Classifications

• • C—CHEMISTRY; METALLURGY
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F1/00—Treatment of water, waste water, or sewage
  • C02F1/02—Treatment of water, waste water, or sewage by heating
  • C02F1/025—Thermal hydrolysis
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  • 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
  • C01B3/40—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 characterised by the catalyst
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/005—Spinels
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
  • B01J23/74—Iron group metals
  • B01J23/755—Nickel
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
  • B01J37/02—Impregnation, coating or precipitation
  • B01J37/03—Precipitation; Co-precipitation
  • B01J37/038—Precipitation; Co-precipitation to form slurries or suspensions, e.g. a washcoat
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  • 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
  • C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
  • C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
  • C01B3/16—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts
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  • 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
  • C01B3/323—Catalytic reaction of gaseous or liquid organic compounds other than hydrocarbons with gasifying agents
  • C01B3/326—Catalytic reaction of gaseous or liquid organic compounds other than hydrocarbons with gasifying agents characterised by the catalyst
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
  • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
  • C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
• • 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
  • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
  • C10G3/42—Catalytic treatment
  • C10G3/44—Catalytic treatment characterised by the catalyst used
  • C10G3/45—Catalytic treatment characterised by the catalyst used containing iron group metals or compounds thereof
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  • 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
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  • 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
  • C01B2203/06—Integration with other chemical processes
  • C01B2203/062—Hydrocarbon production, e.g. Fischer-Tropsch 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
  • C01B2203/10—Catalysts for performing the hydrogen forming reactions
  • C01B2203/1041—Composition of the catalyst
  • C01B2203/1047—Group VIII metal catalysts
  • C01B2203/1052—Nickel or cobalt catalysts
• • 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
  • C01B2203/10—Catalysts for performing the hydrogen forming reactions
  • C01B2203/1041—Composition of the catalyst
  • C01B2203/1082—Composition of support materials
• • 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
  • C01B2203/1205—Composition of the feed
  • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
• • 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
  • C01B2203/1205—Composition of the feed
  • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
  • C01B2203/1217—Alcohols
• • 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
  • C01B2203/1205—Composition of the feed
  • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
  • C01B2203/1217—Alcohols
  • C01B2203/1223—Methanol
• • 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
  • C01B2203/1205—Composition of the feed
  • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
  • C01B2203/1235—Hydrocarbons
• • 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
  • C01B2203/148—Details of the flowsheet involving a recycle stream to the feed of the process for making hydrogen or synthesis gas
• • C—CHEMISTRY; METALLURGY
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F2101/00—Nature of the contaminant
  • C02F2101/30—Organic compounds
  • C02F2101/34—Organic compounds containing oxygen
• • C—CHEMISTRY; METALLURGY
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
  • C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
  • C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
  • C02F2103/365—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds from petrochemical industry (e.g. refineries)
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
  • C10G2300/10—Feedstock materials
  • C10G2300/1011—Biomass
  • C10G2300/1014—Biomass of vegetal origin
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
  • C10J2300/00—Details of gasification processes
  • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
  • C10J2300/169—Integration of gasification processes with another plant or parts within the plant with water treatments
• • 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
  • Y02P20/50—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
  • 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 application relates to a method defined in claim 1 and an apparatus defined in claim 14 for treating a side water fraction. Further, the applica tion relates to a use of the method defined in claim 16.
• thermochemical routes such as by a gasification and Fischer-Tropsch (FT) reaction. Also different side fractions form in these processes.
• FT Fischer-Tropsch
• APR aqueous-phase reforming
• APR aqueous-phase reforming
• catalysts mainly platinum- and nickel-based in form of parti cles.
• These catalysts have been prepared with differ ent supports and metal dopants to enhance the perfor mance of the catalysts.
• product selectivity and durability of the catalysts are questionable.
• Fur thermore few reactor designs have been tested for APR, with a predominant use of tubular packed-bed re actors.
• intensified reactors have been con sidered to improve mass transport in APR, and conse- quently, increase the product efficiency.
• platinum-washcoated microchannels and membrane reac- tors enhance the performance
• catalyst loading and re placement are significant barriers for scale up appli cations.
• noble metal-based catalysts are ex pensive and economically inefficient in large scales.
• the objective is to disclose a new type meth od and apparatus for treating water fractions derived from biorefineries. Further, the objective is to dis close a new type method and apparatus for producing hydrogen from the aqueous solutions derived from bio refineries. Further, the objective is to disclose an improved method and apparatus for treating water frac tions in an aqueous-phase reforming. Further, the ob jective is to produce a new type catalyst to be used in the aqueous-phase reforming. Further, the objective is to prepare a new type catalyst. Further, the objec tive is to disclose a catalyst composition for coating a substrate.
• Fig. 1 is a flow chart illustration of a method and an apparatus according to one embodiment
• Fig. 2 shows results from one example carried out according to one method embodiment.
• the side water fraction (1) comprising at least one undesired organic compound is treated by means of a reforming treatment (2) in order to con vert the organic compound into at least hydrogen (5) and optionally also other compounds (6) selected from the group comprising organic compounds, such as modi fied organic compounds, hydrocarbons, carbondioxide, carbonmonoxide and their combinations, and the reform ing treatment (2) is catalyzed by Ni/NiAl 2 0 4 catalyst (3), preferably Ni/NiAl 2 0 4 washcoat catalyst.
• An apparatus for treating a side water frac tion (1) which comprises at least one undesired com pound and which is formed in a thermochemical treat ment of biomass can comprise at least one reforming treatment device (12) in which the side water fraction (1) comprising at least one undesired organic compound is treated in order to convert the organic compound into at least hydrogen (5) and optionally also other compounds (6) selected from the group comprising or ganic compounds, such as modified organic compounds, hydrocarbons, carbondioxide, carbonmonoxide and their combinations, and Ni/NiAl 2 0 4 catalyst (3) , preferably Ni/NiAl 2 0 4 washcoat catalyst, which is arranged inside the reforming treatment device (12) for catalyzing the reforming treatment (2) .
• FIG. 1 One embodiment of the method and the apparatus is shown in Fig 1.
• the biomass means any bio mass.
• the biomass is a lignocellu- losic based biomass.
• the biomass has been treated by converting into biofuels.
• the biomass may be converted into the biofuels by thermochemical routes such as by a gasification and Fischer-Tropsch (FT) reaction of syngas or other feedstock, or by a pyrolysis and bio-oil reforming.
• the biomass has been treated by means of at least one process step which is selected from the group compris ing the gasification, Fischer-Tropsch (FT) reaction of syngas, pyrolysis, bio-oil refining and their combina tions.
• FT Fischer-Tropsch
• the biomass has been treated by means of the gasification and/or the Fischer- Tropsch (FT) reaction of syngas. In one embodiment, the biomass has been treated by means of the pyrolysis and/or the bio-oil refining. In one embodiment, the side water fraction (1) is formed in the Fischer- Tropsch reaction or in the bio-oil refining.
• FT Fischer- Tropsch
• the side water fraction (1) means any water fraction, biorefinery water fraction, water based side fraction or water based residue frac tion, in which fraction may be any fraction, separated fraction, flow, stream, outflow or their combination.
• the side water fraction may comprise at least one harmful organic compound, such as hydrocarbon, oxygen ated hydrocarbon or other organic compound or the like, for example alcohols, aldehydes, ketones, acids, aliphatic, aromatic and cyclic hydrocarbons.
• the side water fraction comprises at least one organic compound, e.g. MeOH, organic compound with longer carbon chain or other compound. In one embodi ment, the side water fraction comprises at least MeOH.
• the side water fraction comprises organic compound with longer carbon chain, such as al cohol, ketone, aldehyde and/or organic acid.
• the side water fraction comprises 1 - 40 % by volume organic compounds, e.g. organic hydrocarbons or other organic compounds.
• the side water fraction comprises over 5 % by volume, preferably 5 - 40 % by volume, more preferably 5 - 20 % by volume, organic compounds.
• the side water fraction comprises 1 - 10 % by volume or ganic compounds.
• the Ni/NiAl 2 0 4 catalyst (3) is arranged in the form of a film, preferably a thin film, onto a substrate.
• the substrate can be formed from a metal material or a ceramic material or other suitable material.
• the substrate can be a wall, reactor wall, static mixer, mesh, fi bres, fillers or other suitable substrate which are formed from the metal or ceramic material, or for ex ample, open cell foams which are formed from the ce ramic material.
• the Ni/NiAl 2 0 4 catalyst is Ni/NiAl 2 0 4 washcoat catalyst, more preferably Ni/NiAl 2 0 4 spinel washcoat catalyst, wherein the Ni/NiAl 2 0 4 is as a thin washcoat layer on the substrate, such as on the metal or ceramic surface of the substrate.
• the washcoat catalyst can be formed by preparing a catalytically active washcoat composition from a carrier material, preferably with a high surface area, e.g. aluminium oxide based carrier material, and one or more catalyst agents, e.g. met als, and by arranging the formed catalytically active washcoat composition onto the substrate, such as the metal or ceramic structure.
• a carrier material preferably with a high surface area, e.g. aluminium oxide based carrier material, and one or more catalyst agents, e.g. met als, and by arranging the formed catalytically active washcoat composition onto the substrate, such as the metal or ceramic structure.
• Ni content of the Ni/NiAl 2 0 4 catalyst (3) is 8 - 20 wt%. In one embodi ment, Ni content of the Ni/NiAl 2 0 4 catalyst is 8 - 15 wt%, in one embodiment 10 - 14 wt%, and in one embodi ment about 11 - 13 wt%.
• the Ni/NiAl 2 0 4 catalyst (3) is prepared such that a catalyst agent, e.g. Ni, is impregnated, e.g. by an incipient wetness impregnation method, to a carrier material, e.g. boehmite, to form a catalytic material.
• a catalyst agent e.g. Ni
• Ni catalyst agent can be a Ni- precursor such as nickel nitrate or other precursor.
• the resulting catalytic material e.g. in form of pow der, is dried and calcined, for example to transform nickel nitrate/boehmite into nickel oxide/boehmite .
• a slurry is prepared.
• the slurry is prepared by mixing the resulting catalytic material with a binder, an acid and water.
• the slurry is ar ranged by washcoating onto a substrate, such as a met al or ceramic substrate, and the washcoated substrate is thermally treated, e.g. by means of a high tempera ture calcination. Then a thin layer of Ni/NiAl 2 0 4 can be formed onto the substrate.
• the Ni/NiAl 2 0 4 catalyst (3) is prepared such that Ni-precursors are impregnated into a boehmite carrier material to form a catalytic material, and the catalytic material, preferably in a powder form, is dried and calcinated, and a slurry comprising at least the catalytic material, and pref erably at least suitable liquid, is prepared and stirred, and the substrate is washcoated with the slurry, and the washcoated substrate is thermally treated, such as dried, calcinated and treated by re duction.
• the catalytic material is dried by means of under pressure or vacuum drying or their combination. In one embodiment, the catalytic material is dried under vacuum.
• the catalytic material is calcinated at a temperature of 450 - 550 °C, preferably at 490 - 510 °C.
• Ni-precursor can be converted, e.g. from nickel nitrate to nickel oxide.
• the slurry comprises at least the catalytic material and water, preferably ion-exchanged water. Further, the slurry may comprise a suitable solution and acid, such as HN0 3 , and a binder.
• the sub strate is pre-treated and calcinated before the wash coating.
• the formed washcoated sub strate is dried at a temperature of 400 - 600 °C, preferably 450 - 550 °C, for a sufficient time, e.g. about 3 - 7 min, such as about 5 min.
• the washcoated substrate is slowly dried by air flow at ambient temperature and pressure before the above flash-drying.
• the washcoated substrate is calcinated at a temperature of 700 - 900 °C, preferably 750 - 850 °C, for a sufficient time, e.g. about 1.5 - 2.5 hours, such as about 2 hours, to fix the catalytic material on the substrate.
• the formed washcoat catalyst is treated by reduction at a temperature of 350 - 450 °C, preferably 370 - 430 °C, with a sufficient H2:N2 ratio.
• H2:N2 ratio can be about 1.
• the reforming treatment (2) is a 3-phase reforming treatment.
• the reforming treatment (2) is an aqueous-phase reforming (APR) .
• the aqueous-phase reforming (APR) is carried out at temperature which is 200 - 250 °C, preferably about 230 °C, and under pres sure which is 30 - 34 bar, preferably 32 bar.
• an aqueous solution which comprises 0.1 - 10 wt%, preferably 3 - 7 wt%, organic compounds and which is formed from the side water fraction (1) is fed to the aqueous-phase reforming (APR) .
• the side water fraction (1) is diluted with water before the feeding to the aqueous-phase reform ing (APR) .
• APR aqueous-phase reform ing
• the aqueous-phase reform ing means any aqueous-phase reforming, catalytic aque ous-phase reforming or the like.
• At least hy drogen (5) and optionally some other compounds (6), such as organic compounds, hydrocarbons, carbondioxide and/or carbonmonoxide are formed.
• at least hydrogen (5) is formed.
• car- bondioxide and carbonmonoxide can be formed during the reforming treatment (2) .
• hydrogen and carbondioxide are formed.
• also some hydrocarbons, e.g. methane, ethane or other hy drocarbon can be formed during the reforming treat ment (2) .
• methane is formed.
• also some organic compounds e.g.
• the reforming treatment products can be formed during the reforming treat ment (2) .
• at least a part of the reforming treatment products are gaseous products.
• at least a part of the reforming treatment products are liquid products.
• the reforming treatment products are mainly gas eous products.
• the reforming treat ment products are mainly liquid products.
• the gaseous reforming treatment products can comprise at least CO, C0 2 , CH 4 , C 2 H 6 , C 2 H 4 and/or C 3 H 6 .
• the liquid reforming treatment products can comprise alcohol, ketones, aldehydes and/or organic acids.
• the method comprises more than one reforming treatment step or device (12), such as aqueous-phase reforming (APR) step or reactor.
• the apparatus comprises more than one reforming treatment device (12), such as aqueous-phase reforming reactor.
• the hydrogen (5) is fed back to the thermochemical treatment, e.g. to the Fischer-Tropsch (FT) unit, to adjust H 2 /CO ratio.
• the hydrogen (5) is fed back to the bio-oil refining unit for hydrotreatment, e.g. to im prove hydrotreatment of pyrolysis oils, e.g. hydro genation, hydrodeoxygenation or the like.
• the apparatus comprises at least one feed inlet for supplying the side water fraction (1) to the reforming treatment device (12) .
• the feed inlet of the side water fraction may be any suitable inlet known per se, e.g. pipe, port or the like.
• the apparatus comprises at least one feeding device.
• the feeding device can be any feeding device, equipment or other suitable device for feeding the side water fraction (1) to the reforming treatment device (12) .
• the feeding device is selected from the group comprising pump, compressor, tube, pipe, other suitable feeding device and their combinations.
• the apparatus comprises at least one addi- tion device for adding the catalyst (3) to the reform ing treatment device (12) .
• the addition device may be any suitable addition device.
• the apparatus comprises at least one product outlet for supplying hydrogen (5) or other compound stream (6), such as organic compound, hydrocarbons, carbondioxide and/or carbonmonoxide stream or product out from the reforming treatment device (12) .
• the product outlet may be any suitable outlet known per se, e.g. pipe, outlet port or the like.
• Any suitable reforming treat- ment device (12), e.g. aqueous-phase reforming reac tor, known per se can be used as the reforming device in the apparatus .
• the reforming treatment device (12) is an aqueous-phase reforming reactor.
• the apparatus comprises more than one reforming treatment devices (12) . In one embodiment, at least two reforming treatment devices are arranged in parallel. In one embodiment, at least two reforming treatment devices are arranged sequen tially. In one embodiment, the method is based on a continuous process. In one embodiment, the apparatus is a continuous apparatus. In one embodiment, the method is based on a batch process. In one embodiment, the apparatus is a batch apparatus.
• the apparatus and the method is used and utilized in the aqueous-phase re forming, in the production of biofuels, in the treat ment of the side water fraction after a Fischer- Tropsch (FT) reaction, in the treatment of the side water fraction after bio-oil refining, in the treat ment of the side water fraction after pyrolysis and/or its post-process, in the treatment of the water frac tion comprising at least organic compound, or their combinations .
• FT Fischer- Tropsch
• the different water based streams with harmful organic compounds can be treated effectively.
• High conversion rates and hydro gen selectivity can be obtained when the reforming treatment, such as the aqueous-phase reforming, is catalyzed with Ni/NiAl 2 0 4 catalyst.
• the performance of this catalyst is remarkably superior compared to nick el-based catalysts in a packed-bed tubular reactor.
• the improvement derives from the high activity of the catalyst and the reduction of the internal mass trans fer limitations. Further, this catalyst represents a much less expensive alternative to the traditionally used platinum-based catalysts.
• the method and apparatus offers a possibility to treat different water based side and residue streams easily, and energy- and cost-effectively.
• the present invention provides an industrially applicable, simple and affordable way to treat the water based streams.
• the water based streams can be treated under mild conditions, such as at low temperature and under medium pressure. Further, no evaporation stages are needed.
• the method and apparatus are easy and simple to realize in connection with production processes of biofuels, also in a small scale process. Then more en vironmentally friendly biofuel production process can be provided. Further, the biofuel production process can be optimized by utilizing the hydrogen produced in the reforming treatment device. Further, an amount of waste water for disposal can be decreased.
• Figure 1 presents the method and also the ap paratus for treating a side water fraction (1) derived from a biorefinery.
• the side water fraction (1) has been formed in a thermochemical treatment of lignocellulosic based biomass.
• the lignocellulosic based biomass can be treated by converting into the biofuels by means of the thermochemical routes such as by a gasification and Fischer-Tropsch (FT) reaction of syngas or other feedstock, or by a pyrolysis and bio-oil reforming.
• the side water fraction (1) has been formed in the Fischer-Tropsch reaction or in the bio-oil refining.
• the side water fraction (1) comprises at least one undesired organic compound.
• the side water fraction (1) may comprise 1 - 40 % by volume organic compounds.
• the apparatus comprises at least one re forming treatment device (12), in this embodiment an aqueous-phase reforming (APR) reactor, in which the side water fraction (1) is treated by a reforming treatment (2) in order to convert the organic compound into at least hydrogen (5) and optionally also other compounds (6), such as organic compounds, hydrocar bons, carbondioxide and/or carbonmonoxide .
• the method and apparatus comprise Ni/NiAl 2 0 4 catalyst (3) , preferably Ni/NiAl 2 0 4 spinel washcoat catalyst, which is arranged inside the reforming treatment de vice (12) for catalyzing the reforming treatment (2) .
• the aqueous-phase reforming can be carried out at temperature of 200 - 250 °C and under pressure of 30 - 34 bar.
• the Ni/NiAl 2 0 4 spinel washcoat catalyst (3) is arranged in the form of a film, preferably a thin lay er, onto a substrate, such as a metal substrate or a ceramic substrate.
• a substrate such as a metal substrate or a ceramic substrate.
• the Ni/NiAl 2 0 4 spinel washcoat catalyst (3) is prepared in a catalyst pre paring stage (4) .
• the Ni/NiAl 2 0 4 spinel washcoat cata lyst can be formed such that a Ni-precursor, e.g. nickel nitrate, is impregnated by an incipient wetness impregnation method to a boehmite carrier material to form a catalytic material.
• the resulting catalytic ma terial in form of powder is dried and calcined, for example to transform nickel nitrate/boehmite into nickel oxide/boehmite .
• a slurry comprising at least the catalytic material is prepared by mixing the re sulting catalytic material, for example with a binder, an acid and water.
• the slurry is arranged by washcoat ing onto a metal or ceramic substrate, and the wash- coated substrate is thermally treated, e.g. by means of drying, calcination and treatment by reduction.
• Ni/NiAl 2 0 4 can be formed onto the substrate.
• Ni content of the Ni/NiAl 2 0 4 spinel washcoat catalyst is 10 - 16 wt%.
• the hydrogen (5) may be recirculated and fed back to the thermochemical treatment, e.g. to the
• APR aqueous-phase reforming
• the main problems of the APR were mass transfer limitations, and the low activity and stability of the catalysts. Both external and internal mass transfers were limited in a 3-phase system of the APR, with sol id catalyst, liquid feedstock and gaseous products. This limitation negatively affected the conversion of reactants and the selectivity towards desired prod ucts.
• catalysts with low activity such as typical, previous known Ni-based and Ce-promoted cata lysts, decreased the conversion and selectivity.
• Plat inum-based catalysts commonly exhibit good performance in terms of activity. However, the noble metal-based catalysts are expensive and economically inefficient in large scales.
• Ni/NiAl 2 0 4 spinel washcoat catalyst was found to overcome these problems.
• the mass transfer limitations can be decreased by means of the inexpen sive and durable Ni/NiAl 2 0 4 spinel washcoat catalyst which actively and selectively converts the feedstock into targeted products in the operating conditions of the APR process.
• a side water fraction formed from lignocellulosic biomass in a Fischer-Tropsch re- actor was treated with the catalyst in the aqueous- phase reforming (APR) reactor according to the process of Fig. 1.
• APR aqueous- phase reforming
• the aqueous-phase reforming (APR) was carried out at about 230 °C under pressure of about 32 bar.
• the feedstock of the APR was an aqueous solution, formed from the side water fraction, with 5 wt% organ ic compounds, especially MeOH.
• the treatment was car ried out with the Ni/NiAl 2 0 4 spinel washcoat catalyst in the aqueous-phase reforming (APR) reactor. Further, the treatment was carried out with two comparative catalysts, NiAl-catalyst and NiCeAl-catalyst, in the aqueous-phase reforming (APR) reactor.
• the Ni/NiAl 2 0 4 spinel washcoat catalyst comprised about 10 - 13 wt%
• NiAl-catalyst and NiCeAl-catalyst comprised about 10 - 13 wt% Ni on y-Al 2 0 3 support. Further, NiCeAl- catalyst was Ce-promoted.
• Y (%) means yield.
• CtG is calculated as total mol of carbon- containing gaseous products divided by the mol of car- bon-containing compounds in the feeding solution.
• Ni/NiAl 2 0 4 spinel washcoat catalyst was more highly ac tive in the aqueous phase reforming (APR) when com pared to the comparative catalysts.
• the performance of the Ni/NiAl 2 0 4 spinel washcoat catalyst was remarkably superior compared to nickel-based catalysts. High con version rates and hydrogen selectivity could be ob tained when the aqueous-phase reforming was catalyzed with the Ni/NiAl 2 0 4 spinel washcoat catalyst.
• the im provement derives from the high activity of the cata- lyst and the reduction of the internal mass transfer limitations in the thin layer of the washcoat.
• Ni/NiAl 2 0 4 spinel wash- coat catalyst with 13 wt% Ni content was prepared. This catalyst was used in the tests of Example 3.
• Ni-metal precursor such as nickel nitrate was impregnated by means of an incipient wetness impregna tion into a boehmite carrier material in a powder form in order to form a catalytic material.
• the catalytic material in a powder form was dried by means of a vac uum drying and calcinated at 500 °C to convert nickel nitrate/boehmite into nickel oxide/boehmite .
• a slurry composition comprising 44.4 wt% catalyt ic material, 2.01 wt% Disperal 10 solution, 1.05 wt% HN0 3 and 52.54 wt% ion-exchanged water was prepared and stirred by means of a magnetic stirring at 700 rpm for 24 hours.
• a metal substrate was washcoated with the slurry.
• the substrate was pre-treated by an ace tone/isopropanol wash and water rinsing, and the sub strate was calcinated at 900 °C for 6 hours before the washcoating.
• the washcoated substrate was dried by a slow drying with hot air flow and by a fast drying at 500 °C for 5 min.
• the devices and equipments of the aqueous- phase reforming process used in these examples are known per se in the art, and therefore they are not described in any more detail in this context.
• the method, apparatus and catalysts are suit able in different embodiments for treating different kinds of water fractions and streams.

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