can be complemented with a sulfur-removal facility or other modifications. No new process equipment or other postprocessing steps are required as will be described later in the text. In this fashion according to the invention, the light fractions of crude tall oil are processed into hydrocarbon chains of desired length and quality that are suited for processing high-quality biofuels.
  • the heaviest tall oil fractions generally known as bottoms distillate, bottoms oil or bottoms fraction 15 are processed in the gasification reactor 2 of the BtL plant and/or are used in energy generation 16 . Furthermore, if necessary, the bottoms fraction 15 may be returned to the cellulose plant and burnt there in a lime kiln.
  • the bottoms fraction (bottoms distillate) 15 of the distillation column contains tar-like hydrocarbon compounds of long carbon chains (longer than C 30 ) that are kept in a fluid state and next pumped from a storage container to the gasification reactor 2 of the BtL plant.
  • the gasification reactor 2 is a pressurized oxygen gasifier most advantageously operated at a high temperature, whereto the comminuted biomass is fed in pulverized form into the burner section of the reactor, wherein it reacts with oxygen to produce raw syngas.
  • the high-temperature gasifier facilitates a very simple arrangement for the gasification of the tall oil bottoms fraction.
  • the gasifier needs an infeed distributor whereon the heated bottoms fraction is pumped.
  • the feedstock will gasify completely and its ash will mix with the ash of the other raw material being combusted. No other new process equipment or refining steps are required as described later in the text.
  • An essential feature is that depending on the amount of tall oil feedstock, the capacity of a BtL plant may be increased by as much as 5-50% with regard to a plant not using tall oil as feedstock.
  • FIG. 2 is illustrated an embodiment of a distillation process in more detail.
  • tall oil 18 is fed into a distillation column 12 .
  • tall oil in liquid form is removed tall oil in liquid form and passed to a heater 20 , wherein the tall oil is evaporated.
  • the heater temperature is kept at a given level, the light fatty acids evaporating at a lower temperature are vaporized while the heavier fractions respectively remain in liquid form.
  • Suitable temperature for the heater is 150-350° C. Heating of the tall oil can be performed using various heat sources 31 available in a BtL plant such as steam, combustible gases or a portion of bottoms fraction 15 separated in the process.
  • FIG. 3 is shown another embodiment, also illustrated as alternative 14 b in FIG. 1 , wherein tall oil is processed further prior to feeding the distilled fractions to the BtL process.
  • the embodiment of FIG. 2 is based on the assumption that the catalyst used in the hydrocracking of BtL products is also suitable for processing tall oil distillates. However, this is a challenging demand with respect to the catalyst being used inasmuch as tall oil contains sulfur that acts as a catalyst poison. Furthermore, it is most undesirable to allow sulfur to pass to the end product.
  • the hydrocracking catalysts can be chosen separately for tall oil and biowax.
  • tall oil 18 is passed to distillation column 12 via a possible pretreatment step 26 .
  • the pretreatment step 26 means, e.g., esterification of the fatty/resin acids of tall oil with the help of an additive 25 , in the present case most advantageously with methanol.
  • Sulfur 30 is removed from the fraction separated in distillation column 12 , because it acts as a catalyst poison in the postprocessing unit 27 .
  • the distillate is condensed in step 21 and clarified in step 22 .
  • FIG. 3 is depicted as a horizontal dashed line the balance line of process flows between the BtL plant 32 and tall oil processing unit 33 so that the BtL plant 32 is to the left and tall oil processing unit 33 is to the right.
  • Combustible gases 17 can be utilized either in the refinery unit furnaces of the BtL plant or, alternatively, the sulfur-free process gases can be reformed to produce hydrogen.
  • the hydrogenated distillate 24 can be fed as a sidestream to the final distillation of the BtL product, while the bottoms distillate 15 is used in gasification or energy generation. If the tall oil-based biofuel is desired to be kept apart from the BtL biofuel, the distillate 24 may be later distilled into end products in a separate distillation plant.
  • the BtL plant 32 provides energy in the form of steam or gases for heating the distillation equipment 31 .
  • the invention provides significant benefits via the essential feature of the invention allowing the use of tall oil as feedstock in a BtL plant in the production a biofuel and facilitating efficient use of bottoms distillate in gasification, black liquor combustion or energy generation.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • General Chemical & Material Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Fats And Perfumes (AREA)
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US13/241,688 2010-11-16 2011-09-23 Method for utilizing distillation fractions obtained from distillation of tall oil in btl or cellulose factory Abandoned US20120117879A1 (en)

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FI20106204 2010-11-16
FI20106204A FI20106204L (fi) 2010-11-16 2010-11-16 Menetelmä mäntyöljyn tislauksesta saatavien tislejakeiden hyödyntämiseksi btl- tai sellutehtaassa

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EP (1) EP2452998A1 (ru)
CA (1) CA2752909A1 (ru)
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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20110097680A1 (en) * 2009-10-26 2011-04-28 Vapo Oy Method for heating the inlet air of a biomass dryer by means of an intermediate circuit and utilizing the circulating heating liquid of the dryer when the factory producing liquid biofuels is integrated with another factory

Citations (4)

* Cited by examiner, † Cited by third party
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