WO2014087048A1 - Procédé pour la réduction de l'empreinte carbone de combustible produit dans une installation de transformation de biomasse en liquide (btl) - Google Patents

Procédé pour la réduction de l'empreinte carbone de combustible produit dans une installation de transformation de biomasse en liquide (btl) Download PDF

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Publication number
WO2014087048A1
WO2014087048A1 PCT/FI2013/051122 FI2013051122W WO2014087048A1 WO 2014087048 A1 WO2014087048 A1 WO 2014087048A1 FI 2013051122 W FI2013051122 W FI 2013051122W WO 2014087048 A1 WO2014087048 A1 WO 2014087048A1
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WO
WIPO (PCT)
Prior art keywords
carbon dioxide
btl
plant
ccs
syngas
Prior art date
Application number
PCT/FI2013/051122
Other languages
English (en)
Inventor
Jorma Kautto
Mika Timonen
Original Assignee
Vapo Oy
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 Vapo Oy filed Critical Vapo Oy
Publication of WO2014087048A1 publication Critical patent/WO2014087048A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/002—Removal of contaminants
    • C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
    • C10K1/005—Carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/002—Removal of contaminants
    • 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
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/02—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
    • C10L1/026—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only for compression ignition
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/26—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds
    • C22B3/30—Oximes
    • 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
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • 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
    • Y02E50/10—Biofuels, e.g. bio-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
    • 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
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/10—Reduction of greenhouse gas [GHG] emissions
    • Y02P10/146—Perfluorocarbons [PFC]; Hydrofluorocarbons [HFC]; Sulfur hexafluoride [SF6]

Definitions

  • the invention relates to a method in accordance with the preamble of claim 1 for improving the reduction of carbon footprint of fuel produced in a BtL plant.
  • the invention also relates to a use in accordance with claim 11 and an apparatus in accordance with claim 1 utilizing the method.
  • biomass is gasified in a high- temperature or a low-temperature gasifier.
  • the function of a BtL plant is to convert biomass into liquid fuels (Biomass to Liquid) from syngas generally through Fischer-Tropsch synthesis.
  • the gasifier operates at a temperature higher than the ash melt temperature, more specifically at about 1200 - 1400 °C. Depending on the technology used, gasification takes place at a pressure of 1 - 40 bar.
  • syngas The synthetic gas generated in gasification and further subjected to purification is generally called syngas, when it is subsequently used in preparation of other products such as ammonia or long-chain aromatic hydrocarbons.
  • the raw syngas generated in gasification must be cooled and purified free from dust, and other components except hydrogen and carbon monoxide need be separated from the gas stream.
  • the resulting pure syngas i.e., hydrogen and carbon monoxide is passed to a Fischer-Tropsch reactor (FT reactor), wherein paraffinic hydrocarbons are generated in the presence of a catalyst.
  • FT reactor Fischer-Tropsch reactor
  • the FT process is typically carried out at a pressure of 20 - 40 bar and at a temperature of about 200 °C.
  • the wax-like product thus obtained is known as biowax.
  • the biowax taken out from the FT process requires further refining in order to produce therefrom fuels suited for engine use by way of, i.a., hydrogenation, cracking and distillation.
  • Hydrogenation refers to processing in a hydrogen atmosphere, wherein double bonds between carbons are saturated. Cracking in turn refers to breaking excessively long hydrocarbon chains in a reactor. Distillation finally separates the fuel fractions from each other thus resulting in diesel fuel, naphtha, kerosene, liquefied petroleum gas, etc.
  • the raw syngas is washed with methanol wherein carbon dioxide is dissolved. Actually no chemical reaction is involved, but instead the cold methanol acts as a physical absorbent.
  • the dissolved carbon dioxide is separated in a multi-step process from the methanol that is recycled to the gas purification step. While the functional details of the purification method are not essential in the present invention, the separation efficiency must be high enough to produce carbon dioxide with a degree of purity greater than 95 mole percent.
  • Carbon dioxide is a greenhouse gas that absorbs thermal radiation emitted from the earth to the sky and resultingly leads to global warming. Global warming in turn causes local draught, heavy rainfall, tropical storms, melting of glaciers and other undesirable meteorological effects, whereupon international agreements have been made to limit carbon dioxide emissions in order to slow down global warming. Carbon dioxide emissions can be reduced by way of improving, e.g., the energy efficiency of production processes and transportation, as well as using renewable energy sources and cutting down energy consumption. In order to reach international emission objectives, it is also necessary to apply carbon dioxide capture and sequestration methods commonly referred to by abbreviation CCS (Carbon Capture and Storage).
  • CCS Carbon Capture and Storage
  • a CCS process covers the capture of carbon dioxide from the flue gases of a combustion plant and final sequestration thereof from the atmosphere.
  • CCS techniques are in a vigorous phase of development with good expectations to be adopted in the 2020's.
  • the crucial technological challenges posed herein are focused on the capture of carbon dioxide from flue gases, transport to long-term storage site and safe final sequestration.
  • the CCS techniques can be optimally employed in processes involving high carbon dioxide emissions and releasing carbon dioxide incessantly. These kinds of processes include, i.a., large fossil-fuel power plants, steel factories, chemical plants, oil refineries and paper/pulp mills.
  • a BtL process includes a carbon dioxide capture process that is the first step in a CCS process. It is further known from literature that in principle a CCS process can be combined with a BtL process thus allowing improvements in the carbon footprint of the product. However, a problem herein has been that the theoretical solutions disclosed in literature to this end have not been practicable in industrial scale.
  • the salient feature of the arrangement according to the present invention makes it possible to develop a practicable method allowing an economically viable way of capturing carbon dioxide that may be utilized and subjected to further processing in the industry.
  • Carbon dioxide captured in syngas purification can find many uses inasmuch it can be utilized industrially, e.g., in beverage carbonation, as fire extinction gas, as protective gas in the metal processing industry, in greenhouses to elevate the carbon dioxide concentration of the greenhouse thus enhancing the growth of plants and in like usage.
  • the carbon footprint of the BtL plant end product may as well be +20 gco 2 / J or -100 gco 2 /MJ, however currently valid regulations dictate equal amounts thereof to be mixed with diesel fuel since their biogenic carbon origins are today considered equal. Hence, presently it is most advantageous, unfortunately, to release carbon dioxide to the atmosphere in the interest of the profitability and economics of an industrial plant.
  • the carbon dioxide released by a BtL plant has a biogenic origin which means that it stems from vegetation-based carbon, typically from wood for instance. If a BtL plant is designed so as to use fossil fuels minimally, e.g., when starting the plant process or producing hydrogen, the carbon footprint of the electricity used by the plant is low and the emissions from the feedstock harvesting chain are minimal, also the carbon footprint of fuels produced by the plant remains realty low. While the computational carbon footprint of a fossil fuel is 86 gco 2 /MJ, the typical carbon footprint of a fuel produced in a BtL plant is typically in the order of 10 - 20 gco 2 /MJ.
  • carbon dioxide must be transported to its final storage location either via a dedicated pipeline or, e.g., liquefied for shipping, whereby its volume is reduced by a factor of about one thousand.
  • liquefied carbon dioxide is handled at a temperature of about -50 °C and a pressure of 7 bar.
  • Pipeline transfer of gaseous carbon dioxide becomes profitable when the amounts of carbon dioxide to be moved are large, typically in the order of 0 million tons per year and the transfer distances are in appropriate proportion to the gas volume to be moved. Economic transport of small C0 2 volumes is possible when the distances are shorter than 500 km. Transport of large amounts in the order of 10 Mt/yr is even feasible over greater distances. In all cases the technical challenges and other practical aspects of pipeline construction must be taken into account not forgetting that gaseous carbon dioxide is odorless and even hazardous when inhaled in large quantities.
  • Carbon dioxide must first be pressurized using com- pressors and subsequently cooled to a temperature of -50 °C to liquefy the carbon dioxide. Such a cooling process also needs compression of the refrigerant.
  • Intermediate storage of carbon dioxide is required, e.g., for transport in ships.
  • the required volume of the intermediate storage is dictated by the plant's production capacity and size of transportation vehicle that in turn is chosen to suit the transportation distance and available waterway depth.
  • gas in the intermediate storage must be kept in liquefied form.
  • Suitable final sequestration sites in Europe can be found at the North Sea, for instance. Preliminary plans have even been drafted to lay carbon dioxide transportation pipelines from Continental European countries, e.g., Germany, Scandinavian countries particularly from Norway, as well as from Great Britain to the final sequestration sites on the North Sea. For longer transportation distances also carbon dioxide tankers are being developed with a cargo capacity of 10,000 - 100,000 tons.
  • a CCS process may basically be adapted to function as a separate unit along with a BtL process, whereby improvements could be achieved in the carbon footprint of the end product.
  • the present invention provides a solution for integrating both processes to function as single entity in a BtL plant.
  • the process is capable of liquefying 570,000 tons carbon dioxide per annum, while the biofuel yield is 100,000 tons per annum with a heat value of 44 MJ/kg.
  • the C0 2 footprint of biodiesel produced in a BtL plant without a CCS process is 10 - 20 gco2 MJ. If a CCS process is included, the end product carbon footprint can be made substantially negative down to -70, even as low as -90 gco2 J.
  • a product thus produced with a fossil-origin diesel fuel in a ratio of 50/50 for instance, an almost carbon emissions neutral fuel with regard to atmospheric pollution is obtained.
  • a BtL plant provides a process for capturing carbon dioxide from syngas without any additional investments in the capture process proper.
  • An essential feature of the present invention for carbon dioxide capture comprises integration of a CCS process with a BtL process proper into a single entity.
  • the integration concept draws upon the inherent characteristics of a BtL plant including use and recycling of C0 2 in the BtL process in both compressing and shipping of the gas.
  • biofuels are considered carbon neutral meaning that carbon dioxide released to the atmosphere from a biofuel is returned to vegetation via photosynthesis.
  • carbon dioxide is removed from such a cycle, it is respectively also removed from the atmosphere, whereby the balance sheet of a fuel produced or derived through the process is considered to result in a negative carbon footprint.
  • An essential feature of the invention is that the entire carbon dioxide capture process may presently be implemented with improved efficiency as an integral part of a BtL plant thus bringing up integration benefits that also enhance the process and energy efficiency of a CCS process.
  • the characterizing properties of the invention are crucial in the implementation of the method and use thereof. More specifically, the invention is characterized by what is stated in the claims.
  • Fig. 1 shows Table 1 on the composition of carbon dioxide in the method according to the invention
  • Fig. 2 shows a process flow schematic for implementing the method according to the invention.
  • the syngas may have the exemplifying composition listed in the table thereof.
  • the CO 2 gas flows emerging therefrom may be one or several with a varying composition, pressure and temperature.
  • the amount of mass flow is related to the size of the BtL plant typically being in the order of 0.3 - 1.0 tco 2 y corresponding to about 40,000 - 130,000 kg C 02 .
  • the carbon dioxide flows listed in Table 1 are combined.
  • Carbon dioxide is pressurized with the help of a compressor to a pressure of about 20 bar.
  • the compressed gas must be dehumidified because otherwise the water freezing during liquefaction starts to condense in the process equipment.
  • the flow is cooled in heat exchangers down to -35°C for which task the equipment comprises a refrigerator machinery. Since the temperature level is the same as that used in the prior-art Rectisol processTM, the two machineries may be combined.
  • the flow pressure drops to 7 bar, whereby also its temperature falls down to about -50°C thus causing liquefaction of the CO2 flow.
  • the fraction remaining gaseous in liquefaction is recycled to the BtL plant.
  • the nonliquid flow comprises mainly hydrogen, carbon monoxide, methane, nitrogen and argon.
  • the flow may be utilized at the BtL plant to increase the end product yield, e.g., by way of passing the flow to a gasifier or using it as fuel in a steam reformer.
  • the liquefied C0 2 is stored in a thermally insulated tank for later post- processing or transportation, most advantageously by shipping to a final sequestration site. During storage, a portion of the liquefied carbon dioxide evaporates and is recycled to the carbon dioxide liquefaction step.
  • Fig. 2 illustrating the entire process wherein the BtL process 41 proper is shown as a simplified diagram, since the details thereof are irrelevant to the function of the invention.
  • the biomass 1 is first fed to a preprocessing step 2, wherein the moist wood-based feedstock is dried and homogenized into a suitable particle size. Drying can be carried out with the help of hot water flows 40 receiving a portion of their warmth from the cooling circulations of CCS process refrigeration machineries 14 and 17 as well as the cooling of compressors 10.
  • the dried biomass is gasified 3, whereupon the raw syngas is cooled and washed 4.
  • the gas pressure is elevated with the help of a compressor unit 5 to a level of about 40 - 80 bar required in the subsequent process steps.
  • the separated carbon dioxide 18 is taken for intermediate storage to a gas tank, wherefrom a portion of carbon dioxide 8 is passed 44 for use in gasi- fication 3 in the production and inert gas circulation of gasifier gas.
  • Surplus portion 42 is compressed to an elevated pressure of about 20 bar with the help of compressor 10, whereupon the pressurized carbon dioxide 9 is taken to water separation 1 1 , that is, to dehumidification.
  • water separation 1 1 that is, to dehumidification.
  • a portion of the moisture carried along with the gas is separated as waste/condensate water 28.
  • Dehumidification is most optimally carried out with the help of intermediate-pressure steam 29 taken out from FT synthesis step 7.
  • Condensate 39 is returned to the condensate water system of the BtL plant.
  • cooling unit 17 performs cooling of carbon dioxide flow with help of cooling water 30 running a closed circulation loop and thus is returned at an elevated temperature 38 to the cooling unit 17. Therein the water performs separation of waste/condensate water 28 from the
  • the dehumidified and pressurized carbon dioxide 20 is taken to liquefaction 12, wherein the gas flow is cooled with the help of refrigerant 34 circulating in the common refrigeration machinery 14 of the gas purification process 6, whereupon the carbon dioxide is allowed to expand to the storage pressure of about 7 bar. During its expansion, the gas flow also cools down to its liquefaction temperature thus assuming a liquid state as liquid carbon dioxide 21 that can be stored in a tank 13, for instance.
  • the refrigeration machinery is most advantageously operated commonly with the syn gas purification process 6, whereby it provides a flow of refrigerant 35 for cooling the syn gas and methanol into absorption state and further receives the warmed refrigerant 36 as well as the refrigerant flow 33 coming from the liquefaction step.
  • the carbon dioxide is pumped along pipeline 22 to further processing or transportation, most advantageously in a tank carrier 16.
  • C02-gases expanded during loading of the ship are received along pipeline 23 at the liquefaction unit for re-liquefaction.
  • the tank carrier takes the carbon dioxide to a final sequestration site. While the actual operations of shipping as well as the further processing or final storage of the carbon dioxide are not covered by scope of the present, it is plausible that commercial service providers can be found to carry out these steps.
  • the entire volume of the gas flow 20 does not liquefy inasmuch as it also is cleaned free from impurities in the form of flash-off gases 25 including, i.a., hydrogen, carbon monoxide, methane, nitrogen and argon. These components are taken a flash-off gas treatment unit 15.
  • the recovered nonliquefying components 26 are chiefly combustible gases that can be utilized in the BtL process 41 for the purpose of increasing the end product yield, e.g., in hydrogen reforming or as feedstock or fuel of the reformer unit.
  • Operating heat of carbon dioxide dehumidification unit needs steam 29 that is available from the BtL plant 41 , e.g., from the cooling circulation 7 of the FT reactor or from the intermediate exhaust output of turbine 5 of the syngas turbocompressor.
  • Condensate/waste waters 27 and 28, as well as 39, formed in the CCS process may be safely handled in the condensate water system and wastewater plant of the BtL plant.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Geology (AREA)
  • Materials Engineering (AREA)
  • Mechanical Engineering (AREA)
  • Metallurgy (AREA)
  • Manufacturing & Machinery (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Treating Waste Gases (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

L'invention porte sur l'amélioration de la réduction de l'empreinte carbone d'un combustible produit dans une installation de transformation de biomasse en liquide (BtL) (41). La caractéristique essentielle de l'invention est que l'appareil destiné à la purification de gaz de synthèse produit dans une installation BtL est employé dans la séparation de dioxyde de carbone et sa récupération pour traitement supplémentaire et/ou stockage final.
PCT/FI2013/051122 2012-12-04 2013-12-02 Procédé pour la réduction de l'empreinte carbone de combustible produit dans une installation de transformation de biomasse en liquide (btl) WO2014087048A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FI20126265 2012-12-04
FI20126265A FI20126265L (fi) 2012-12-04 2012-12-04 Menetelmä BtL-laitoksessa valmistettavan polttoaineen hiilijalanjäljen tehostamiseksi

Publications (1)

Publication Number Publication Date
WO2014087048A1 true WO2014087048A1 (fr) 2014-06-12

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PCT/FI2013/051122 WO2014087048A1 (fr) 2012-12-04 2013-12-02 Procédé pour la réduction de l'empreinte carbone de combustible produit dans une installation de transformation de biomasse en liquide (btl)

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FI (1) FI20126265L (fr)
WO (1) WO2014087048A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2572409A (en) * 2018-03-29 2019-10-02 Hurudza Munyaradzi Mkushi George Methods and systems of upgrading syngas via CO² recovery

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2009065352A1 (fr) * 2007-11-16 2009-05-28 Accelergy Shanghai R & D Center Co., Ltd. Procédé intégré de conversion de charbon en liquides
US20120032452A1 (en) * 2010-08-09 2012-02-09 Kuku Lai O Waste Material, Coal, Used Tires and Biomass Conversion to Alternative Energy and Synthetic Fuels Solutions System with Carbon Capture and Liquefaction
WO2012095556A1 (fr) * 2011-01-14 2012-07-19 Vapo Oy Procédé d'utilisation de l'énergie thermique des gaz en produit dans une usine appartenant à la filière btl
EP2484427A2 (fr) * 2011-02-08 2012-08-08 Neste Oil Oyj Procédé de lavage de gaz à deux étages

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2009065352A1 (fr) * 2007-11-16 2009-05-28 Accelergy Shanghai R & D Center Co., Ltd. Procédé intégré de conversion de charbon en liquides
US20120032452A1 (en) * 2010-08-09 2012-02-09 Kuku Lai O Waste Material, Coal, Used Tires and Biomass Conversion to Alternative Energy and Synthetic Fuels Solutions System with Carbon Capture and Liquefaction
WO2012095556A1 (fr) * 2011-01-14 2012-07-19 Vapo Oy Procédé d'utilisation de l'énergie thermique des gaz en produit dans une usine appartenant à la filière btl
EP2484427A2 (fr) * 2011-02-08 2012-08-08 Neste Oil Oyj Procédé de lavage de gaz à deux étages

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
VAN VLIET, O.P.R ET AL.: "Fischer-Tropsch diesel production in a well-to-wheel perspective: A carbon, energy flow and cost analysis", ENERGY CONVERSION AND MANAGEMENT, vol. 50, no. 4, 2009, pages 855 - 876 *

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2572409A (en) * 2018-03-29 2019-10-02 Hurudza Munyaradzi Mkushi George Methods and systems of upgrading syngas via CO² recovery

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