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WO2013068643A1 - A method and a system for producing liquid fuel from biomass - Google Patents

A method and a system for producing liquid fuel from biomass Download PDF

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Publication number
WO2013068643A1
WO2013068643A1 PCT/FI2012/051085 FI2012051085W WO2013068643A1 WO 2013068643 A1 WO2013068643 A1 WO 2013068643A1 FI 2012051085 W FI2012051085 W FI 2012051085W WO 2013068643 A1 WO2013068643 A1 WO 2013068643A1
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WO
WIPO (PCT)
Prior art keywords
synthesis gas
gas
filtered
quenching
biomass
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.)
Ceased
Application number
PCT/FI2012/051085
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English (en)
French (fr)
Inventor
Jari Hangasluoma
Peter RÖGER
Pekka Jokela
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.)
UPM Kymmene Oy
Original Assignee
UPM Kymmene Oy
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Filing date
Publication date
Application filed by UPM Kymmene Oy filed Critical UPM Kymmene Oy
Publication of WO2013068643A1 publication Critical patent/WO2013068643A1/en
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • 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
    • C01B3/02—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
    • C01B3/48—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 followed by reaction of water vapour with carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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    • 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
    • C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
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    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
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    • C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
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    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
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    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/463—Gasification of granular or pulverulent flues in suspension in stationary fluidised beds
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    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
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    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/723—Controlling or regulating the gasification process
    • 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
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    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C10K1/024—Dust removal by filtration
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    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
    • C10K1/06—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials combined with spraying with water
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    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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    • 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
    • C10K3/023—Reducing the tar content
    • C—CHEMISTRY; METALLURGY
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    • 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]
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    • 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
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    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
    • 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
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    • C10G2300/10—Feedstock materials
    • C10G2300/1011—Biomass
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    • C10G2300/10—Feedstock materials
    • C10G2300/1011—Biomass
    • C10G2300/1014—Biomass of vegetal origin
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    • 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
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    • C10G2300/1011—Biomass
    • C10G2300/1018—Biomass of animal origin
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    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4056—Retrofitting operations
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    • 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
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    • 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
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    • 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
    • Y02P20/141—Feedstock
    • Y02P20/145—Feedstock the feedstock being materials of biological origin
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock

Definitions

  • the invention relates to a process for producing liquid biofuel from solid biomass.
  • synthesis gas is produced by gasifying the solid biomass and the synthesis gas is post processed to produce biofuel.
  • post processing the synthesis gas is reformed and before reforming the synthesis gas is cleaned e.g. by filtration.
  • Liquid fuels are commonly used in many areas of human life including heating, transportation and producing electricity. Liquid fuels are often made of fossile oil containing substances by distillation and cracking. However, sustainable energy sources have received a lot of interest in recent years due to environmental changes— observed or predicted— such as global warming. One possibility to use liquid fuels and answer the environmental issues is to produce liquid fuels from biomass.
  • Gasification is a promising process for converting solid biomass to gaseous or liquid fuel.
  • solid biomass is first converted to a synthesis gas, which can be further processed to produce liquid fuel or gaseous fuel or both liquid and gaseous fuels.
  • the gasification is done at an elevated temperature, e.g. 850 ⁇ .
  • the synthesis gas thus pr oduced typically comprises tars and methane. Both tars and methane influence the possibilities of utilizing the synthesis gas, and therefore, their content may be reduced by reforming.
  • oxygen, steam, and synthesis gas are reacted at elevated temperature.
  • the reformed synthesis gas is sent to a Fischer-Tropsch (FT) synthesis process to produce liquid biofuel.
  • FT Fischer-Tropsch
  • the synthesis gases or reformed synthesis gases need to be cleaned, since the FT -process is sensitive to impurities such as solid particles, e.g. ash.
  • impurities such as solid particles, e.g. ash.
  • efficient cleaning of synthesis gas and recycling of intermediate process products are still problematic in the process.
  • the yield of the process depends on the order in which different process steps are performed.
  • the overall consumption of energy and raw materials depends on the recycling of intermediate process products.
  • the investment costs for a system for producing liquid fuel from solid biomass depends on the complexity of the process equipment, and the complexity of the process equipment may depend on the process itself.
  • a method for producing liquid fuel from solid biomass is disclosed.
  • the biofuel yield of the process is relatively high, partly due to efficient recycling of intermediate process products and partly due to the order of different process steps.
  • synthesis gas is produced from solid biomass in a gasification reactor.
  • the synthesis gas is cleaned by filtration before a reforming process to protect reformer-reactor and reformer-catalyst from fouling (deposition of particulate matter such as ash, soot, dust), thus improving the yield and stability of the reforming process.
  • the synthesis gas is hot and filters can only be operated up to a certain maximum temperature.
  • the synthesis gas is cooled before filtration. The features of the method are described in the independent claim 1 .
  • the synthesis gas is cooled by recycling gases in the process, and mixing recycled gases with synthesis gas.
  • the recycled gases are cooler than the synthesis gas, and thereby mixing recycled gas with synthesis gas cools the synthesis gas.
  • the synthesis gas is quenched by spraying liquid onto the synthesis gas before filtration. At least part of the liquid evaporates, thereby cooling the synthesis gas.
  • recycled gases may be mixed with the synthesis gas to further cool the synthesis gas. Quenching reduces the amount of recycled gases in the process, and thus decreases the size and complexity of process equipment. These reductions show also as smaller investment costs for the system for producing liquid biofuel from biomass.
  • water is used for quenching, the generated additional steam in the synthesis gas has beneficial effects in the reforming process. Furthermore some of the heat picked up by the quench water can be recovered for drying the raw biomass.
  • a cooling device can be used in the process, as described in the independent claim 13.
  • Figure 1 shows a process for producing biofuel from biomass
  • Figure 2 shows more details of the process of Fig. 1 ,
  • Figure 3a shows a process of gasifying biomass to produce synthesis gas in a process for producing liquid biofuel from solid biomass
  • Figure 3b shows quenching, filtration, reforming, and cooling of synthesis gas in a process for producing liquid biofuel from solid biomass
  • Figure 3c shows synthesis gas shifting, synthesis gas scrubbing, and subsequent process steps in a process for producing liquid biofuel from solid biomass
  • Figure 4a shows recycling gases to cool synthesis gas in a process for producing liquid biofuel from solid biomass
  • Figure 4b shows quenching and recycling gases to cool synthesis gas in a process for producing liquid biofuel from solid biomass
  • Figure 4c shows quenching and recycling gases to cool synthesis gas in another process for producing liquid biofuel from solid biomass
  • Figure 4d shows optimizing the amount of quenching liquid
  • Figure 4e shows a process for producing liquid biofuel from solid biomass, wherein only the tail gases are recycled
  • Figure 5a shows an embodiment of a quencher 210
  • Figure 5b shows another embodiment of a quencher 210
  • Figure 5c shows a third embodiment of a quencher 210.
  • Gasification is a promising process for converting solid biomass to fuel.
  • solid biomass is converted to synthesis gas, which can be further processed to produce liquid fuel or gaseous fuel or both liquid and gaseous fuels.
  • the present invention relates especially to a process for producing liquid fuels from wood-based solid biomass.
  • the process comprises gasifying solid biomass to synthesis gas and post processing the synthesis gas to biofuel.
  • the post processing comprises conditioning the synthesis gas to a product gas, Fischer-Tropsch processing the product gas to product fluid, and upgrading the product fluid to biofuel.
  • the conditioning comprises
  • the conditioning may further comprise at least one of
  • the whole post processing may comprise
  • gasification is performed in a fluidized bed to increase the yield of synthesis gas from the gasification process.
  • the synthesis gas is cleaned before reforming to improve the yield and stability of the reforming process.
  • gasification is typically done at an elevated temperature. Therefore, cleaning of synthesis gas poses a problem since e.g. there is no filter, which can withstand such high temperatures.
  • excessive cooling of synthesis gases before reforming is not beneficial and should therefore be optimized, since the synthesis gas is reformed typically at an elevated temperature.
  • the synthesis gas is cleaned by filtration before reforming.
  • synthesis gas is cooled by quenching before filtration. Quenching is done by spraying quenching liquid onto the synthesis gas in a quencher before filtration.
  • synthesis gas is cooled by mixing recycled gas in the process. Recycled gas may comprise at least one of: scrubbed synthesis gas, tail gas 397 of an acid gas removal phase, FT tail gas 395, and off gas 410, as will be discussed in more detail later.
  • synthesis gas is cooled both by quenching and by gas mixing, in either order.
  • Synthesis gas is cooled in a cooling device 218.
  • the cooling device 218 comprises at least one of a quencher and a gas mixer. If the cooling device comprises a quencher and a gas mixer, the cooling device comprises means for conveying synthesis gas from the quencher to the gas mixer or from the gas mixer to the quencher.
  • Figs. 3a-3c describe in more detail an embodiment of the invention.
  • biomass 100 e.g. wood based biomass is stored in a container 102.
  • the container is located in normal atmosphere and therefore the container 102 contains typically air and the biomass 100.
  • Air on the other hand comprises nitrogen.
  • From the container 102 biomass is fed using a lock hopper mechanism to another container 108.
  • the lock hopper mechanism is used to remove nitrogen from the biomass-air mixture, since the presence of nitrogen has some disadvantages in the later process steps.
  • the lock hopper mechanism is also used to recycle carbon containing gases, namely carbon dioxide CO2, available from later process steps. Recycling of CO2 is advantageous, as liquid biofuel comprises carbon.
  • the lock hopper mechanism comprises two air lock valves 104 and a third container 106.
  • Biomass-air mixture is first fed to the container 106. At least some air is removed from the container by feeding carbon dioxide (CO2) 120 to the container 106. Carbon dioxide replaces at least some of the air in the container 106.
  • the biomass-air-CO2 mixture is then fed to the container 108. Carbon dioxide 120 may be used also in the container 108 to remove air from the container 108.
  • CO2 may be fed to the process also to increase the carbon content of the biomass-air- CO2 feed.
  • CO2 may be available from an Acid Gas Removal -process. From the container 108 biomass 100 is fed with a feeder 122 through a channel 135 to a gasification reactor 150.
  • the gasification reactor is a fluidized bed reactor.
  • bed material 130 is fed to the gasification reactor 150.
  • Bed material 130 is fed to the process from a container 132 through the channel 135.
  • the bed material 130 comprises dolomite, since this reduces the tar content of the synthesis gas 200. More preferable the bed material consists essentially of dolomite.
  • the gasification reactor 150 is a fluidized bed reactor.
  • the fluidized bed reactor comprises means for forming a fluidized bed of biomass 100 and bed material 130.
  • the means may comprise nozzles through which fluidizing gases are fed to the reactor from below.
  • Biomass 100 and bed material 130 are arranged in a fluidized state by feeding oxygen 140 and steam 142 to the gasification reactor 150.
  • Oxygen is fed to the reactor in order to facilitate burning of some of the biomass. Burning releases energy from the biomass 100 and thus heats the gasification reactor 150 and the material in the reactor.
  • the temperature in the gasification reactor 150 may be e.g. about 850 ⁇ .
  • the gasification reactor may be pressurized .
  • the (absolute) pressure in the gasification reactor may be e.g. 10 bar.
  • Bottom ash 155 comprises ash (burned biomass), impurities (such as stones or metal pieces), and bed material 130.
  • Synthesis gas 200 is led from the gasification reactor 150 through a cyclone 160. Cyclone 160 separates synthesis gas 200 from solid materials such as bed material, ash (burned biomass), and biomass. Solid material is fed back to the gasification reactor through the channel 165. Synthesis gas 200 is conveyed to subsequent process steps. Solid material is removed from the synthesis gas in the cyclone 160 to clean the synthesis gas 200 before filtration, at least to some degree.
  • synthesis gas 200 is filtered in a filtration unit 220 and reformed in a reformer 240. It has been noticed that the yield and the stability of the reforming process step increase, if the synthesis gas is filtered before reforming. Moreover, since reforming requires a relatively high temperature, the synthesis gas is advantageously not cooled between the filtration unit 220 and the reformer 240. Therefore, the filtered synthesis gas may be conveyed to the reformer 240 such that the temperature of the filtered synthesis gas leaving the filtration unit 220 is essentially same as the temperature of the filtered synthesis gas entering the reformer 240, to minimize heating of the filtered synthesis gas in the reformer 240.
  • the filtered synthesis gas may also be heated before the reformer 240.
  • the filtered synthesis gas is conveyed to the reformer 240 such that the temperature of the filtered synthesis gas leaving the filtration unit 200 is less than the temperature of the filtered synthesis gas entering the reformer 240, to minimize heating of the filtered synthesis gas in the reformer 240.
  • the system comprises a heater arranged to heat the filtered synthesis gas.
  • the heater (not shown in Fig. 3b) is arranged to heat the filtered synthesis gas before the reformer.
  • the heater may be e.g. a heat exchanger.
  • the heater may be arranged to heat the filtered synthesis gas using the heat of at least one of: the reformer 240, the synthesis gas in the reformer, the reformed synthesis gas, the synthesis gas 200 before quenching, the material in the cyclone, the cyclone 160, the material in the gasifier, and the gasifier 150.
  • the filtration unit 220 may not withstand such a high temperature.
  • the filtration unit 220 may comprise filter plates 225 to filter the synthesis gas.
  • the filter plates 225 may comprise metallic plates for filtering the synthesis gas.
  • Such metallic plates are typically designed to operate at maximum temperatures of 600-800 ⁇ , dep ending on the metal used in the filter plates 225. Therefore, the synthesis gas needs to be cooled before filtration.
  • synthesis gas 200 is cooled by quenching the synthesis gas 200 in a cooling device 218.
  • the cooling device 218 comprises a quencher 210.
  • the synthesis gas is cooled by spraying quenching liquid 215 onto the synthesis gas.
  • synthesis gas 200 is cooled also by mixing (quenched) synthesis gas with recycled gas 205.
  • the recycled gas 205 comprises only scrubbed synthesis gases or at least one of: a part of scrubbed synthesis gas, tail gas 397 of an acid gas removal phase, FT tail gas 395, and off gas 410, as will be discussed in more detail later.
  • synthesis gas may be cooled only by mixing recycled gas, only by quenching, or both by quenching and mixing recycled gas, the last option shown in Fig. 3b.
  • the temperature of the recycled gas 205 is much lower than the temperature of the synthesis gas.
  • the temperature of scrubbed synthesis gas may be in the range of 30 - 150 ⁇ .
  • recycled gas 205 may be mixed with synthesis 200 gas before or after the quencher 210. Recycled gas 205 may be obtained from later phases of the process, as will be discussed later.
  • the recycled gas comprises only scrubbed synthesis gas and recycled FT tail gas 395 is introduced into the gasifier 150.
  • the mass ratio of recycled gas 205 to synthesis gas 200 depends on the temperature of the gases as well as the maximum allowed temperature of the gas filtration unit 220. If the ratio is high, i.e. a lot of gas needs to be recycled, piping for the recycled gas 205 needs a lot of space in the gasification system, and material costs for the piping become significant. Therefore the ratio of mass flow of the recycled gas 205 to mass flow of the synthesis gas 200 is preferably small. Most preferably the cooling is done only by quenching.
  • the synthesis gas 200 is cooled by quenching in a quencher 210 to produce quenched synthesis gas.
  • quenching liquid 215 is sprayed onto the synthesis gas 200.
  • the evaporation temperature of the quenching liquid 215 is so low that the quenching liquid 215 is evaporated when the quenching liquid 215 is sprayed onto the synthesis gas 200.
  • the liquid 215 comprises water.
  • the quenching liquid 215 may comprise at least 90 % of water.
  • the quenching liquid may consist essentially of demineralized water.
  • the synthesis gas 200 is quenched in the quencher 210 by spraying quenching liquid 215 onto the synthesis gas 200, some of the quenching liquid 215 is evaporated. Preferably all the quenching liquid 215 is evaporated. Evaporation of the quenching liquid 215 effectively converts sensible heat into latent heat, and therefore, the temperature of the synthesis gas 200 decreases significantly in the quencher 210.
  • the quenched synthesis gas may be further cooled by mixing it with recycled gas 205, as depicted in Fig. 3b. Mixing with cool gas is referred to as gas cooling. However, in another embodiment (cf. Fig. 4c), the gas cooling is performed before quenching, The process comprises at least one of gas cooling and quenching. In case the process comprises both the steps, the steps may be in either order. The synthesis gas after these steps will be referred to as filterable synthesis gas. In an embodiment, scrubbed synthesis gas is not recycled. In this embodiment, other gases may be recycled in the process. If such gases are recycled, at least one of the tail gases from the FT process 395, the tail gases 397 from the acid gas removal phase, and the off gas 410 from the upgrading are recycled.
  • the ratio of mass flow of the recycled gas 205 to mass flow of the synthesis gas 200 may be less than 10 %, for example about 5 %. If only the tail gases and the off gases are recycled, the FT tail gases 395 and the off gases 410 may be recycled to the gasifier 150 and acid gas removal tail gases 397 may be recycled to a container 108, 106 for biomass.
  • the filterable synthesis gas entering the filtration unit 220 is preferably dry, i.e. the filterable synthesis gas does not comprise liquid droplets of quenching liquid 215.
  • the filterable synthesis gas is filtered to filtered synthesis gas.
  • the filtered synthesis gas is led to a reformer 240.
  • the temperature of the filtered synthesis gas may be below 800 ⁇ and as an example 700 ⁇ . However, reforming of synthesis gas is performed in a higher temperature.
  • the temperature in the reformer 240 may be between 900 - 950 ⁇ .
  • the synthesis gas is preferably not cooled further after the quencher 210 or the point 212 of recycle gas 205 cooling, whichever is the later in the process, and before the filtration unit 220.
  • the system may comprise a gas mixer at the point 212 of recycle gas 205 cooling.
  • the method may comprise using a gas mixer to cool the synthesis gas 200.
  • the filterable synthesis gas is conveyed to the filtration unit 220 such that the temperature of the filterable synthesis gas leaving the quencher 210 or the point 212 of recycle gas 205 cooling, whichever is the later in the process, is essentially the same as the temperature of the synthesis gas in the filtration unit 220.
  • the filtered synthesis gas may be conveyed from the filtration unit 220 to the reformer 240 such that the temperature of the filtered synthesis gas leaving the filtration unit 220 is essentially same as, or less than, the temperature of the filtered synthesis gas entering the reformer 240.
  • part of the synthesis gas is burned in the reformer 240.
  • oxygen 230 (O 2 )
  • steam 232 (H 2 O) is fed to the reformer 240.
  • Filtered synthesis gas is reformed in the reformer 240 to decrease the amount of tars and methane in the filtered synthesis gas. Furthermore, the filtered synthesis gas is reformed to reformed synthesis gas.
  • steam (H 2 O) and carbon monoxide (CO) may react to produce carbon dioxide (CO 2 ) and hydrogen (H 2 ).
  • the tar and methane of the synthesis gas may react with steam to produce carbon monoxide and hydrogen.
  • the fluid may comprise water. It may also comprise steam.
  • water 252 is fed to the heat exchanger 250, and in the heat exchanger 250, the water 252 is evaporated to produce steam 254.
  • Steam 254 is used for generating power, such as electricity. Steam 254 may be superheated i.e. heated above the saturation temperature. In the heat exchanger 250, the reformed synthesis gas is cooled to cooled synthesis gas. The temperature of the cooled synthesis gas may be e.g. 150-300 ⁇ .
  • the cooled synthesis gas 300 is led to a gas shifting process.
  • the cooled synthesis gas flow 300 may be divided into a first part 302 and a second part 304.
  • the first part 302 is led to a gas shifter 310.
  • the second part 304 bypasses the gas shifter and is led to subsequent process steps without gas shifting.
  • the mass ratio of the first part 302 and the second part 304 may be controlled e.g. with a valve 306.
  • the ratio of hydrogen (H 2 ) to carbon monoxide (CO) is modified to optimize the performance of the subsequent FT process.
  • steam 259 is also fed to the gas shifter 310.
  • Steam 259 may comprise steam 399 obtained from a heat exchanger 386.
  • the molar ratio of H 2 to CO in the shifted synthesis gas 315 is between 2.5 to 1 and 1 .0 to 1 .
  • the molar ratio of H 2 to CO in the shifted synthesis gas 315 is between 2.1 to 1 and 1 .8 to 1 .
  • the mixture of the first part 302 after the gas shifter 310 and the second part 304 of the cooled synthesis gas will be called shifted synthesis gas.
  • the shifted synthesis gas 315 is conveyed to a scrubber 320.
  • the scrubber comprises two scrubbing stages, a first stage 330 and a second stage 340.
  • a (first) scrubbing solution (331 , 332) is circulated.
  • the scrubbing solution 331 is led from the first stage 330 to a heat exchanger 335, after which the cooled scrubbing solution 332 is led to the first stage 330.
  • the circulation of the scrubbing solution may be enabled with a pump (not shown in the figure).
  • the cooled scrubbing solution 332 is sprayed onto the shifted synthesis gas to scrubb the shifted synthesis gas.
  • the scrubbing solution is essentially in liquid form to ensure scrubbing.
  • the (first) scrubbing solution (331 , 332) comprises water.
  • the scrubbing solution may consist of water or it may consist essentially of water.
  • heat is recovered from the scrubbing solution.
  • a cool heat transfer medium 336 is fed to the heat exchanger 335 where it heats to a heated heat transfer medium 337.
  • the heat transfer medium may comprise water.
  • the recovered heat may be used to dry biomass 100.
  • the heated heat transfer medium may be conveyed to the container 102 (Fig. 3a), where the biomass is stored. Even if not shown in Fig. 3c, the system may comprise means for conveying the heated heat transfer medium 337 from the heat exchanger 335 to a dryer 450 (cf.
  • the container 102 may be used as the dryer 450 for biomass.
  • the dryer 450 may be located near the container 102.
  • the system may comprise means for conveying the dried biomass from the dryer 450 to the container 102.
  • a second scrubbing solution is circulated.
  • the second scrubbing solution 341 is led from the second stage 340 to a heat exchanger 345, after which the cooled second scrubbing solution 342 is led to the second stage 340.
  • the second scrubbing solution is sprayed onto the shifted synthesis gas to scrubb the shifted synthesis gas.
  • the second scrubbing solution is essentially in liquid form to ensure scrubbing.
  • the circulation of the second scrubbing solution may be enabled with a pump (not shown in the figure).
  • the second scrubbing solution comprises water.
  • the second scrubbing solution may consist of water or it may consist essentially of water.
  • the first scrubbing solution may be used as the second scrubbing solution.
  • heat is recovered from the second scrubbing solution.
  • a cool heat transfer medium 346 is fed to the heat exchanger 345 where it heats to a heated heat transfer medium 347.
  • the heat transfer medium may comprise water.
  • the temperature of the heated heat transfer medium 347 may be e.g. 60 ⁇ .
  • Condensate 350 is treated as liquid waste and fed to a waste water treatment plant.
  • the condensate 350 comprises the quenching liquid 215.
  • In the scrubber 320 shifted synthesis gas is scrubbed to scrubbed synthesis gas.
  • the scrubbed synthesis gas is led to an acid gas removal step 385.
  • the scrubbed synthesis gas is purified in an acid gas removal unit, which is a physical wash processing unit such as Rectisol®, Purisol®, or Selexol®.
  • the acid gas removal step 385 produces product gas 400 and a tail gas 397.
  • the tail gas 397 comprises CO 2 .
  • the tail gas 397 consists essentially of CO 2 , and the tail gas 397 is used as the carbon dioxide 120 (cf. Fig. 3a).
  • a part 380 of the scrubbed synthesis gas is circulated in the process to cool the synthesis gas 200 or quenched synthesis gas before the filtration unit 220 to obtain the filterable synthesis gas.
  • the scrubbed synthesis gas is divided to a first part 390 and to a second part 380.
  • the first part 390 is compressed and conveyed to the acid gas removal step to produce product gas 400.
  • the second part 380 is recycled to the process and used as the recycled gas 205 (c.f. Fig. 3b).
  • the tail gas 397 from the acid gas removal step 385 may be used as the recycled gas 205.
  • the product gas 400 is further conveyed to a Fischer-Tropsch synthesis process for producing product fluid 396 and FT tail gases 395 from the product gas 400.
  • the Fischer-Tropsch synthesis process is denoted by "FT" in Fig. 3c.
  • the product fluid 396 comprises liquid, and waxy compounds.
  • Heat is recovered from FT processing unit with a heat exchanger 386.
  • the heat exchanger 386 is arranged in connection with the FT processing unit, is arranged to cool the FT processing unit, and is arranged to recover heat from the FT processing unit.
  • the heat is recovered to a heat transfer liquid, such as water 398, which is fed to the heat exchanger 386.
  • the steam 399 may be used in preceding process steps.
  • the steam 399 may be used in at least one of following: the gasification reactor 150 as the steam 142, the reformer 240 as the steam 232, and the gas shifter 310 as steam 259.
  • the product fluid 396 is further upgraded in an upgrading unit to produce biofuel.
  • FT tail gas 395 is obtained from the FT process.
  • the tail gas may comprise CO, H 2 and light hydrocarbons, e.g. methane.
  • the FT tail gas 395 may be recycled to the process, as the recycled gas 205, or to the gasifier 150, as will be discussed later.
  • the product fluid 396 is upgraded to produce biofuel and off gas 410.
  • the upgrading process comprises hydrocracking of product fluid 396 and fractionated distillation to obtain liquid biofuels such as at least one of biodiesel and kerosene.
  • the formed waxy-compounds, i.e. FT-wax are hydrocracked into middle distillates.
  • the hydrocracking process produces also light end hydrocarbons which are considered as the off gas 410, which also contains unconverted hydrogen.
  • the off gas 410 may also be recycled to the process as the recycled gas 205 and /or to the gasifier 150. (not shown in the figure).
  • Fig. 4a shows some parts of a process for producing liquid fuel from biomass.
  • the synthesis gas is cooled to filterable synthesis gas only by gas cooling using recycled gases 205.
  • the recycled gases comprise gases from the scrubber 320.
  • the FT tail gases 395 may be recycled to the gasifier 150. Alternatively or in addition, the FT tail gas 395 may be used for synthesis gas cooling. These possibilities are illustrated with the dotted lines near the symbol 395 in Fig. 4a.
  • the tail gas 397 from the acid gas removal step 385 may be recycled as the CO2 used the containers 106 and 108 for the biomass. Even if not shown in the figure, the tail gas 397 may, alternatively or in addition, be used to cool the synthesis gas.
  • the off gas 410 may be recycled to the gasifier 150, or used to cool the synthesis gas. If gases 395, 397, 410 are used to cool the synthesis gas, they may be mixed with the synthesis gas 200, or with other recycled gas 205, including the other of these gases 395, 397 and 410. Feeding of biomass and gasification are not shown in detail in Fig. 4a, as they are described in detail above. However, process steps between cooling of synthesis gases and FT, and recycling of different gases is shown in more detail.
  • synthesis gas 200 is cooled at the point 212, where the synthesis gas is mixed with the recycled gas 205.
  • a part 380 of the scrubbed synthesis gas is used as the recycled gas 205.
  • all or part of the tail gases 395 and 397 and the off gas 410 may be used as the recycled gas 205 (not shown for the tail gas 397 or the off gas 410).
  • the recycled gas 205 comprises scrubbed synthesis gas, and may further comprise at least one of the FT tail gas 395, the acid gas removal tail gas 397, and the off gas 410.
  • the 4a comprises piping for conveying the recycled gas 205 from the scrubber 320 to the synthesis gas before it enters the filtering unit 220.
  • the system may also comprise piping for conveying recycled gas 205 (i.e. the FT tail gas 395) from the FT processing unit to the synthesis gas.
  • the system may also comprise piping for conveying recycled gas 205 (i.e. the acid gas removal tail gas 397) from the acid gas removal unit to the synthesis gas.
  • the system may also comprise piping for conveying the recycled gas 205 (i.e. the off gas 410) from the upgrading unit to the synthesis gas.
  • the circulation of recycled gas is ensured with at least one booster compressor (not shown in the figure).
  • High pressure steam is produced from water in the heat exchanger 250. This high pressure steam is used to generate power.
  • steam 399 is produced in the heat exchanger 386 arranged to cool the FT reactor. Steam 399 may be used in at least one of: the gasification reactor 150, the reformer 240, and the gas shifter 310.
  • Heat from the scrubber 320 is used to dry biomass in a dryer 450. Heat is transferred to the dryer 450 by conveying the heated heat transfer medium 337 to the dryer 450.
  • Fig. 4b shows some parts of an embodiment of the invention, as described above.
  • synthesis gas 200 is quenched in the quencher 210 before the filtration unit 220.
  • demineralized water is used as the quenching liquid 215.
  • quenched synthesis gas is further cooled by mixing quenched synthesis gas with recycled gas 205 at the point 212.
  • Recycled gas 205 comprises a part of scrubbed synthesis gas 380 and may comprise at least one of FT tail gas 395, acid gas removal tail gas 397, and off gas 410.
  • Fig. 4c shows another embodiment of the invention. Compared to Fig.
  • synthesis gas 200 and recycled gas 205 are mixed before the quencher 210 at the point 212. This may be done e.g. to reduce the temperature of the quencher 210.
  • the gas flow in the quencher 210 is increased, as compared to the embodiment of Fig. 4b.
  • the turbulence of the flow in the quencher 210 may be increased, and the quenching liquid 215 may be evaporated more rapidly in the quencher.
  • Figs. 4a-4c may comprise multiple points 212 for mixing recycled gas and synthesis gas.
  • the different components of the recycled gas 205 the scrubbed synthesis gas, the tail gases 395, 397, and the off gas 410; may be mixed with the synthesis gas 200 in the same or in different locations.
  • Fig. 4d shows another embodiment of the invention.
  • a quencher 210 is used to quench the synthesis gas.
  • the scrubbed synthesis gas is not recycled in the process to cool the synthesis gas. Therefore, in this embodiment, essentially all scrubbed synthesis gas is conveyed to compression and acid gas removal processes to produce the product gas.
  • At least one of the tail gas 395 from the FT process, the tail gas 397 from the acid gas removal step, and the off gas 410 may be recycled as recycled gas 205.
  • the amount of quenching water 215 is selected such that the synthesis gas cools enough for filtration purposes in the quencher 210. This has some beneficial effects in the process and the process equipment, as will be discussed below.
  • the target temperature of the filterable synthesis gas may be 650 .
  • the mass flow of the recycled synthesis gas, where the recycled synthesis gas consists of scrubbed synthesis gas with the temperature 20 should be approximately 30% of th e mass flow of the uncooled synthesis gas.
  • the mass flow of the recycled synthesis gas, where the recycled synthesis gas consists of CO 2 e.g.
  • the tail gas 397 from the acid gas removal step with the temperature 20 "C should be approximately 50% of the mass flow of the uncooled synthesis gas.
  • the mass flow of the water should be approximately only 8% of the mass flow of the uncooled synthesis gas.
  • the gas has to be heated up to reformer operation temperature by partial combustion of synthesis gas with oxygen. Due to the effect described above, the heat duty to be fulfilled in the reformer in the case of a water quench is much lower compared to a gas cooled synthesis gas. The effect may even be larger, if the steam feed to the reformer can be decreased (since it is replaced by quench water steam).
  • the heat load to the heat exchanger 250 is smaller. For that less high pressure steam is produced. This is shown in the Figs. 4b - 4e as "less steam" near the heat exchanger 250.
  • the advantage is that the size of the heat exchanger 250 can be smaller.
  • piping from the scrubber 320 to the filtration unit 220 and the booster compressor for the recycled gas 205 are not needed. Essentially all scrubbed synthesis gas is conveyed to compression and acid gas removal processes to produce the product gas. Therefore, the system of Fig. 4d or 4e does not comprise means for recycling scrubbed synthesis gas in the process.
  • the recycled gases 205 are free scrubbed synthesis gas.
  • the recycled gas 205 consist at least one of the FT tail gas 396, the acid gas removal tail gas 397 and the off gas 410. Furthermore, the recycled gases are recycled to the process to or before the gasifier 150.
  • Fig. 4e shows the embodiment of Fig 4d, where the FT tail gas 395 is recycled to the gasifier 150, and the acid gas removal tail gas 397 is recycled to the process as the CO 2 used in the lock hopper.
  • the off gas 410 may be recycled to the gasifier 150.
  • the system comprises means for conveying FT tail gas from the Fischer-Tropsch processing unit to the gasifier 150.
  • the system further comprises means for conveying the tail gases 397 from the acid gas removal step to a container containing the biomass. In addition to the container 106 in the lock hopper, the tail gas can be conveyed to another container.
  • the tail gas 397 consists essentially of CO 2 .
  • the system comprises means for conveying the off gas 410 from the upgrading unit to the gasifier 150. Also in the other embodiments shown in Figs. 4a-4d, the FT tail gas and/or the off gas 410 may be recycled to the gasifier 150, and the tail gases 397 may be recycled to the lock hopper. This embodiment has essentially the same advantages as the embodiment of Fig. 4d.
  • Quenching produces steam that is comprised in the quenched synthesis gases.
  • all the steam needed in the reforming process is comprised in the quenched synthesis gases, and therefore also in the filtered synthesis gases.
  • the filtered synthesis gases are reformed with only oxygen 230.
  • All the needed steam is comprised in the filtered synthesis gas and no excess steam 232 (Fig. 3b and Figs. 4a- 4c) is needed.
  • the excess steam 232 can be used also to smoothen the hot spots in the reformer, as generated by the oxygen injection.
  • Figs. 5a - 5c three embodiments are shown in Figs. 5a - 5c.
  • the quenching liquid 215 is evaporated in the quencher 210. Therefore, the size of the droplet in the quenching spray needs to be reasonably small.
  • the flow of the quenching liquid into the quencher should be small enough such that essentially all the liquid becomes evaporated.
  • the flow of the quenching liquid should be kept small also in order not to excessively cool the synthesis gas before the reformer 240, as the temperature of the cooled synthesis gas in the reformer 240 should be high.
  • the flow of the quenching liquid should be large enough to facilitate the required cooling.
  • the pressure of the synthesis gas 200 arriving into the quencher 210 may be essentially the same as the pressure in the gasification reactor 150, i.e. for example approximately 10 bar(a).
  • the volumetric flow of the quenching liquid is defined by the flow velocity of the quenching liquid, and the cross sectional area of the conduit wherein the quenching liquid is arranged to flow.
  • the flow, i.e. mass flow, of the quenching liquid is defined by the density of the quenching liquid and the volumetric flow. The density is affected e.g. by the temperature of the quenching liquid. As the bulk modulus of a liquid is large (e.g. compared to the bulk modulus of a gas), density of the quenching liquid generally is practically independent on pressure.
  • the flow velocity and pressure of the quenching liquid 215 are controlled with a pump 515.
  • the quencher 210 comprises nozzles 510 for spraying the quenching liquid 215 to the quencher 210.
  • the droplet size of the sprayed quenching liquid may depend on the quenching liquid 215, the pressure of the quenching liquid 215 and the nozzle 510.
  • water was used as the quenching liquid 215.
  • the pressure with which the liquid 215 is sprayed may be of the order of 20 - 40 bar.
  • a suitable amount of quenching liquid is about 5 m-% of the synthesis gas flow to the quencher 210.
  • the temperature of the synthesis gas was decreased from about 850 ⁇ to about 700 ⁇ .
  • Fu rthermore all the water used for quenching was evaporated in the quencher 210.
  • a suitable ratio of the mass flow of the quenching liquid 215 to the mass flow of the synthesis gas before quenching depends on the amount of recycled gas in the process.
  • a suitable ratio of the mass flow of the quenching liquid 215 to the mass flow of the synthesis gas before quenching may be in the range of 4 - 15 %, depending on the needed temperature decrease of the synthesis gas.
  • the quenched synthesis gas may be cooled by mixing it with recycled gas.
  • the temperature of the filterable synthesis gas depends on the filtering unit, and may be from 600 to 800 ⁇ .
  • the temperature of the synthesis gas before quenching may be from 800 to 900 ⁇ .
  • the temperature and mass flow of the synthesis gas 200 before the quencher 210 may vary significantly. The variation may be due to the variation in the amount of synthesis gas produced in the gasification reactor 150.
  • the flow of recycled gas 205 affects the temperature and mass flow of gases in the quencher 210.
  • the amount of quenching liquid (water) 215 depends on the temperature requirement of the filtration unit 220, and on the amount of recycled gas 205, as mixed with the quenched synthesis gas.
  • the amount of quenching liquid is defined, to a reasonable accuracy, by the flow velocity, as discussed above.
  • the system may comprise one or more sensors arranged to measure at least one value of at least one process variable.
  • the process variable may be one of temperature, pressure, flow velocity, and composition.
  • a value of the process variable may be measured from the synthesis gas.
  • the value may be measured before or after the quencher 210.
  • the value may be measured before or after the point 212, where the synthesis gas is mixed with the recycled gas 205. In case the synthesis gas is cooled both by quenching and by gas cooling, the value may be measured before or after both of these locations or in between these locations.
  • the system may comprise a temperature sensor 530 to measure the temperature of the synthesis gas entering the quencher 210.
  • the system may comprise a flow velocity sensor 532 to measure the flow velocity of the synthesis gas entering the quencher 210.
  • the system may comprise a pressure sensor to measure the pressure of the synthesis gas entering the quencher 210.
  • the system may comprise a composition sensor 534 to analyze the composition of the synthesis gas entering the quencher 210. Information on the composition is needed, if accurate information on the heat capacity of the synthesis gas entering the quencher 210 is needed.
  • the sensor(s) is/are arranged to send the measured value(s) of at least one process variable to a controller 535.
  • the value(s) may be used to deduce information indicative of the thermal flow and/or heat capacity flow of the synthesis gas in the quencher.
  • the controller 535 may be arranged to control the pump 515. Moreover, by controlling the pump 515, the controller may be arranged to control at least one process parameter.
  • the process parameter may be the pressure of the quenching liquid 215 or the flow velocity of the quenching liquid 215.
  • the controller 535 may be arranged to use the information on at least one process variable to control at least one of process parameter.
  • the controller may e.g. calculate another flow velocity for the quenching liquid based on the information indicative of the thermal flow of the synthesis gas. The controller may use this calculated flow velocity to control the actual flow velocity of the quenching liquid.
  • a reliable and accurate temperature control is crucial to protect the filtering unit 220.
  • the shape of the quencher may comprise a cylindrical part.
  • the nozzles 510 may be arranged close to the central axis of the cylindrical part, as shown in Fig. 5a.
  • the nozzles are further arranged to an upper part of the quencher 210, and the nozzles spray the quenching liquid 215 downwards towards the lower part of the quencher.
  • the nozzles 510 are thus arranged to spray the liquid 215 parallel to the central axis of the cylindrical part.
  • the nozzles 510 may also be arranged to spray the liquid 215 essentially parallel to the direction of the flow of the synthesis gas 200 in the quencher 210. This direction is depicted with the arrow 520.
  • the quenching liquid 215 may also be sprayed essentially perpendicular to the direction of the synthesis gas flow 520.
  • the nozzles 510 may be located near the walls of the quencher 210 and arranged to spray the liquid 215 towards the central axis of the quencher 210.
  • At least one sensor is arranged to measure at least one value of at least one process variable form the synthesis gas flow leaving the quencher 210. This may simplify the control, since the synthesis gas may be quenched to reduce the temperature to a level that the filtering unit can withstand. Alternatively, the synthesis gas may be quenched to a higher temperature, and later cooled by mixing with recycled gas 205 to a level that the filtering unit can withstand.
  • a sensor is arranged to measure the temperature of the synthesis gas flow leaving the quencher 210 and arranged to send the measured information to the controller 535.
  • the controller 535 is arranged to use the information on the temperature to control the flow velocity of the quenching liquid 215.
  • the controller 535 may e.g. increase the flow velocity of the quenching liquid 215 if the measured temperature of the quenched synthesis gas is too high.
  • the controller may decrease the flow velocity of the quenching liquid 215 if the measured temperature of the quenched synthesis gas is too low.
  • This control mechanism is independent of the composition and heat capacity of the synthesis gas entering the quencher 210. Additional online analysis as for the cases depicted in Fig. 5a and 5b is not required.
  • a sensor/sensors may be arranged to measure at least one value of at least one process variable, wherein the process variable is one of the temperature, the flow velocity, the pressure, and the composition of the filterable synthesis gas, i.e. synthesis gas after mixing the recycled gas to the synthesis gas.
  • the sensor/sensors may send the measured information to a controller 535 arranged to control at least one process parameter, wherein the process parameter is one of
  • the system may comprise such sensors.
  • the temperature of the filterable synthesis gas may be controlled by controlling the mass flow of the recycled gas 205.
  • the temperature of the filterable synthesis gas may be controlled by at least one of the mass flow of the recycled gas 205 and the flow velocity of the quenching liquid 215.
  • the embodiments described above may be used for producing liquid fuel from solid biomass.
  • the overall process yield, stability and robustness is enhanced by filtering synthesis gas before reforming. Filtration is enabled by cooling the synthesis gas. Synthesis gas could be cooled by mixing with recycled gas and/or by quenching.
  • the embodiments described in detail how the amount of energy required for heating the synthesis gas to achieve reformer operating temperature could be reduced.
  • the embodiments described in detail what other surprising beneficial effect water quenching has in the overall process. In comparison to gas cooling, water quenching is characterized by lower oxygen consumption in the reformer, a smaller size of the heat exchanger 250, increased capacity for medium pressure steam production, increased capacity for heat production for drying biomass and increased liquid product yield. Still further, since water- quenching the synthesis gas leads to lower volumetric and mass flows, some of the piping and equipment may be decreased in size or totally omitted, which reduces the overall investment costs of such a system.

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PCT/FI2012/051085 2011-11-09 2012-11-06 A method and a system for producing liquid fuel from biomass Ceased WO2013068643A1 (en)

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KR20190106798A (ko) * 2018-03-09 2019-09-18 보르지크 게엠베하 퀀칭 시스템
WO2021185827A1 (en) * 2020-03-17 2021-09-23 Velocys Technologies Limited Process for the manufacture of a useful product from waste materials and/or biomass

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KR102309356B1 (ko) * 2015-03-24 2021-10-06 구씽 리뉴어블 에너지 인터내셔널 홀딩 게엠베하 고온 합성 가스를 냉각시키기 위한 방법
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JP2018509520A (ja) * 2015-03-24 2018-04-05 グッシング リニューアブル エナジー インターナショナル ホールディング ゲーエムベーハー 高温の合成ガスを冷却する方法
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WO2021185827A1 (en) * 2020-03-17 2021-09-23 Velocys Technologies Limited Process for the manufacture of a useful product from waste materials and/or biomass
US11578281B2 (en) 2020-03-17 2023-02-14 Velocys Technologies Ltd Method for producing a saleable product from synthesis gas derived from and/or comprising waste material and/or biomass
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US20230174878A1 (en) * 2020-03-17 2023-06-08 Velocys Technologies Limited Process for the manufacture of a useful product from waste materials and/or biomass
US11873458B2 (en) 2020-03-17 2024-01-16 Velocys Technologies Ltd Process
US12129439B2 (en) * 2020-03-17 2024-10-29 Velocys Technologies Limited Process for the manufacture of a useful product from waste materials and/or biomass

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