EP2188210A2 - Procédé et installation pour la production d'un gaz de synthèse à partir de biogaz - Google Patents

Procédé et installation pour la production d'un gaz de synthèse à partir de biogaz

Info

Publication number
EP2188210A2
EP2188210A2 EP08785493A EP08785493A EP2188210A2 EP 2188210 A2 EP2188210 A2 EP 2188210A2 EP 08785493 A EP08785493 A EP 08785493A EP 08785493 A EP08785493 A EP 08785493A EP 2188210 A2 EP2188210 A2 EP 2188210A2
Authority
EP
European Patent Office
Prior art keywords
biogas
oxygen
synthesis gas
plant
gas
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Withdrawn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
EP08785493A
Other languages
German (de)
English (en)
Inventor
Lothar Günther
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.)
DGE Dr Ing Guenther Engineering GmbH
Original Assignee
DGE Dr Ing Guenther Engineering GmbH
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 DGE Dr Ing Guenther Engineering GmbH filed Critical DGE Dr Ing Guenther Engineering GmbH
Publication of EP2188210A2 publication Critical patent/EP2188210A2/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1462—Removing mixtures of hydrogen sulfide and carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/52—Hydrogen sulfide
    • B01D53/526—Mixtures of hydrogen sulfide and carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/84—Biological processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/96—Regeneration, reactivation or recycling of reactants
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
    • C01B13/02—Preparation of oxygen
    • C01B13/0229—Purification or separation processes
    • C01B13/0248—Physical processing only
    • C01B13/0259—Physical processing only by adsorption on solids
    • 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
    • C01B3/36—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 oxygen or mixtures containing oxygen as 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
    • C01B3/382—Multi-step processes
    • 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
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/52—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquids; Regeneration of used liquids
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M21/00—Bioreactors or fermenters specially adapted for specific uses
    • C12M21/04—Bioreactors or fermenters specially adapted for specific uses for producing gas, e.g. biogas
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
    • C12M47/14—Drying
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
    • C12M47/18—Gas cleaning, e.g. scrubbers; Separation of different gases
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P5/00—Preparation of hydrocarbons or halogenated hydrocarbons
    • C12P5/02—Preparation of hydrocarbons or halogenated hydrocarbons acyclic
    • C12P5/023—Methane
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/10—Oxidants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/112—Metals or metal compounds not provided for in B01D2253/104 or B01D2253/106
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/304—Hydrogen sulfide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/05—Biogas
    • 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
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
    • 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
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
    • 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0415—Purification by absorption in liquids
    • 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/042—Purification by adsorption on solids
    • C01B2203/043—Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
    • 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
    • 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
    • C01B2203/0872—Methods of cooling
    • 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
    • C01B2203/0872—Methods of cooling
    • C01B2203/0888—Methods of cooling by evaporation of a fluid
    • C01B2203/0894—Generation of steam
    • 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
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1258—Pre-treatment of the feed
    • 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
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1258—Pre-treatment of the feed
    • C01B2203/1264—Catalytic pre-treatment of the feed
    • C01B2203/127—Catalytic desulfurisation
    • 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
    • C01B2203/14—Details of the flowsheet
    • C01B2203/142—At least two reforming, decomposition or partial oxidation steps in series
    • 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
    • C01B2203/16—Controlling the process
    • C01B2203/1604—Starting up the process
    • 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
    • C01B2203/80—Aspect of integrated processes for the production of hydrogen or synthesis gas not covered by groups C01B2203/02 - C01B2203/1695
    • C01B2203/84—Energy production
    • 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
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
    • 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
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—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
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
    • 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
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/59—Biological synthesis; Biological purification

Definitions

  • the invention relates to a process for the production of synthesis gas from biogas and a plant suitable for carrying out the process.
  • Synthesis gas can be catalytically converted into higher hydrocarbons, in particular liquid fuels for internal combustion engines, by a conventional procedure.
  • Biogas is produced by anaerobic (oxygen-free) fermentation of organic material and is used as a renewable energy source.
  • biomass-containing raw materials manure, such as manure and manure, renewable raw materials, a distinction is made in sewage gas, landfill gas and biogas.
  • Biogas is to be understood below to mean all gases produced by fermentation.
  • the aforementioned gases also contain carbon dioxide and hydrogen sulfide as well as small residual amounts of other chemicals.
  • a method for the liquefaction of biogas in which the biogas components methane, carbon dioxide and water without separation, optionally with the addition of water, via a catalyst endothermic to synthesis gas with a carbon monoxide / hydrogen ratio between 1 : 1 to 1: 3 to be implemented.
  • the synthesis gas is then converted by catalytic hydrogenation into liquid hydrocarbons.
  • DE 198 27 154 C2 a method and an apparatus for the production of methanol from biogas are described, wherein biogas is thermally catalytically heat neutral in a reformer in the presence of a circulation catalyst without addition of steam added in synthesis gas.
  • the biogas is catalytically converted under increased pressure and elevated temperature in a two-stage reforming process to synthesis gas and separated from this by a physical wash CO 2 .
  • the scrubbing solution is released and releases the desorbed components of CO 2 and H 2 S at the outlet, which are burned together with air and released into the environment.
  • the pure synthesis gas is then catalytically converted to methanol.
  • the circulation catalyst is regenerated in a downstream combustion stage by oxidation of the carbon deposited in the reformer.
  • the invention has for its object to provide a process for the production of synthesis gas from biogas, which is characterized by a more economical process control and higher yield. Furthermore, a suitable for carrying out the process plant to be created.
  • Hydrogen sulfide is removed biologically by the addition of oxygen and / or oxygen-containing oxidant.
  • oxygen or oxidant are metered so that in the purified biogas (methane gas) an excess of oxygen of at least 1, 0 VoI.-% is included.
  • the purified biogas does not have to be dehumidified. It is subsequently compressed, heated and mixed with superheated steam. During the reforming process, heat energy is thus additionally generated by an exothermic oxidation of oxygen contained in the biogas with hydrogen as a quick initial ignition for the start of the reaction in the catalyst bed, for the endothermic conversion of methane to synthesis gas. This is of great economic advantage, since the reforming process is thus initiated by a self-raising temperature of the biogas and, therefore, no external energy is required and the catalyst volume can be reduced.
  • the hydrogen sulfide contained in the biogas can already be separated in the fermenter, by means of additives, such as. Iron salts, or by adding pure oxygen or oxygen-containing oxidant.
  • additives such as. Iron salts, or by adding pure oxygen or oxygen-containing oxidant.
  • the removal of hydrogen sulfide can also be done only in a downstream biological desulfurization, in which case, however, the total amount of oxygen required must be supplied including for the required oxygen excess.
  • the oxygen-containing oxidant z. As H 2 O 2 or NaOCI be used.
  • the desulphurisation of biogas is a complicated process, because different reactions are superimposed:
  • the total amount of oxygen to be supplied should be at least 8.5 moles O 2 / mole H 2 S to ensure the required oxygen excess.
  • the purified biogas contains at least 0.05% by volume of hydrogen.
  • the oxygen excess in the purified biogas should be measured continuously or at specific time intervals, as a controlled variable for the supply of water and external heat energy for the reforming process.
  • the biogas contained CO 2 and small residual amounts of hydrogen sulfide are separated by means of physical or chemical washing with an amine-containing washing solution.
  • the hydrogen sulfide content can thus be reduced to a few hundredths of ppm.
  • the purified biogas is added after compression superheated steam, which is formed from accumulating in the heat recovery stages condensate.
  • all components of organic sulfur should be completely removed prior to introduction into the reformer to avoid damage to the catalyst.
  • the reforming process is preferably carried out in two stages. First, the purified biogas (methane gas) is compressed to a pressure of 10 to 50 bar, heated to a temperature of about 600 to 800 0 C and then added to the required residual amount of oxygen and / or water or saturated steam.
  • a first reforming step at reaction temperatures of 800 to 900 ° C, the reaction to about at least 90 vol .-% to synthesis gas, wherein a portion of the required heat energy is generated by reaction of the excess oxygen contained in the methane gas.
  • the subsequent second reforming carried out under oxygen at reaction temperatures of about 1000 ° C, the further reaction up to about 99.5 vol .-% synthesis gas.
  • the oxygen gas to be supplied is heated in a heat exchanger and added to the synthesis gas immediately before it enters the secondary reformer.
  • the provision of oxygen-containing gas can be carried out by means of a pressure swing adsorption plant.
  • the thermal energy required for the high reaction temperatures during the reforming stages can be provided to a large extent without external energy.
  • the synthesis gas generated in the second reform ingme used for indirect heating of methane gas.
  • the fermentation substrate produced in the biogas plant is used as fuel to generate heat of reaction for the first reforming stage.
  • This allows a particularly economical conversion of biogas into synthesis gas.
  • fermentation substrate can be used as a fuel for incinerators certain garbage, such as household waste.
  • carbon dioxide is finally separated off in a scrubbing column by means of an amine-containing scrubbing solution.
  • the CO 2 -free synthesis gas can subsequently be used in a manner known per se for the synthesis of liquid fuels, methanol, ammonia or separation into hydrogen and carbon monoxide.
  • the respective detergent solutions from the biogas and synthesis gas scrubbing are preferably fed to a common detergent regeneration.
  • the purified detergent is circulated.
  • a plant suitable for carrying out the process consists of a biogas plant with at least one fermenter, a plant for the treatment and drying of fermentation substrate in the biogas plant, a biogas plant downstream biological desulfurization and downstream of this first scrubbing column for the removal of carbon dioxide, a compressor for compressing the Methane gas at synthesis gas pressure, a first heat exchanger for heating the compressed methane gas to temperatures above 500 0 C, a reformer unit for the catalytic conversion of methane gas in synthesis gas, at least one unit for heat recovery from synthesis gas and / or flue gas, a second wash column for the separation of carbon dioxide Synthesis gas and a supply for oxygen or oxidizing agent.
  • the reformer unit preferably consists of a primary reformer and a downstream secondary reformer.
  • the supply of oxygen or oxidant is connected via a first line to a second heat exchanger for heating oxygen-containing gas to synthesis gas temperature, which is incorporated in the line for supplying synthesis gas in the secondary reformer.
  • the secondary reformer is connected to an outlet line, which runs as a heat carrier coil through a heat exchanger, which is connected upstream of the primary reformer and intended for heating the methane gas.
  • the synthesis gas leading line is connected after the first heat exchanger via a line with another (third) heat exchanger for generating steam. This heat exchanger is connected via a further line with a fourth heat exchanger for generating hot water.
  • synthesis gas line is connected to a fifth heat exchanger for generating hot water or steam in combination. Via another line, the synthesis gas passes into the second wash column.
  • the fourth heat exchanger is a hot water leading and Return line integrated with the Biosgasstrom and the fermentation substrate treatment plant connected, for the provision of hot water for heating purposes.
  • the primary reformer is connected to a flue gas-carrying line which communicates with a heat exchanger unit which is designed as a steam superheater.
  • the system is equipped with a steam drum, which is connected to the heat exchangers intended for the production of steam and hot water, for receiving condensate and steam returned from the heat exchangers, and passing on excess, temporarily stored steam.
  • the biogas plant and the desulphurization plant are connected to lines for the supply of oxygen or oxidant.
  • the third heat exchanger and the fifth heat exchanger are equipped with a common superheater stage.
  • an adsorber For the desulfurization of the biogas, an adsorber can be provided which is arranged after the first scrubbing column.
  • Excess steam which is no longer needed within the plant, can be supplied to a steam turbine for generating electric power.
  • Biogas is produced in a biogas plant BO with 20 fermenters and 10 secondary fermenters using maize silage as fermentation substrate.
  • 10000 Nm 3 l of biogas 45.5 t / h of maize silage are required, which corresponds to a sludge quantity of 350 m 3 / h.
  • the maize silage as a biological raw material passes through a suitable feed 1 in the individual fermenters, which are heated by means of the line 3 supplied hot water (about 80 0 C). This hot water can also come as a return from the fermentation substrate R4.
  • moist fermentation substrate 4 is dried in a processing plant R4 and the resulting wastewater discharged via a line 36, which is recycled for a new Anmaischrea in the fermenter.
  • the fermentation substrate 4 is dried after treatment with a decanter in the treatment plant R4 by means of steam or hot water. Steam is generated in the steam generators W2 and W5 and supplied via the line 37. Hot water is generated in the heat exchanger W3 and fed and discharged via the supply and return lines 30 and 31.
  • the operation of the fermenter for the production of biogas is controlled so that biogas is produced with the lowest possible content of hydrogen sulfide.
  • pure oxygen is introduced into the fermenter via the line 5 and dosed so that sets an oxygen concentration of 0.2 vol .-% in the biogas as oxygen excess.
  • the produced biogas 2 is fed to a downstream biological desulfurization unit R1, in which the proportion of hydrogen sulfide is reduced by further addition of oxygen via the line 22 to a value of 10 to 50 ppm.
  • the biogas 6 produced after the removal of H 2 S in the desulfurization unit R1 has the following composition:
  • the desulfurized biogas 6 is subsequently fed to a scrubbing column K1.
  • a scrubbing column K1 In this under normal pressure or low vacuum (-10 to 150 mbar), the washing process to remove CO 2 , residual H 2 S and COS (organic sulfur compounds) carried out using an amine-containing wash solution.
  • This has an amine concentration of 15 to 70%, preferably 50%, being used as the amine diethanolamine.
  • the washing process carried out in a countercurrent principle in a scrubbing column with a packed bed of bulk CO 2 and the other aforementioned compounds are chemically bound in the detergent solution. This is subsequently regenerated in a separate plant, so that the detergent solution can be recycled.
  • the separated carbon dioxide is removed via the line 27 for further utilization.
  • the purified biogas discharged via line 7 (amount of 5360 Nm 3 / h) has the following composition:
  • the purified methane gas should contain after the removal of the CO 2 at least 1.0 vol .-% of oxygen as an excess of oxygen, so that the reforming process is initiated by own temperature increase. It is advantageous if the biogas still hydrogen (eg 0.2 vol .-%) is included. 1.8 vol .-% oxygen excess thus correspond to 8.5 mol of O 2 / mol H 2 S, based on the hydrogen sulfide-containing biogas with a sulfur content of about 1500 ppm.
  • the compressed biogas is not cooled and the heat of compression is used simultaneously for the heating of the biomethane to the synthesis gas temperature.
  • synthesis gas production can also be carried out under normal pressure, in the present example the biomethane is compressed to a pressure of 15 bar (energy consumption about 480 kW).
  • the biomethane is not cooled in the last compressor stage and mixed at a temperature of 150 ° C in line 7 with overheated to 450 0 C steam pressure of 20 bar and relaxed to a pressure of 15 bar.
  • the overheated steam required for this purpose is generated in the heat exchanger unit W6, W5 and supplied via the line 23.
  • 13650 kg / h of superheated steam and 2.5 kg / Nm 3 bio- or methane gas are mixed, wherein in the line 8, a mixing temperature of the biomethane / steam mixture of about 350 0 C is established.
  • the biomethane / steam mixture 8 is subjected to fine desulfurization, using hydrogen contained in the biomethane. This removes organic sulfur, such as thiophene, according to the subsequent reaction.
  • the organic sulfur compounds decompose to C 4 H 10 and hydrogen sulfide.
  • the organic sulfur occurs only in traces of a few ppm, but acts as a catalyst poison and should therefore be removed.
  • the hydrogen sulfide thus formed is completely bound in the adsorber A1 by adsorption on zinc oxide.
  • the loaded with zinc sulfide adsorbent is disposed of separately.
  • desulfurized biomethane / steam mixture of about 350 ° C is heated to a temperature of about 650 0 C.
  • the heat transfer medium used is the synthesis gas discharged from the heat exchanger W7, which passes via the line 12 into the heat exchanger W1. This cools by the heat exchange process from about 950 to about 670 0 C and is supplied via the line 13 to the heat exchanger W2.
  • the methane gas / steam mixture heated to about 650 ° C. is fed via the line 10 to the primary reformer R2 and catalytically converted into synthesis gas in this at a reaction temperature of about 900 ° C.
  • the excess of oxygen in the methane gas / Vapor mixture 10 in the primary reformer R2 generates additional heat energy by an exothermic oxidation of oxygen contained in the biogas with hydrogen as a quick initial ignition for the start of the reaction in the catalyst bed.
  • dried fermentation substrate 24 is used as fuel in the treatment plant R4.
  • a flue gas with a temperature of 990 to 1030 0 C is generated in the combustion chamber B1.
  • the required heat of reaction of 11.23 MW is transmitted by radiation to the biogas or methane gas.
  • the guidance of the biogas or methane gas takes place in catalyst tubes in the firing space of the primary reformer R2. In the primary reformer R2 and in the downstream secondary reformer R3, the following three main reactions proceed as temperature-dependent equilibrium reactions.
  • the endothermic reaction in the primary reformer R2 requires a heat output of 11.23 MW. Since the oxygen contained in the biogas reacts with heat release of heat, thus increasing the gas temperature in the Katalysatorroh ren by about 25 0 C spontaneously and thus there is a correspondingly hot zone for the endothermic methane conversion to CO and H 2 available.
  • the synthesis gas leaving the primary reformer R2 via line 11 (amount 29996 Nm 3 / h) has the following composition:
  • This syngas 11 are then fed via the line 25 1500 Nm 3 / h oxygen-containing gas having an oxygen content of 92 vol .-% and 8 vol .-% nitrogen, and was heated in the heat exchanger W7 from 25 0 C to 900 0 C.
  • R3 as a heat carrier exiting the synthesis gas is used from the secondary reformer, which thereby cools of 1025 0 C to 950 0 C.
  • the proportion of methane gas still contained in the synthesis gas 11 is converted with the release of heat to synthesis gas, wherein the temperature of the synthesis gas increases from 900 to 1025 ° C.
  • the synthesis gas leaving the secondary reformer R3 has the following composition: CH 4 0.15 vol.%
  • the hot synthesis gas is used several times for heat recovery for an energetically advantageous process management, as already partially explained above.
  • the synthesis gas is cooled by heat to the oxygen-containing gas to a temperature of about 950 0 C.
  • the 950 0 C hot synthesis gas passes via the line 12 into the heat exchanger W1 and is cooled by heat to the methane gas 9 to about 670 0 C.
  • the 670 0 C hot synthesis gas is fed via the line 13 to the steam generator W2 and cooled during the steam generation up to 300 0 C. This releases 2.78 MW of heat, which is used to produce 5,200 kg / h of 20 bar steam.
  • the generated steam is returned to the steam drum B2.
  • the approximately 330 0 C hot synthesis gas is subsequently fed to the heat exchanger W3, in which the synthesis gas is cooled under operating pressure of 15 bar to a temperature of 60 0 C.
  • Via a pressure circuit (pump P3 and lines 31, 30, 3) so that hot water is produced at a temperature of 120 ° C to 80 ° C, depending on the supplied amount of water.
  • the resulting heat is 7.3 MW. This amount of heat is therefore so high because the vast majority of water in the synthesis gas condenses under these conditions.
  • a total of 7688 kg / h of condensate accumulate, which are returned via the lines 32, 34 by means of the pump P2 back into the steam drum B2 and used for steam generation.
  • synthesis gas is further cooled in the downstream heat exchanger W4 pressurized with cooling water to a temperature of 30 0 C.
  • a cooling capacity of 620 KW must be dissipated via the cooling water and condensate further 243 kg / h of condensate, which pass through the line 33 in the line 34.
  • the predried synthesis gas with a quantity of 19645 Nm 3 / h has the following composition:
  • the synthesis gas thus obtained can then be worked up further (for example by drying or separating off portions of hydrogen and carbon monoxide by means of pressure swing adsorption).
  • the synthesis gas obtained can also be used for further synthesis to methanol, ammonia or liquid hydrocarbons.
  • the withdrawn at the head of the primary reformer R2 hot flue gas having a temperature of about 1100 0 C is supplied via the line 18 to the steam superheater W6, W5.
  • Superheated steam is removed via line 23 and added to the biogas or methane gas.
  • steam enters the steam drum B2.
  • the circuit of the heat exchangers W6 and W5 is shown only symbolically, since both heat exchangers W6 and W5 are interconnected and thus there is no apparatus-technical separation. This is necessary because due to different heat transfer, the interpretation must be made so that no exceedances of maximum permissible wall temperatures.
  • the heat exchanger W6 is therefore integrated in the heat exchanger W5 and connected to an economizer, not shown.
  • the flue gas leaving the steam superheater W6, W5 has a temperature of about 220 ° C. and is then fed via the line 20 to the exhaust gas purification stage K3. Via the line 21, the purified flue gas is discharged to the environment.
  • the steam drum B2 is additionally supplied via the line 35 condensate (heating via economizer) and discharged steam discharged via the line 37, which can be used for example for external power generation.
  • fermentation substrate in a quantity of 21, 2 t / h after pretreatment in the decanter with a water content of 70%, which after treatment and drying to a residual moisture of 30% has a calorific value of 4.1 kW, is produced as secondary raw material. kg owns.
  • 9.1 t / h of the dried fermentation substrate as a fuel a heating power of approximately 37.31 MW is generated.
  • the consumption of heating power for the fermentation substrate drying (hot water 120 0 C) and detergent regeneration (hot water 160 "C) is 13.9 MW.
  • the detergent regeneration falls from the heating power to be used with a temperature of 160 0 C, a waste heat in the amount of 65% of the energy used. This can be done from the waste heat of the detergent regeneration, the heating of the fermenter (hot water 80 0 C), which is usually required only at outdoor temperatures of below 20 0 C. The total balance thus results in a surplus of heat energy of 0.8 MW, which can be used elsewhere.

Abstract

L'invention se rapporte à un procédé de production de gaz de synthèse à partir de biogaz et à une installation appropriée pour la réalisation du procédé. Le but de l'invention est de remédier aux inconvénients de l'état de la technique et, à ce titre, de proposer un procédé qui se distingue par une réalisation économique du processus et un meilleur rendement. A cet effet, avant la transformation catalytique du biogaz, on sépare presque complètement de celui-ci, le sulfure d'hydrogène et le dioxyde de carbone dans des étapes séparées de purification, le sulfure d'hydrogène étant éliminé par voie biologique, par addition d'oxygène et/ou d'un agent d'oxydation contenant de l'oxygène. L'oxygène ou l'agent d'oxydation est ajouté dans une quantité telle qu'un excès d'oxygène d'au moins 1,0 % en volume est présent dans le biogaz purifié (gaz méthane). Le biogaz est condensé sans déshumidification, chauffé et mélangé à de la vapeur surchauffée. En fonction de l'excès d'oxygène, de l'énergie thermique supplémentaire est produite pendant le processus de reformage, par oxydation exothermique de l'oxygène présent dans le biogaz avec de l'hydrogène dans le lit catalytique, pour la transformation endothermique du méthane en gaz de synthèse.
EP08785493A 2007-08-16 2008-08-12 Procédé et installation pour la production d'un gaz de synthèse à partir de biogaz Withdrawn EP2188210A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102007038760A DE102007038760B3 (de) 2007-08-16 2007-08-16 Verfahren und Anlage zur Herstellung von Synthesegas aus Biogas
PCT/EP2008/006614 WO2009021710A2 (fr) 2007-08-16 2008-08-12 Procédé et installation pour la production d'un gaz de synthèse à partir de biogaz

Publications (1)

Publication Number Publication Date
EP2188210A2 true EP2188210A2 (fr) 2010-05-26

Family

ID=40076272

Family Applications (1)

Application Number Title Priority Date Filing Date
EP08785493A Withdrawn EP2188210A2 (fr) 2007-08-16 2008-08-12 Procédé et installation pour la production d'un gaz de synthèse à partir de biogaz

Country Status (6)

Country Link
US (1) US8187568B2 (fr)
EP (1) EP2188210A2 (fr)
CN (1) CN101801842B (fr)
BR (1) BRPI0815478A2 (fr)
DE (1) DE102007038760B3 (fr)
WO (1) WO2009021710A2 (fr)

Families Citing this family (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20120275992A1 (en) * 2009-11-24 2012-11-01 Juzer Jangbarwala Dual Purpose Gas Purification by Using Pressure Swing Adsorption Columns for Chromatographic Gas Separation
US8658026B2 (en) 2011-12-22 2014-02-25 Iogen Corporation Method for producing fuel with renewable content having reduced lifecycle greenhouse gas emissions
US8945373B2 (en) 2011-12-22 2015-02-03 Iogen Corporation Method for producing renewable fuels
EP2695946A1 (fr) 2012-08-09 2014-02-12 Methapower Biogas GmbH Procédé et installation destinés à la fabrication de diméthyléther
WO2014041645A1 (fr) * 2012-09-12 2014-03-20 三菱重工業株式会社 Dispositif de reformage et dispositifs pour la fabrication de produits chimiques le comprenant
US10005963B2 (en) 2012-09-20 2018-06-26 University Of South Florida Systems and methods for producing liquid fuels from landfill gases
CN104591083B (zh) * 2015-01-28 2017-03-01 张进勇 一种制氢方法
US11242988B2 (en) * 2016-02-16 2022-02-08 Thermochem Recovery International, Inc. Two-stage energy-integrated product gas generation system and method
DE102017200435A1 (de) * 2017-01-12 2018-07-12 Siemens Aktiengesellschaft Verfahren und Vorrichtung zur Herstellung von Kohlenwasserstoffen
US10696906B2 (en) 2017-09-29 2020-06-30 Marathon Petroleum Company Lp Tower bottoms coke catching device
KR20210097189A (ko) * 2018-12-06 2021-08-06 라벤 에스알 엘엘씨 스팀/co2 개질에 의한 수소 및 ft 생성물의 제조
CA3109675A1 (fr) 2020-02-19 2021-08-19 Marathon Petroleum Company Lp Melanges de mazout a faible teneur en soufre pour l`amelioration de la stabilite et methodes connexes
CN111547678B (zh) * 2020-04-08 2022-03-25 华南农业大学 沼气全组分热催化制备甲醇的方法及系统
US11845713B2 (en) * 2021-01-22 2023-12-19 Standard Alcohol Company Of America, Inc. Biogas conversion to mixed alcohols
US11905468B2 (en) 2021-02-25 2024-02-20 Marathon Petroleum Company Lp Assemblies and methods for enhancing control of fluid catalytic cracking (FCC) processes using spectroscopic analyzers
US20220268694A1 (en) 2021-02-25 2022-08-25 Marathon Petroleum Company Lp Methods and assemblies for determining and using standardized spectral responses for calibration of spectroscopic analyzers
US11898109B2 (en) 2021-02-25 2024-02-13 Marathon Petroleum Company Lp Assemblies and methods for enhancing control of hydrotreating and fluid catalytic cracking (FCC) processes using spectroscopic analyzers
EP4323308A1 (fr) 2021-04-15 2024-02-21 Iogen Corporation Procédé et système de production d'hydrogène renouvelable à faible intensité de carbone
WO2022221954A1 (fr) 2021-04-22 2022-10-27 Iogen Corporation Procédé et système de production de combustible
FR3122839A1 (fr) * 2021-05-12 2022-11-18 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Installation et Procédé de production de gaz de synthèse présentant un moyen de limiter les émissions de CO2 par récupération de chaleur
FR3122840A1 (fr) * 2021-05-12 2022-11-18 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Installation et Procédé de production de gaz de synthèse présentant un moyen de limiter les émissions de CO2 au moyen de vapeur
IT202100023411A1 (it) * 2021-09-10 2023-03-10 Enerva H2 Srl Metodo e apparato di produzione di energia elettrica da biomassa organica
US11802257B2 (en) 2022-01-31 2023-10-31 Marathon Petroleum Company Lp Systems and methods for reducing rendered fats pour point
US11807530B2 (en) 2022-04-11 2023-11-07 Iogen Corporation Method for making low carbon intensity hydrogen

Family Cites Families (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3463603A (en) * 1967-03-17 1969-08-26 Shell Oil Co Method of separating acidic gases from gaseous mixture
US3501516A (en) * 1968-11-29 1970-03-17 Pritchard & Co J F Method for production of methanol
DE3130013A1 (de) * 1981-07-30 1983-02-17 Battelle-Institut E.V., 6000 Frankfurt "verfahren zur verfluessigung von biogas"
NL9300833A (nl) * 1993-05-13 1994-12-01 Gastec Nv Werkwijze voor de produktie van waterstof/koolmonoxide mengsels of waterstof uit methaan.
DE4322738A1 (de) * 1993-07-08 1995-01-12 Norbert Dr Volk Verfahren und Vorrichtung zur mikrobiellen Reinigung schwefelwasserstoffhaltiger Brenngase
DE19827154C2 (de) * 1998-06-18 2003-01-30 Irt Innovative Recycling Techn Verfahren zur Herstellung von Methanol aus Biogas sowie eine Vorrichtung zur Durchführung des Verfahrens
JP2000351607A (ja) * 1999-06-09 2000-12-19 Mitsubishi Heavy Ind Ltd 水素製造装置
US6299994B1 (en) * 1999-06-18 2001-10-09 Uop Llc Process for providing a pure hydrogen stream for use with fuel cells
AU2001236060A1 (en) * 2000-03-02 2001-09-12 Ebara Corporation Fuel cell power generation method and system
JP4533515B2 (ja) * 2000-08-16 2010-09-01 三菱重工業株式会社 合成ガスの製造方法
DE20202722U1 (de) * 2001-03-05 2002-05-16 Lipp Gmbh Vorrichtung zum Entschwefeln von Biogas mit Mikroorganismen
JP2003081603A (ja) * 2001-07-04 2003-03-19 Hitachi Ltd 水素製造装置及びそれを用いた発電システム
US6797253B2 (en) * 2001-11-26 2004-09-28 General Electric Co. Conversion of static sour natural gas to fuels and chemicals
BR0215051A (pt) * 2001-12-18 2004-12-07 Jerrel Dale Branson Sistema e método para extração de energia a partir de resìduo agrìcola
US6984372B2 (en) * 2002-09-06 2006-01-10 Unitel Technologies, Inc. Dynamic sulfur tolerant process and system with inline acid gas-selective removal for generating hydrogen for fuel cells
US7427388B2 (en) * 2004-03-19 2008-09-23 Air Products And Chemicals, Inc. Process for improving prereforming and reforming of natural gas containing higher hydrocarbons along with methane
DE102004027442B4 (de) * 2004-06-04 2006-07-06 Applikations- Und Technikzentrum Für Energieverfahrens-, Umwelt- Und Strömungstechnik (Atz-Evus) Verfahren zur Entfernung von schwefelhaltigen Verbindungen aus Biogas
US7037485B1 (en) * 2004-11-18 2006-05-02 Praxair Technology, Inc. Steam methane reforming method
DE102005031224A1 (de) 2005-07-01 2007-01-04 DOPHEIDE, Hans-Jürgen Alternative Nutzungsvariante für Biogasanlagen
US20070130832A1 (en) * 2005-12-13 2007-06-14 General Electric Company Methods and apparatus for converting a fuel source to hydrogen

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2009021710A2 *

Also Published As

Publication number Publication date
DE102007038760B3 (de) 2009-01-02
CN101801842B (zh) 2013-07-31
CN101801842A (zh) 2010-08-11
WO2009021710A2 (fr) 2009-02-19
WO2009021710A3 (fr) 2009-05-14
US8187568B2 (en) 2012-05-29
BRPI0815478A2 (pt) 2015-02-10
US20110175032A1 (en) 2011-07-21

Similar Documents

Publication Publication Date Title
DE102007038760B3 (de) Verfahren und Anlage zur Herstellung von Synthesegas aus Biogas
EP2361138B1 (fr) Procédé et dispositif pour épurer des gaz bruts, en particulier un biogaz pour obtenir du méthane
DE60116602T2 (de) Brennstoffzellen-energiegewinnungsverfahren und -system
EP2288425B1 (fr) Procédé et installation de purification de biogaz pour la récupération de méthane
EP2038045B1 (fr) Procédé de purification de biogaz produit par une installation de production de biogaz et système de purification de biogaz
DE112010001543B4 (de) Verfahren und Vorrichtung zum Zurückführen von Restgas
CN101918305A (zh) 利用甲醇生产氢气和燃料，生产氢气和燃料的方法及设备
DE102008002963A1 (de) Polygenerationssysteme
CA2469653A1 (fr) Systeme et procede d'extraction d'energie des dechets agricoles
DE2926892A1 (de) Verfahren zur herstellung eines wasserstoffhaltigen gases
DE112020005178T5 (de) Ammoniak-Derivat-Produktionsanlage und Ammoniak-Derivat-Produktionsverfahren
CN105531222A (zh) 通过co2还原法的合成气生产
EP2485980B1 (fr) Procédé permettant de faire fonctionner un processus de centrale igcc à séparation de co2 intégrée
DE112011104569T5 (de) Verfahren und Vorrichtung zum Reformieren von produziertem Gas
DE102009056660B4 (de) Verfahren und Anlage zur chemisorptiven Abtrennung von Kohlendioxid aus Bio- oder Klärgas mittels einer aminhaltigen Waschlösung und Regeneration der beladenen Waschlösung
DE102013113946A1 (de) System und Verfahren zur CO2 - Erfassung mittels eines H2- Separators, der Wärmeentschwefelungstechnologie verwendet.
DE1958033A1 (de) Erzeugung von Wasserstoff oder Ammoniaksynthesegas bei mittlerem Durck
WO2017114882A1 (fr) Procédé à haut rendement énergétique pour la méthanisation et la récupération de dioxyde de carbone simultanées
EP0215930B1 (fr) Generation d'energie thermique par la combustion de gaz de synthese
CN210261105U (zh) 一种利用黄磷尾气制备多种合成气的装置
CN107099348A (zh) 利用煤炭地下气化产品气生产合成天然气的方法
DE102019000803A1 (de) Verfahren zur Erzeugung von Synthesegas
DE102010024429A1 (de) CO2 freies IGCC Kraftwerk mit Heißgasreinigung und optimierter CO2 Abtrennung
CN206692604U (zh) 一种用焦炉气与水煤浆制备水煤气的系统
DE4121290A1 (de) Verfahren zur thermischen umsetzung von schwefelwasserstoff zu elementarem schwefel

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 20100310

AK Designated contracting states

Kind code of ref document: A2

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MT NL NO PL PT RO SE SI SK TR

AX Request for extension of the european patent

Extension state: AL BA MK RS

DAX Request for extension of the european patent (deleted)
RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: DGE DR.-ING. GUENTHER ENGINEERING GMBH

17Q First examination report despatched

Effective date: 20141128

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20150409