EP1080034A1 - Procede et appareil de production de gaz de synthese - Google Patents

Procede et appareil de production de gaz de synthese

Info

Publication number
EP1080034A1
EP1080034A1 EP99917245A EP99917245A EP1080034A1 EP 1080034 A1 EP1080034 A1 EP 1080034A1 EP 99917245 A EP99917245 A EP 99917245A EP 99917245 A EP99917245 A EP 99917245A EP 1080034 A1 EP1080034 A1 EP 1080034A1
Authority
EP
European Patent Office
Prior art keywords
gasifier
reformer
synthesis gas
biomass
outlet
Prior art date
Legal status (The legal status 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 status listed.)
Withdrawn
Application number
EP99917245A
Other languages
German (de)
English (en)
Inventor
Hubertus Johannes Veringa
Katrien Hemmes
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Energieonderzoek Centrum Nederland ECN
Original Assignee
Energieonderzoek Centrum Nederland ECN
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 Energieonderzoek Centrum Nederland ECN filed Critical Energieonderzoek Centrum Nederland ECN
Publication of EP1080034A1 publication Critical patent/EP1080034A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • 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
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/384—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts the catalyst being continuously externally heated
    • 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
    • C10K3/00—Modifying 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
    • C10K3/001—Modifying 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 thermal treatment
    • C10K3/003—Reducing the tar content
    • C10K3/006—Reducing the tar content by steam reforming
    • 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
    • C10K3/00—Modifying 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
    • C10K3/02—Modifying 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
    • C10K3/04—Modifying 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]
    • 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
    • C10K3/00—Modifying 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
    • C10K3/06—Modifying 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 mixing with gases
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
    • C01B2203/0822—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel the fuel containing hydrogen
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0838—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel
    • C01B2203/0844—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel the non-combustive exothermic reaction being another reforming reaction as defined in groups C01B2203/02 - C01B2203/0294
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0866—Methods of heating the process for making hydrogen or synthesis gas by combination of different heating methods
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/141—Feedstock
    • Y02P20/145—Feedstock the feedstock being materials of biological origin

Definitions

  • the invention relates to a method for forming synthesis gas from hydrocarbons, comprising: - feeding a first hydrocarbon and an oxidant to a gasifier and discharging synthesis gas from the gasifier,
  • German patent application DE-A-3, 242.206 discloses an apparatus in which coal in powdered form or a heavy oil fraction are partially oxidized in a gasifier, with the addition of oxygen, at a pressure of between 30 and 100 bar and a temperature of between 1000°C and 1400°C.
  • the hot synthesis gas formed in the process is passed over a water bath to remove soot and slags and is then passed through a tubular reactor in which catalytic steam reforming of LPG takes place at a pressure of between 10 and 40 bar and a temperature of between 750°C and 1000°C.
  • the synthesis gases formed in the gasifier and in the reformer are finally mixed in such a ratio that the desired H 2 /CO ratio is obtained.
  • the known apparatus is relatively complex and is not suitable for gasification of biomass and/or residues, whose partial oxidation does not, owing to the relatively high oxygen content naturally present, afford a suitable synthesis gas. Furthermore, when biomass and/or residues are used as a hydrocarbon source for the gasifier, the temperature achieved may be insufficiently high for driving the flow of heat to the reformer. Finally, the known apparatus, in which the reformer is completely integrated with the gasifier, is inflexible with respect to the operating point to be selected of mass streams fed in and the H /CO ratio of the synthesis gas formed.
  • the method according to the present invention is characterized in that the first hydrocarbon contains biomass and/or residues and in that part of the synthesis gas discharged from the gasifier is combusted, the heat liberated in the process being supplied to the reformer.
  • the avoided fossil CO 2 emission yield, 9co 2 of the process according to the present invention is likewise relatively high: 9co 2 - LHV(H 2 +CO) out /LHV (natural gas) ⁇ n .
  • the production of CO 2 per kg of H 2 + CO produced is small, and the avoided (fossil) CO 2 emission is therefore large.
  • the gasifier and the reformer according to the present invention are not integrated to a large degree, it is possible for the H 2 /CO ratio to be adjusted over a wide range.
  • a reliable process is obtained, since it is possible, in the event of the supply of biomass and/or residues being interrupted, for the 3 steam reformer to be operated separately, with the option of feeding the burner of the reformer with natural gas and gas from the gasifier.
  • the process according to the invention can take place using a relatively simple apparatus, the only measure required being to fit a branch line between the outlet of the gasifier and the reformer.
  • the gasifier delivers a synthesis gas which is rich in CO and relatively low in hydrogen
  • steam reforming gives precisely the opposite result
  • a combination of the two gas streams provides a mixed gas whose composition can be controlled by selecting the ratio between the input of fossil hydrocarbons and biomass. This allows the quality of the syngas of the biomass gasification to be increased and the H 2 /CO ratio of the mixed gas to be freely adjusted.
  • the hydrogen/carbon monoxide ratio of the mixed gas is between 0.7 and 5, preferably between 2 and 3. At these values, the mixed gas is suitable for a large number of downstream processes, such as admixture into the gas grid, secondary energy generation, generation of heat and/or power, and production of organic compounds as starting materials for the processing industry.
  • An apparatus in which the method according to the present invention can be implemented advantageously comprises, for example, a gasifier whose bed material is circulated, for the biomass and/or the residues, to which the steam reformer for the fossil hydrocarbon, preferably natural gas, is connected via a branch line.
  • a gasifier whose bed material is circulated, for the biomass and/or the residues, to which the steam reformer for the fossil hydrocarbon, preferably natural gas, is connected via a branch line.
  • Figure 1 shows a schematic depiction of the combined biomass/residues gasification and hydrocarbon reforming
  • Figure 2 shows a schematic depiction of the syngas composition according to the present invention
  • Figures 3 and 4 respectively, show the energy streams and mass streams of a syngas production process according to the present invention.
  • Figure 1 shows a gasifier 1 with a first inlet 2 for biomass and/or residues, and a second inlet 3 for an oxidant such as, for example, oxygen.
  • the apparatus also comprises a reformer 4 with a first inlet 5 for the supply of fossil hydrocarbons and a steam supply 6.
  • the outlet 8 of the gasifier 1 is connected to the reformer 4 by means of a branch line 7.
  • the outlet 8 of the gasifier is further connected to a purification apparatus 10 such as, for example, a scrubber to remove cyclic hydrocarbons and other contaminants such as H 2 S, HC1. alkali metals, tarry materials and dust from the syngas.
  • a purification apparatus 10 such as, for example, a scrubber to remove cyclic hydrocarbons and other contaminants such as H 2 S, HC1. alkali metals, tarry materials and dust from the syngas.
  • the outlet 9 of the 4 reformer 4 " can be connected to the outlet 12 of the purification apparatus 10 to form ' a mixed gas which can be fed to a CO 2 separator 13.
  • the outlet 14 of the CO 2 separator 13 is connected to a gas separation apparatus 15 for adjusting the composition of the product gas.
  • the gas coming from the gas separation apparatus 15 can be fed to the gas grid, can be used for production of energy, or can, for example, be used as process gas, where CO and H 2 can be reacted together catalytically to produce economically interesting hydrocarbons according to known and proven conversion technologies. It is also possible for the synthesis gas available from the outlet 9 of the reformer 4 to be fed, in its entirety or in part, to the gas grid via line 16.
  • the waste heat of the gases formed at the outlet of the gasifier 1 and the reformer 4 is returned, via heat exchangers 17 and 18, to the gasifier 1 and the reformer 4, respectively.
  • the process in the apparatus according to the present invention is determined by the following reactions: In the gasifier 1, the reaction taking place is: biomass + O 2 ⁇ CO + H 2 + C0 2 + H 2 O + C x H y .
  • the choice of gasification system provides the additional freedom to adjust the relative composition of the gas components.
  • hydrocarbons (C x H y ) may form part of the gas components.
  • the shift reaction CO + H 2 O ⁇ -> CO 2 + H 2 occurs. Since the gasifier 1 is operated autothermally, CO 2 and H 2 O are formed therein. If the oxidant used is ambient air, the synthesis gas at the outlet 8 of the gasifier may also comprise nitrogen. In the reformer 4, CO 2 is formed as a result of the shift reaction taking place to a significant degree. For a number of applications or downstream conversion routes of the process gas, the presence of minor components need not be a disadvantage. If the presence of minor components is not disadvantageous, a relatively coarse removal technique in, for example, purification apparatus 10 may be sufficient. To lower the nitrogen content in the product of the biomass gasifier 1 , it would be possible to use pure oxygen, rather than air, in the gasification.
  • the water can likewise be removed in a simple manner from the process gas.
  • the "gasifier 1 and the reformer 4 are operated at temperatures of between 750° ' C and 1000°C, for example about 800°C-900°C.
  • the gasifier 1 can, for example, be formed by a gasifier having an external burner, such as is manufactured by Manufacturing Technology Conversion International, with a temperature of 850°C and a pressure of 1 bar.
  • the reformer 4 comprises a steam reformer known per se having a burner which, for example, is operated at a pressure of 1 bar and a temperature of 1200°C, the pressure in the reformer 4 being 1 bar and the temperature being 815°C.
  • the burner of the reformer is fed with synthesis gas coming from the gasifier.
  • Figure 2 in the form of a graph, shows how varying the ratio of the quantity of methane fed to the reformer 4 via the inlet 5 and the quantity of biomass fed to the gasifier 1 via the inlet 2 allows the composition of the mixed gas formed after combining the synthesis gases from outlets 9 and 12 to be varied.
  • the gasifier 1 delivers a synthesis gas which mainly comprises CO
  • the steam reformer 4 comprises synthesis gas mainly containing H 2
  • the H 2 /CO ratio can be adjusted by selecting the ratio between the input of natural gas and of biomass.
  • the H 2 /CO ratio is around 2-3 mol/mol. This ratio is particularly beneficial for forming organic compounds, including liquid hydrocarbons.
  • Figures 3 and 4 respectively show the energy and mass streams of the process according to the present invention for an H /CO ratio of 3.16.
  • the figures in brackets give percentages for an energy or mass yield of the synthesis gas formed in total.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Industrial Gases (AREA)

Abstract

L'invention concerne un procédé et un appareil permettant de former du gaz de synthèse à partir de la biomasse et/ou de résidus. Dans un gazéifieur à biomasse et/ou à résidus est formé du gaz de synthèse dont une partie est brûlée, la chaleur de combustion étant transférée à un reformeur. Dans le reformeur, un hydrocarbure fossile est converti en gaz de synthèse qui est mélangé avec le gaz de synthèse formé dans le gazéifieur. Le procédé et l'appareil selon l'invention permettent d'obtenir un rendement élevé en gaz froid, la production de CO2 par kilogramme de gaz de synthèse (H2 et CO) produit étant basse. Grâce au bas niveau d'intégration du gazéifieur et du reformeur, le rapport H2/CO peut être ajusté sur une large plage. L'appareil selon l'invention est relativement simple et fiable, étant donné que la seule liaison entre le reformeur et la sortie du gazéifieur se fait par l'intermédiaire d'une ligne de branchement. Le couplage du gazéificateur et du reformeur selon l'invention permet le passage graduel de l'utilisation du combustible fossile à une source d'hydrocarbure plus facile à renouveler. En outre, la qualité du gaz de synthèse formée dans le gazéifieur à biomasse peut être améliorée par mélange avec le gaz de synthèse provenant du reformeur, et la régulation des courants d'alimentation permet l'obtention d'une composition de gaz de synthèse variable (rapport H2/CO).
EP99917245A 1998-04-29 1999-04-29 Procede et appareil de production de gaz de synthese Withdrawn EP1080034A1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
NL1009038 1998-04-29
NL1009038A NL1009038C2 (nl) 1998-04-29 1998-04-29 Werkwijze en inrichting voor het vormen van synthesegas.
PCT/NL1999/000256 WO1999055618A1 (fr) 1998-04-29 1999-04-29 Procede et appareil de production de gaz de synthese

Publications (1)

Publication Number Publication Date
EP1080034A1 true EP1080034A1 (fr) 2001-03-07

Family

ID=19767054

Family Applications (1)

Application Number Title Priority Date Filing Date
EP99917245A Withdrawn EP1080034A1 (fr) 1998-04-29 1999-04-29 Procede et appareil de production de gaz de synthese

Country Status (6)

Country Link
EP (1) EP1080034A1 (fr)
JP (1) JP2002512933A (fr)
AU (1) AU3540499A (fr)
CA (1) CA2330302A1 (fr)
NL (1) NL1009038C2 (fr)
WO (1) WO1999055618A1 (fr)

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BR0104703A (pt) 2000-02-29 2002-02-05 Mitsubishi Heavy Ind Ltd Sistema de sìntese se metanol fazendo uso de biomassa
US6448441B1 (en) * 2001-05-07 2002-09-10 Texaco, Inc. Gasification process for ammonia/urea production
GB2409460B (en) * 2002-06-25 2005-12-14 Chevron Usa Inc Process for conversion of LPG and CH4 to syngas and higher valued products
US6774148B2 (en) 2002-06-25 2004-08-10 Chevron U.S.A. Inc. Process for conversion of LPG and CH4 to syngas and higher valued products
CA2496839A1 (fr) * 2004-07-19 2006-01-19 Woodland Chemical Systems Inc. Methode de production d'ethanol a partir de gaz de synthese a teneur elevee en monoxyde de carbone
EP1877520B8 (fr) * 2005-01-18 2013-11-13 Elementa Group, Inc. Procede de reformage a la vapeur du'n materiau carbone
US20070011945A1 (en) * 2005-07-05 2007-01-18 Gerard Grootveld Systems and methods for producing synthesis gas
CA2615576A1 (fr) * 2005-07-20 2007-01-25 Shell Internationale Research Maatschappij B.V. Preparation d'un gaz de synthese
FR2904830B1 (fr) 2006-08-08 2012-10-19 Inst Francais Du Petrole Procede de production de gaz de synthese avec oxydation partielle et vaporeformage
FR2904831B1 (fr) * 2006-08-08 2012-09-21 Inst Francais Du Petrole Procede et installation de traitement de petrole brut avec conversion de residu asphaltenique
DE102006050057A1 (de) * 2006-10-24 2008-04-30 Linde Ag Steuerungsverfahren bei der Synthesegaserzeugung
US7837973B2 (en) 2007-05-08 2010-11-23 Air Products And Chemicals, Inc. Hydrogen production method
US8592492B2 (en) * 2010-03-08 2013-11-26 Praxair Technology, Inc. Using fossil fuels to increase biomass-based fuel benefits
US9169443B2 (en) * 2011-04-20 2015-10-27 Expander Energy Inc. Process for heavy oil and bitumen upgrading
AU2012350757B2 (en) * 2011-12-13 2015-03-26 Shell Internationale Research Maatschappij B.V. Fischer-Tropsch process
CN102807848B (zh) * 2012-07-19 2014-08-06 中国海洋石油总公司 一种煤制油深水恒流变合成基钻井液
US9290422B2 (en) 2012-11-27 2016-03-22 Praxair Technology, Inc. Hybrid plant for liquid fuel production
US9145525B2 (en) * 2013-06-26 2015-09-29 Praxair Technology, Inc. Acid gas management in liquid fuel production process
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EP3891096A4 (fr) 2018-12-06 2022-10-12 Raven Sr, Inc. Production d'hydrogène et de produits ft par vaporeformage/reformage au co2
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Also Published As

Publication number Publication date
NL1009038C2 (nl) 1999-11-01
JP2002512933A (ja) 2002-05-08
CA2330302A1 (fr) 1999-11-04
WO1999055618A1 (fr) 1999-11-04
AU3540499A (en) 1999-11-16

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