WO2010092819A1 - エタノールの製造方法 - Google Patents
エタノールの製造方法 Download PDFInfo
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- WO2010092819A1 WO2010092819A1 PCT/JP2010/000861 JP2010000861W WO2010092819A1 WO 2010092819 A1 WO2010092819 A1 WO 2010092819A1 JP 2010000861 W JP2010000861 W JP 2010000861W WO 2010092819 A1 WO2010092819 A1 WO 2010092819A1
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- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
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- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
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- B01J23/56—Platinum group metals
- B01J23/64—Platinum group metals with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/656—Manganese, technetium or rhenium
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- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/80—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with zinc, cadmium or mercury
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- B01J23/8926—Copper and noble metals
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- B01J23/8933—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/8993—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with chromium, molybdenum or tungsten
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- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
- B01J37/0201—Impregnation
- B01J37/0207—Pretreatment of the support
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- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/1516—Multisteps
- C07C29/1518—Multisteps one step being the formation of initial mixture of carbon oxides and hydrogen for synthesis
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- B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
- B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
- B01J21/08—Silica
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- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
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- C10J2300/00—Details of gasification processes
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- C10J2300/0913—Carbonaceous raw material
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- C10J2300/092—Wood, cellulose
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- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
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- C10J2300/0973—Water
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- C10J2300/00—Details of gasification processes
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- C10J2300/00—Details of gasification processes
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- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
- C10J2300/1656—Conversion of synthesis gas to chemicals
- C10J2300/1665—Conversion of synthesis gas to chemicals to alcohols, e.g. methanol or ethanol
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- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1853—Steam reforming, i.e. injection of steam only
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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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- 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
- Y02E50/10—Biofuels, e.g. bio-diesel
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- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
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- Y02P20/145—Feedstock the feedstock being materials of biological origin
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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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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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- 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
Definitions
- the present invention relates to a method for producing ethanol, and uses ethanol, which is a raw material gas generated by a thermochemical gasification reaction of biomass, that is, renewable organic resources excluding fossil resources. It is related with the manufacturing method.
- thermochemical gasification reaction of biomass it is common to generate a mixed gas of carbon monoxide and hydrogen using a gasification furnace such as a fixed bed or a fluidized bed.
- a gasification furnace such as a fixed bed or a fluidized bed.
- An object of the present invention is to provide a method for producing ethanol in which a raw material gas containing hydrogen and carbon monoxide obtained by gasification of biomass is directly converted into ethanol with high efficiency and high yield.
- the present invention provides a raw material gas generated by a thermochemical gasification reaction of biomass in the presence of a catalyst containing rhodium, at least one transition metal, and at least one element selected from lithium, magnesium, and zinc. It is the manufacturing method of ethanol made to react by.
- the catalyst is supported on a silica carrier and is composed of rhodium, manganese, lithium, and scandium.
- the catalyst is supported on a silica carrier and is composed of rhodium, molybdenum, iridium, copper, and palladium.
- the method for producing ethanol as described above which is any one of a catalyst comprising rhodium, magnesium, zirconium, and lithium.
- the raw material gas generated from the biomass by the thermochemical gasification reaction is purified and reacted in the ethanol synthesizer, and the unreacted raw material gas and by-product gas separated from the reaction product are mixed by the lower hydrocarbon reforming device. After reforming reaction to carbon oxide and hydrogen, it is circulated to the ethanol synthesizer, then the crude ethanol liquid is separated in a multistage distillation column, and further a residual acetaldehyde is obtained by a hydrotreating apparatus provided with a reaction catalyst with hydrogen. In the method for producing ethanol, acetic acid and ethyl acetate are converted into ethanol.
- the ethanol production method of the present invention uses a catalyst containing rhodium and at least one transition metal, and further another metal, so that a gas containing carbon monoxide and hydrogen obtained by a thermochemical gasification reaction of biomass is used. It can be used to produce ethanol directly with high efficiency.
- FIG. 1 is a diagram illustrating steps from biomass gasification to ethanol production.
- the ethanol production method and ethanol production catalyst of the present invention is a gas containing carbon monoxide and hydrogen
- any gas can be used as a raw material gas, but by a thermochemical reaction of biomass.
- a method of using the obtained biomass gas containing carbon monoxide and hydrogen as a raw material gas will be described as an example.
- FIG. 1 is a diagram for explaining steps from gasification by biomass thermochemical reaction to ethanol production.
- the biomass and superheated steam supplied from the biomass supply unit 2 and the steam supply unit 3 are supplied to a gasification furnace 4 equipped with a reforming catalyst, and hydrogen and monoxide at a high temperature.
- a raw material gas containing carbon is generated.
- gasifier 4 can be used, but a fluidized bed type is preferable.
- the gasification furnace has a supply means for supplying biomass, a heating means for heating the gasification furnace including the reforming catalyst, a biomass supply means for supplying biomass, and a means for supplying superheated steam and an oxidizing agent. ing.
- biomass gas obtained by the thermochemical reaction of biomass By-product low hydrocarbons such as methane and ethane, benzene, polycondensed aromatic hydrocarbons, and oil tar components contained in biomass gas obtained by the thermochemical reaction of biomass can be further converted into reformed gas. Thereby, the conversion efficiency of biomass gasification can be improved and biomass gas of 60% or more can be obtained on the basis of biomass.
- biomass gas a gas mainly composed of carbon monoxide, hydrogen, methane, ethane, ethylene, and carbon dioxide can be obtained.
- the hydrogen yield is increased by high-efficiency gasification of lower hydrocarbons such as methane, ethane, and ethylene, which are by-produced, and the hydrogen / carbon monoxide ratio in the feed gas supplied to the ethanol synthesis reaction is 2 or more.
- ethanol can be produced with high yield and high selectivity using an ethanol synthesizer connected to a biomass gasifier.
- biomass used in the present invention examples include woody biomass and industrial waste biomass such as wood such as cedar, woody building waste, grass sorghum, hagas, sugar beet pomace, sugar beet pomace, rice straw, etc. Can do. Moreover, the thing which grind
- the average particle size of the pulverized biomass is preferably 5 mm or less. If the average particle size exceeds 5 mm, the reaction progresses slowly and it is difficult to perform highly efficient gasification. On the other hand, if it is 0.05 mm or less, the pulverization efficiency is deteriorated.
- the hydrogen / carbon monoxide molar ratio is preferably 2 or more. For this reason, it is necessary to adjust the reaction conditions so that the reaction of the above formula 1-5 can be carried out smoothly.
- the reaction temperature in the gasification furnace 4 is preferably adjusted to 700 to 1000 ° C. Further, by controlling the internal temperature of the gasifier including the reforming catalyst to a high temperature region, the hydrogen yield is increased and a raw material gas having a hydrogen / carbon monoxide molar ratio of 2 or more can be obtained.
- the reforming catalyst is preferably adjusted to 400 to 650 ° C.
- a nickel-based catalyst can be used as the reforming catalyst provided in the gasification furnace 4.
- by-product lower hydrocarbons such as methane and ethane generated from biomass, benzene, polycondensed ring aromatic hydrocarbons, and tar components can be further reformed and gasified.
- a hydrogen gas is increased by an efficient gasification reaction of lower hydrocarbons such as methane and ethane produced as a by-product, and a raw material gas having a hydrogen / carbon monoxide ratio of 2 or more in the raw material gas is obtained. This makes it possible to produce bioethanol with high yield and high selectivity using an ethanol synthesizer connected to a biomass gasifier.
- the ash is taken out from the ash outlet 10, and the generated raw material gas is supplied to the hydrogen reduction device 5 to react with the hydrogen supplied from the hydrogen supply unit 8, so that sulfur compound, ammonia, amine Nitrogen compounds such as the like are reduced.
- the hydrogen reduction device 5 a device including a cobalt-molybdenum catalyst or the like can be used.
- the hydrogen supply unit 8 can be provided with hydrogen obtained by a lower hydrocarbon reforming apparatus.
- desulfurization is performed to remove sulfur compounds such as hydrogen sulfide (H2S), carbonyl sulfide (COS), carbon disulfide (CS2).
- H2S hydrogen sulfide
- COS carbonyl sulfide
- CS2 carbon disulfide
- the desulfurization device 6 a device provided with a zinc oxide desulfurizing agent or the like can be used.
- the raw material gas purified by the hydrogen reduction device 5 and the desulfurization device 6 separates the condensed water separated in the gas-liquid separation device 7 a connected to the outlet of the desulfurization device 6 from the condensed water discharge port 9.
- the pressure of the purified raw material gas is increased by a compressor 11a to a range of 0.2-5.1 MPa, preferably 1.0-3 MPa, and a temperature range of 200-400 ° C., preferably 250-300 ° C.
- SV space velocity of the raw material gas velocity L / h / catalyst volume L
- the raw material gas is brought into contact with the ethanol synthesis catalyst provided in the ethanol synthesizer 12 to perform an ethanol production reaction.
- the ethanol synthesis apparatus 12 is provided with a supply means for supplying the raw material gas to the ethanol synthesis catalyst and a heating means for heating the ethanol synthesis catalyst so as to surround the ethanol synthesis catalyst, and is connected to the outlet of the ethanol synthesis catalyst.
- the gas-liquid separation device 7b separates and recovers a liquid product such as 50-60 vol% ethanol from the outlet reaction gas containing unreacted raw material gas, by-product methane and ethane.
- the ethanol conversion yield and selectivity from the raw material gas on the basis of carbon monoxide are improved and the yield of ethanol that can be produced from 1 ton of unit biomass is 0.3-0. It can be increased to 5 tons.
- the liquid product separated by the gas-liquid separator 7b is supplied to the multistage distillation column 16.
- the gas-liquid separator 7b is provided with a liquid product outlet 13.
- the ethanol concentration is concentrated to 79-90% by volume, and acetic acid, acetaldehyde, propanol, methanol, and the like, which are low boiling point residues, are separated and recovered by the recovery means 17.
- a distillation column equipped with a Raschig ring can be used as the multistage distillation column 16.
- the crude ethanol solution obtained in the multi-stage distillation column 16 is converted into ethanol by the hydrotreating device 19 provided with a reaction catalyst with hydrogen by the liquid supply pump 18 to the remaining acetic acid, acetaldehyde, ethyl acetate and the like. Can increase the yield.
- the reaction catalyst with hydrogen include a CuZnO catalyst and a PdFe catalyst.
- hydrogen generated in the lower hydrocarbon reforming apparatus can be used for the hydrotreating apparatus.
- the ethanol after the hydrogenation treatment is brought into contact with the sodium hydroxide aqueous solution supplied from the sodium hydroxide aqueous solution supply port 20 to remove acidic substances, and then separated in the gas-liquid separator 7c. Subsequently, ethanol is supplied to the multistage distillation column 21 and 95% by volume of ethanol is recovered from the ethanol outlet 23. Further, the residual components excluding ethanol are discharged from the residual component outlet 25. Further, water is removed by the zeolite adsorption separation tower 22, and 99 vol% ethanol is recovered from the ethanol outlet 24.
- a gas raw material containing methane, ethane, ethylene, and carbon dioxide each containing 10% by volume in a mixed gas of carbon monoxide and hydrogen, and not containing In the gas raw material the ethanol production activity is improved by about 2-10% and the stability of the catalyst performance is improved.
- Example 1 Preparation of Catalyst 1 Ethanol aqueous solution of chlorides having a silica support (surface area of 185 m 2 / g) and rhodium, manganese, lithium and scandium in a metal atomic ratio of 1: 0.05: 0.3: 0.15. After being impregnated, the mixture was heated to 100 ° C. for 1 hour under a mixed air flow of hydrogen and nitrogen (1: 4 volume ratio), held for 2 hours, heated to 400 ° C. for 2 hours and held for 2 hours to 25 ° C. The catalyst 1 was prepared by supporting rhodium, manganese, lithium, and scandium on a silica support.
- the volume composition of the obtained raw material gas was 26% carbon monoxide, 54% hydrogen, 10% methane, 1% ethane, 5% carbon dioxide, and the balance was nitrogen.
- the raw material gas was purified by hydrogenation using a CoMo catalyst and a desulfurization processing apparatus using zinc oxide.
- Example 2 Preparation of Catalyst 2 On a silica support (surface area 215 m 2 / g), rhodium, molybdenum, iridium, copper and palladium are each in a metal atomic ratio of 1: 0.3: 0.2: 0.5: 0.3.
- the temperature was raised to 150 ° C for 1 hour under a mixed air flow of hydrogen and nitrogen (1: 3 volume ratio) and held for 2 hours
- the catalyst 2 was heated to 450 ° C. for 2 hours, held for 2 hours, and cooled to room temperature to activate the catalyst 2 to prepare catalyst 2 supporting rhodium, molybdenum, iridium, copper and palladium on a silica support.
- a raw material gas was produced in the same manner as in Example 1 except that 5 kg of rice straw per hour was used as biomass.
- the volume composition of the raw material gas was 28% carbon monoxide, 48% hydrogen, 3% methane, 1% ethane, 15% carbon dioxide, and the balance was nitrogen.
- Ethanol synthesis test The purified raw material gas was supplied at 2.5 MPa and a temperature of 280 ° C. to a reactor filled with catalyst 2 and ceramic balls as a diluent mixed at a volume ratio of 4: 1.
- Example 3 Preparation of Catalyst 3 Aqueous ethanol aqueous solution of each chloride in which the silica carrier (surface area 215 m 2 / g) is rhodium, zirconium, lithium and magnesium at a metal atom ratio of 1: 0.3: 0.5: 0.8. After being impregnated, the mixture was heated to 100 ° C. for 1 hour under a mixed air flow of hydrogen and nitrogen (1: 4 volume ratio), held for 2 hours, heated to 400 ° C. for 2 hours and held for 2 hours, at room temperature.
- the catalyst 3 was prepared by supporting rhodium, zirconium, lithium and magnesium on a silica support.
- Comparative Example Catalyst 4 On a silica support (surface area 245 m 2 / g), iridium chloride, palladium chloride, and nitric acid each having an iridium, copper, and palladium ratio of 1: 0.5: 0.5 in each metal atomic ratio. After impregnating with an aqueous ethanol solution of copper, the mixture was heated to 100 ° C. for 1 hour under a mixed gas flow of hydrogen and nitrogen (1: 2 volume ratio), held for 2 hours, heated to 350 ° C. for 2 hours and held for 2 hours. Thereafter, activation treatment was performed by lowering the temperature to room temperature, and a catalyst 4 in which iridium, copper and palladium were supported on a silica support was prepared.
- Ethanol synthesis test An ethanol synthesis test was conducted under the same conditions as in Example 1 except that the reactor filled with the raw material gas and catalyst 4 used in Example 1 was reacted at 2.5 MPa and 280 ° C. However, after 100 hours, ethanol was 0.5-1 g / catalyst L / h, and the ethanol selectivity based on carbon monoxide was 1% or less.
- the ethanol production method and ethanol production catalyst of the present invention can produce ethanol in a high yield from a raw material gas obtained by a thermochemical gasification reaction of biomass. This makes it possible to synthesize ethanol from raw materials that are difficult to ferment, such as grass wood and rice straw, and industrial waste biomass such as building wood and pulp, thereby expanding the range of raw materials for ethanol production and economical.
- a simple ethanol synthesis method can be used to synthesize ethanol from raw materials that are difficult to ferment, such as grass wood and rice straw, and industrial waste biomass such as building wood and pulp.
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Abstract
Description
なかでも、バイオマスを原料として、重要な化学品であって、自動車の燃料としても期待されているエタノールの効率的な製造方法の確立が求められている。
バイオマスを原料としたエタノールの製造方法として、発酵等の生物学的プロセスを使用してバイオマスから直接エタノールを合成する方法が提案されている。
しかしながら、木質系のバイオマスでは30質量%前後含有されるリグニンやセルロースをエタノールに変換するための前処理には、多大な工程が必要であり高コストであって技術的および経済性の問題があった。また、バイオマスの残渣物が多量に発生し、バイオマスの利用率が低いという問題もある。
しかしながら、バイオマスを熱化学的ガス化反応においては、例えば固定床或いは流動床等のガス化炉等を用いて一酸化炭素と水素の混合ガスを生成することが一般的であるが、発生条件によっては、水素の割合が少なくエタノールを直接合成する目的に使用した場合には、効率的なエタノール合成の原料とならないという問題があった。
また、触媒が、シリカ担体に担持した、ロジウム、マンガン、リチウム、およびスカンジウムからなる触媒、シリカ担体に担持した、ロジウム、モリブデン、イリジウム、銅、およびパラジウムからなる触媒、または、シリカ担体に担持した、ロジウム、マグネシウム、ジルコニウム、およびリチウムからなる触媒のいずれかである前記のエタノールの製造方法である。
バイオマスから熱化学的ガス化反応によって発生させた原料気体を精製し、エタノール合成装置において反応させ、反応生成物から分離した、未反応原料気体および副生気体を低級炭化水素改質処理装置によって一酸化炭素と水素に改質反応処理した後に、前記エタノール合成装置に循環し、次いで、多段蒸溜塔で粗エタノール液を分離し、さらに水素との反応触媒を設けた水素化処理装置によって、残留アセトアルデヒド、酢酸,酢酸エチルをエタノールに変換する前記のエタノールの製造方法である。
本発明のエタノール製造工程1は、バイオマス供給部2と水蒸気供給部3から供給されるバイオマスと過熱水蒸気を、改質触媒を備えたガス化炉4に供給して高温度で、水素と一酸化炭素を含有する原料気体を発生させる。
ガス化炉4には各種のものを用いることができるが、流動床式のものが好ましい。また、ガス化炉にはバイオマスを供給する供給手段と、改質触媒を含むガス化炉を加熱する加熱手段、バイオマスを供給するバイオマス供給手段と、過熱水蒸気と酸化剤を供給する手段を有している。
CO+H2O → CO2 +H2 式1
C+H2O → CO+H2 式2
C+2H2 O → CO2 +2H2 式3
CH4+H2O → CO+3H2 式4
CH4+CO2 → 2CO+2H2 式5
加えて副生するメタン、エタンなどの低級炭化水素の効率なガス化反応により水素収率を増大して原料気体中の水素/一酸化炭素比が2以上の原料気体が得られる。これによりバイオマスのガス化装置に連結するエタノール合成装置を用いて高収量で高選択率でバイオエタノールを製造することができる。
水素還元装置5と脱硫装置6によって精製された原料気体は、脱硫装置6の出口部に連結された気液分離装置7aにおいて分離した凝縮水を凝縮水排出口9から分離する。
これにより原料気体からのエタノールの合成工程において、一酸化炭素基準での原料気体からのエタノール変換収率と選択率を向上すると共に単位バイオマス1トンから製造できるエタノールの収量を0.3-0.5トンに増大することができる。
多段蒸溜塔16においてエタノール濃度79-90体積%に濃縮すると共に、低沸点残留分である酢酸、アセトアルデヒド、プロパノール、メタノールなどを回収手段17で分離回収する。多段蒸溜塔16には、ラシッヒリングを備えた蒸溜塔を用いることができる。
前記多段蒸溜塔16で得られた粗エタノール液を、液体供給ポンプ18によって水素との反応触媒を設けた水素化処理装置19によって、残留する酢酸、アセトアルデヒド、酢酸エチル等をエタノールへと変換させることによって収量を増加させることができる。水素との反応触媒としては、CuZnO触媒やPdFe触媒を挙げることができる。
また、水素化処理装置には、低級炭化水素改質処理装置において生成する水素を利用することができる。
更に、ゼオライト吸着分離塔22で水分を除去して99体積%エタノールをエタノール取り出し口24から回収する。
触媒1の調製
シリカ担体(表面積185m2/g)に、ロジウム、マンガン、リチウム、スカンジウムを各金属原子比で1:0.05:0.3:0.15となるそれぞれの塩化物のエタノール水溶液に含浸した後に、水素と窒素(1:4体積比)の混合気流下で100℃まで1時間昇温し、2時間保持し、400℃まで2時間昇温して2時間保持して25℃に降温することによって活性化処理をし、シリカ担体にロジウム、マンガン、リチウム、スカンジウムを担持した触媒1を調製した。
シリカ担体(表面積265m2/g)に、銅と亜鉛を各金属原子比で1:0.8となるそれぞれの硝酸塩のエタノール水溶液に含浸した後に、水素と窒素(1:2体積比)の混合気流下で100℃まで1時間昇温し、2時間保持し、400℃まで2時間昇温して2時間保持し、25℃に降温することによって活性化処理し、シリカ担体に銅と酸化亜鉛(ZnO)を担持したCu/ZnO触媒1を調製した。
図1で示す装置に、1時間当たり杉木粉10kgを供給して800℃において、水蒸気を供給しながらガス化炉で原料気体を1時間当たり15Nm3 、水素/一酸化炭素(容量比)=2を製造した。
得られた原料気体の体積組成は、一酸化炭素26%、水素54%、メタン10%、エタン1%、二酸化炭素5%、残部は窒素であった。また、原料気体は、CoMo触媒による水素化と、酸化亜鉛を用いた脱硫処理装置で精製した。
精製した原料気体を2.5MPa、温度280℃において、触媒1を充填した反応器Aに導入した後、反応器Aに直結した反応器Bにシリカ担時Cu/ZnO触媒1を充填して、2.5MPa、温度280℃において接触循環反応を行いエタノール選択率80%(一酸化炭素基準)、エタノール空時収率320g/触媒L/hでエタノールが生成した。
1000時間の反応経過においてもエタノール合成性能が維持された。気液分離装置で回収されたエタノール(エタノール52%+水39%(容量比))を蒸留分離とゼオライト吸着精製処理を行なって水を除去して、99体積%エタノール3.5kgを得た。
触媒2の調製
シリカ担体(表面積215m2/g)に、ロジウム、モリブデン、イリジウム、銅とパラジウムを各金属原子比で1:0.3:0.2:0.5:0.3となるそれぞれRh,Mo,Ir,Pdの各塩化物と硝酸銅のエタノール水溶液に含浸した後に、水素と窒素(1:3体積比)の混合気流下で150度Cまで1時間昇温し、2時間保持し、450℃まで2時間昇温して2時間保持して室温に降温することによって活性化処理し、シリカ担体にロジウム、モリブデン、イリジウム、銅とパラジウムを担持した触媒2を調製した。
バイオマスとして稲わら毎時5kgを用いた点を除き実施例1と同様にして原料気体を製造した。原料気体の体積組成は一酸化炭素28%、水素48%、メタン3%、エタン1%、二酸化炭素15%、残部は窒素であった。
エタノールの合成試験
精製した原料気体を2.5MPa、温度280℃において、触媒2と、希釈材としてのセラミックボールを体積比4:1で混合して充填した反応器に供給した。
反応気体を7.1MPa、300℃、SV=9000L/hで接触反応して一酸化炭素転化率58%、エタノール250g触媒L/hとメタノール480g/触媒L/hが得られた。
触媒3の調製
シリカ担体(表面積215m2/g)に、ロジウム、ジルコニウム、リチウム、マグネシウムを各金属原子比で1:0.3:0.5:0.8となるそれぞれの塩化物のエタノール水溶液に含浸した後に、水素と窒素(1:4体積比)の混合気流下で100℃まで1時間昇温し、2時間保持し、400度Cまで2時間昇温して2時間保持し、室温に降温することによって活性化処理し、シリカ担体にロジウム、ジルコニウム、リチウム、マグネシウムを担持した触媒3を調製した。
シリカ担体(表面積165m2/g)に、銅、亜鉛とチタンを各金属原子比で1:0.8:0.2となるように、硝酸銅、硝酸亜鉛、塩化チタン(III)のエタノール水溶液に含浸した後に、水素と窒素ガス(1:2体積比)の混合気流下で100℃まで1時間昇温し、2時間保持し、450℃まで2時間昇温して2時間保持して室温に降温にして活性化処理して、シリカ担体に銅と亜鉛とチタンを担持したCuZnTi触媒を調製した。
実施例1と同様にして、杉木材ペレット毎時10kgを用いて原料気体10Nm3/h、水素/一酸化炭素モル比=1.5を調整した。
エタノールの合成試験
生成した原料気体を触媒3と、CuZnTi触媒を充填した装置に、7.1MPa、290℃、SV=6000L/hにおいて接触反応させてエタノールを460kg/触媒L/h、および酢酸290g/触媒L・hの空時収率を得た。
触媒4の調製
シリカ担体(表面積245m2/g)に、イリジウム、銅とパラジウムを各金属原子比で1:0.5:0.5となるそれぞれイリジウム塩化物、パラジウム塩化物、および硝酸銅のエタノール水溶液に含浸した後に、水素と窒素(1:2体積比)混合気流下で100℃まで1時間昇温し、2時間保持し、350℃まで2時間昇温して2時間保持した後に、室温に降温することによって活性化処理し、シリカ担体にイリジウム、銅とパラジウムを担持した触媒4を調製した。
実施例1で使用した原料気体と触媒4を充填した反応器に2.5MPa、280℃の条件で反応させた点を除き実施例1と同様の条件でエタノール合成試験を行なったところ、100時間後には、エタノールは0.5-1g/触媒L/hのであり、一酸化炭素基準でのエタノール選択率は1%以下であった。
1 バイオマス供給部
2 水蒸気供給部
3 ガス化炉
4 還元装置
5 脱硫装置
7a 気液分離装置
7b 気液分離装置
7c 気液分離装置
8 水素供給部
9 凝縮水排出口
10 灰分取りだし口
11a 循環圧縮機
11b 循環圧縮機
12 エタノール合成装置
13 液状生成物取り出し口
14 オフガス取り出し口
15 低級炭化水素改質処理装置
16 多段蒸留塔
17 回収手段
18 液体供給ポンプ
19 水素化処理装置
20 水酸化ナトリウム水溶液供給口
21 多段蒸留塔
22 ゼオライト吸着分離塔
23 エタノール取り出し口
24 エタノール取り出し口
25 残留成分取り出し口
Claims (3)
- バイオマスの熱化学的ガス化反応によって得られる原料気体を、ロジウムと、少なくとも一種の遷移金属と、リチウム、マグネシウム、亜鉛から選ばれる少なくとも一種の元素と、を含む触媒の存在下で反応させることを特徴とするエタノールの製造方法。
- 触媒が、シリカ担体に担持した、ロジウム、マンガン、リチウム、およびスカンジウムからなる触媒、シリカ担体に担持した、ロジウム、モリブデン、イリジウム、銅、およびパラジウムからなる触媒、または、シリカ担体に担持した、ロジウム、マグネシウム、ジルコニウム、およびリチウムからなる触媒のいずれかであることを特徴とする請求項1記載のエタノールの製造方法。
- バイオマスから熱化学的によって発生させた原料気体を精製し、エタノール合成装置において反応させ、反応生成物から分離した、未反応原料気体および副生気体を低級炭化水素改質処理装置によって一酸化炭素と水素に改質反応処理した後に、前記エタノール合成装置に循環し、次いで、多段蒸溜塔で粗エタノール液を分離し、水素との反応触媒を設けた水素化処理装置によって、アセトアルデヒド、酢酸,酢酸エチルをエタノールに変換することを特徴とする請求項1または2記載のエタノールの製造方法。
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- 2010-02-12 JP JP2010550465A patent/JP4979818B2/ja not_active Expired - Fee Related
- 2010-02-12 CA CA2751882A patent/CA2751882C/en not_active Expired - Fee Related
- 2010-02-12 WO PCT/JP2010/000861 patent/WO2010092819A1/ja active Application Filing
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- 2012-04-13 JP JP2012092146A patent/JP5052703B2/ja not_active Expired - Fee Related
- 2012-04-13 JP JP2012092141A patent/JP5143965B2/ja not_active Expired - Fee Related
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Cited By (13)
Publication number | Priority date | Publication date | Assignee | Title |
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WO2012035019A1 (de) | 2010-09-16 | 2012-03-22 | Basf Se | Verfahren zur herstellung von acrysläure aus ethanol und formaldehyd |
DE102010040923A1 (de) | 2010-09-16 | 2012-03-22 | Basf Se | Verfahren zur Herstellung von Acrylsäure aus Ethanol und Formaldehyd |
US8507721B2 (en) | 2010-09-16 | 2013-08-13 | Basf Se | Process for preparing acrylic acid from ethanol and formaldehyde |
WO2013031598A1 (ja) * | 2011-08-31 | 2013-03-07 | 積水化学工業株式会社 | 酸素化物合成用の触媒及びその製造方法、酸素化物の製造装置ならびに酸素化物の製造方法 |
US9272267B2 (en) | 2011-08-31 | 2016-03-01 | Sekisui Chemical Co., Ltd. | Catalyst for oxygenate synthesis and method for manufacturing same, device for manufacturing oxygenate, and method for manufacturing oxygenate |
WO2013186886A1 (ja) * | 2012-06-13 | 2013-12-19 | 三井造船株式会社 | エタノール製造方法およびエタノール製造装置 |
US20150182939A1 (en) * | 2012-07-23 | 2015-07-02 | Sekisui Chemical Co., Ltd. | System for producing oxygenate and method for producing oxygenate |
US9975105B2 (en) * | 2012-07-23 | 2018-05-22 | Sekisui Chemical Co., Ltd. | System for producing oxygenate and method for producing oxygenate |
JP2014105120A (ja) * | 2012-11-26 | 2014-06-09 | National Institute Of Advanced Industrial & Technology | メタン改質方法および、それに用いるメタン改質触媒 |
EP3246301A4 (en) * | 2015-01-13 | 2018-07-04 | Sekisui Chemical Co., Ltd. | Butadiene production system and butadiene production method |
EP3246302A4 (en) * | 2015-01-13 | 2018-07-04 | Sekisui Chemical Co., Ltd. | Butadiene production system and butadiene production method |
US10065902B2 (en) | 2015-01-13 | 2018-09-04 | Sekisui Chemical Co., Ltd. | Butadiene production system and butadiene production method |
US10189754B2 (en) | 2015-01-13 | 2019-01-29 | Sekisui Chemical Co., Ltd. | Butadiene production system and butadiene production method |
Also Published As
Publication number | Publication date |
---|---|
JP2012149089A (ja) | 2012-08-09 |
CA2751882A1 (en) | 2010-08-19 |
CA2751882C (en) | 2017-03-14 |
JPWO2010092819A1 (ja) | 2012-08-16 |
JP4979818B2 (ja) | 2012-07-18 |
US8927781B2 (en) | 2015-01-06 |
JP5143965B2 (ja) | 2013-02-13 |
CN102333748A (zh) | 2012-01-25 |
JP5052703B2 (ja) | 2012-10-17 |
CN102333748B (zh) | 2014-12-24 |
US20120071697A1 (en) | 2012-03-22 |
JP2012131833A (ja) | 2012-07-12 |
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