WO2016203944A1 - 合成ガスの製造方法および装置 - Google Patents

合成ガスの製造方法および装置 Download PDF

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WO2016203944A1
WO2016203944A1 PCT/JP2016/066110 JP2016066110W WO2016203944A1 WO 2016203944 A1 WO2016203944 A1 WO 2016203944A1 JP 2016066110 W JP2016066110 W JP 2016066110W WO 2016203944 A1 WO2016203944 A1 WO 2016203944A1
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gas
biogas
synthesis gas
reforming
reaction
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PCT/JP2016/066110
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English (en)
French (fr)
Japanese (ja)
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和之 藤本
貴紀 貝川
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エア・ウォーター株式会社
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Priority to PH12017550143A priority Critical patent/PH12017550143A1/en

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    • 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
    • B01J23/89—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
    • 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
    • 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
    • C01B3/40—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
    • 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

Definitions

  • the present invention relates to a method and apparatus for producing a synthesis gas that uses biogas as a raw material and generates a synthesis gas mainly composed of carbon monoxide and hydrogen.
  • Biomass is an ecosystem resource, so its production tends to fluctuate depending on the season. Therefore, in general, there is a concern about the stable supply of biomass compared to petroleum, and there are still problems in storage and transportation.
  • palm palm is cultivated near the equator and is stably produced throughout the year. Such palm palm is used as a raw material for palm oil. In other words, it can be said that palm palm is a biomass that has achieved a stable supply.
  • Palm oil obtained from palm palm is used not only as cooking oil but also as a raw material for margarine, shortening and soap.
  • palm oil as biodiesel fuel has also been promoted.
  • palm oil has one of the highest production volumes in the world, and its consumption is increasing year by year. Accordingly, palm palm production is expected to increase in the future.
  • biogas mixed gas
  • a method of using a synthesis gas mainly composed of carbon monoxide and hydrogen as a raw material and using a methanol synthesis reaction or an ethanol synthesis reaction is employed.
  • the synthesis gas as the raw material is obtained by steam reforming a hydrocarbon gas such as methane and converting it into carbon monoxide and hydrogen.
  • natural gas is often used as the methane for the steam reforming.
  • the use of the above-described biogas as the methane has been studied.
  • the synthesis gas used for the synthesis of methanol or the like has a preferable ratio of carbon monoxide and hydrogen present in the synthesis gas depending on the application.
  • the ratio of hydrogen is significantly higher. That is, the synthesis gas obtained by steam reforming of methane is not a suitable composition as a raw material for methanol synthesis or the like.
  • hydrogen becomes excessive with respect to the reaction.
  • the biogas includes about 40% by volume of carbon dioxide in addition to methane.
  • the carbon dioxide concentration is extremely high.
  • synthesis gas having a high carbon monoxide ratio is generated.
  • carbon monoxide ratio in the synthesis gas is high, carbon is likely to precipitate due to the Budoir reaction (2CO ⁇ C + CO 2 ). If carbon deposits in the equipment downstream of the reformer or on the reforming catalyst, the equipment will be clogged and pressure loss will increase, or the activity of the catalyst will decrease, and the reformer will operate stably. Inhibit.
  • Patent Document 1 is a method for reforming natural gas having a low carbon dioxide concentration.
  • Patent Document 2 is a method for reforming biomethane obtained by removing CO 2 from biogas.
  • Patent Document 1 The above Patent Document 1 has the following description.
  • [Claim 1] A synthesis gas production method for producing a synthesis gas mainly composed of carbon monoxide and hydrogen by reforming a raw material gas containing a hydrocarbon gas and an oxygen gas, Carbon dioxide with respect to the reformed gas in a state where the reformed gas is maintained at a temperature of 700 ° C. or higher so that the equilibrium of the Budoir reaction (2CO ⁇ C + CO 2 ) occurring in the reformed gas generated by the reforming reaction is shifted to the left side
  • a synthesis gas production method characterized by introducing a gas.
  • the reformed gas is maintained at a temperature of 700 ° C.
  • an oxygen introduction passage 1 for introducing oxygen, a carbon dioxide introduction passage 2 for introducing carbon dioxide, and a hydrocarbon introduction passage 3 for introducing natural gas as a hydrocarbon gas merge into a raw material gas introduction passage 4.
  • the source gas is introduced into the reformer 5.
  • Patent Document 1 discloses a method of reforming by adding excessive water vapor in order to suppress carbon deposition from the reformed gas.
  • excess water vapor is added as an oxidizing agent so that the molar ratio of H 2 O / CH 4 is 3 to 5.
  • the first is a method of adjusting the composition by a CO shift reaction downstream of the reformer.
  • the second is a method in which carbon monoxide and hydrogen are separated and purified from the generated synthesis gas and then remixed at a desired ratio.
  • Patent Document 2 The above Patent Document 2 has the following description.
  • the present invention relates to a process for producing hydrogen by steam reforming biomethane and for producing hydrogen by purifying syngas shifted by PSA, which is supplied to produce biomethane. At least one step of purifying the first portion of the biogas, which is modified, and the resulting syngas is shifted and purified by PSA.
  • the emissions from the PSA are used as secondary fuel for the reforming furnace, and the feedstock or partially purified biogas is used as the primary fuel for the furnace.
  • the present invention has been made with the following object in order to solve the above problems.
  • a method and an apparatus for producing a synthesis gas which uses a biogas as a raw material and generates a synthesis gas having a H 2 / CO molar ratio of about 1 to 2 without performing a pretreatment for removing CO 2 .
  • the synthesis gas manufacturing method employs the following configuration.
  • a synthesis gas mainly composed of carbon monoxide and hydrogen by reforming a hydrocarbon-based gas, an oxygen-based gas, and water vapor
  • biogas as the hydrocarbon-based gas
  • carbon dioxide is not separated and removed.
  • the synthesis gas manufacturing method according to claim 2 employs the following configuration in addition to the configuration according to claim 1.
  • methane is 50 volume% or more and 70 volume% or less, and the remainder is a carbon dioxide and an impurity.
  • the synthesis gas manufacturing method according to claim 3 employs the following configuration in addition to the configuration according to claim 1 or 2.
  • the mixing ratio of the biogas, oxygen-based gas, and water vapor is a molar ratio.
  • the syngas production apparatus employs the following configuration. It is equipped with a reformer to obtain a synthesis gas mainly composed of carbon monoxide and hydrogen by reforming a hydrocarbon-based gas, an oxygen-based gas, and steam. Using biogas as the hydrocarbon-based gas, There is no means for separating and removing carbon dioxide from the biogas supplied to the reformer.
  • the synthesis gas manufacturing apparatus described in claim 6 employs the following configuration.
  • methane is 50 volume% or more and 70 volume% or less, and the remainder is a carbon dioxide and an impurity.
  • the synthesis gas manufacturing apparatus described in claim 7 employs the following configuration.
  • the mixing ratio of the biogas, oxygen-based gas, and water vapor is a molar ratio.
  • the synthesis gas production apparatus described in claim 8 employs the following configuration.
  • the catalyst used for the reforming reaction is an Rh-modified (Ni—CeO 2 ) -Pt catalyst, and the combustion reaction and reforming reaction of the hydrocarbon gas proceed simultaneously in the same reaction region.
  • the synthesis gas production method according to claim 1 and the synthesis gas production apparatus according to claim 5 use biogas as the hydrocarbon-based gas, and separate carbon dioxide when the biogas is subjected to a reforming reaction. Do not remove.
  • the present invention generates a synthesis gas mainly composed of carbon monoxide and hydrogen without using a biogas as a raw material. Therefore, according to the present invention, a desired synthesis gas can be obtained without applying cost or power to a carbon dioxide removal process such as PSA.
  • the biogas is composed of 50% by volume or more and 70% by volume or less of methane, and the balance is carbon dioxide and impurities.
  • a desired synthesis gas can be obtained by using a biogas having the above composition as a raw material without applying cost or power to a carbon dioxide removal step such as PSA.
  • the present invention can generate a synthesis gas having a H 2 / CO molar ratio of about 1 to 2 using biogas as a raw material without performing a pretreatment for CO 2 removal.
  • the synthesis gas production method according to claim 4 and the synthesis gas production apparatus according to claim 8 use an Rh-modified (Ni-CeO 2 ) -Pt catalyst as a catalyst used in the reforming reaction, and Gas combustion reaction and reforming reaction proceed simultaneously in the same reaction zone.
  • a combustion reaction that is an exothermic reaction and a reforming reaction that is an endothermic reaction are simultaneously advanced in the same reaction region. Therefore, the present invention can use the heat energy generated in the combustion reaction as a heat source for the reforming reaction, and the energy efficiency is improved.
  • an exothermic reaction and an endothermic reaction proceed simultaneously, and thermal neutralization occurs.
  • the temperature rise in the reaction region is suppressed as compared with the case where a region for performing the catalytic combustion reaction alone is provided in the reformer. That is, according to the present invention, the heat-resistant material used for the reformer and the heat-resistant structure of the reformer itself do not have such a high temperature specification, and the equipment cost can be reduced.
  • FIG. 1 is a process diagram for explaining a synthesis gas production method.
  • (A) is a process showing an example of an embodiment to which the present invention is applied, and
  • (B) is a conventional process.
  • the target synthesis gas production method is to obtain synthesis gas by reforming biogas.
  • the resulting synthesis gas is a gas containing carbon monoxide and hydrogen as main components.
  • the synthesis gas can be used for, for example, synthesis of carbon monoxide and hydrogen to produce methanol or ethanol.
  • the biogas is a gas mainly composed of methane and carbon dioxide.
  • a desulfurization step and a CO 2 removal step are performed as a pretreatment for introducing the biogas into the steam reforming step.
  • a sulfur component that is a poisoning component of the reforming catalyst is removed.
  • the CO 2 removal step removes carbon dioxide contained in a large amount in biogas.
  • a PSA method is adopted as the CO 2 removal step.
  • biomethane mainly composed of methane is introduced into the steam reforming process.
  • a hydrocarbon-based gas, an oxygen-based gas, and water vapor are subjected to a reforming reaction to produce a synthesis gas mainly composed of carbon monoxide and hydrogen.
  • Biogas is used as the hydrocarbon gas.
  • the reforming reaction is a heat neutralization reforming reaction.
  • carbon dioxide is not separated and removed. That is, this embodiment does not have a step of separating and removing carbon dioxide from biogas, and does not use a carbon dioxide separation and removal device.
  • the biogas targeted by the present invention is a kind of biofuel.
  • the biogas is a gas generated by fermenting or anaerobically digesting biological waste, organic fertilizer, biodegradable substances, sludge, sewage, garbage, energy crops, and the like.
  • the biogas can be produced by fermenting, for example, palm palm pomace or sugarcane in a highly airtight fermenter.
  • the main components of the biogas are methane and carbon dioxide, which may contain nitrogen, hydrogen, oxygen, sulfur, etc. as other impurities.
  • methane having a general composition of 50% by volume or more and 70% by volume or less and the balance being carbon dioxide and impurities.
  • methane is less than 50% by volume, the generation efficiency of synthesis gas decreases. Further, the composition of the generated synthesis gas is not suitable for the synthesis of methanol or ethanol.
  • a process for removing carbon dioxide in biogas is required, which requires extra power and cost.
  • the biogas contains a sulfur content regardless of whether it is derived from animals or plants.
  • the sulfur content is a poisoning component for the reforming catalyst and loses the catalytic activity. For this reason, in this embodiment, the desulfurization process which removes a sulfur content from the biogas before introduce
  • the desulfurization step for example, desulfurization using a hydrogenation catalyst that converts a sulfur content into hydrogen sulfide and a hydrogen sulfide adsorbent can be employed.
  • a hydrogenation catalyst for example, a catalyst in which a metal such as nickel, cobalt, or molybdenum is supported on alumina or silica-alumina can be used.
  • the sulfur content is separated as hydrogen sulfide by reaction with hydrogen.
  • the hydrogen sulfide adsorbent include those that are adsorbed and removed by chemical reaction such as zinc oxide adsorbent and iron adsorbent, and those that are physically adsorbed such as activated carbon adsorbent. be able to.
  • the sulfur content it is preferable to reduce the sulfur content to 1 ppm or less.
  • Desulfurized biogas is mixed with a predetermined amount of water vapor, mixed with oxygen, and introduced into the reforming process.
  • an Rh-modified (Ni—CeO 2 ) —Pt catalyst is used as the catalyst used in the reforming process in the reforming step, and the combustion reaction and reforming reaction of the hydrocarbon gas are performed in the same reaction region. Progress at the same time.
  • Rh-modified (Ni—CeO 2 ) —Pt catalyst which is a quaternary catalyst, as a catalyst for the reforming reaction
  • a part of the hydrocarbon is completely burned, and the hydrocarbon is converted into CO 2 and H 2 O.
  • a combustion reaction that converts to The reforming reaction is an endothermic reaction and proceeds using the combustion heat generated by this combustion reaction.
  • the reforming reaction, CO 2 and H 2 O produced by combustion reaction, and of H 2 O was introduced as CO 2 and the raw material contained in the raw material biogas is reacted with residual hydrocarbons into H 2 and CO
  • the reforming reaction to be converted proceeds on the catalyst to convert hydrocarbons into H 2 and CO.
  • Rh-modified (Ni—CeO 2 ) —Pt catalyst can be obtained, for example, by supporting Rh on the surface of an alumina carrier having an appropriate surface area, then supporting Pt, and simultaneously supporting Ni and CeO 2. .
  • alumina carrier having an appropriate surface area
  • Pt palladium
  • Ni and CeO 2 nickel
  • various variations are possible for the selection of the material and shape of the carrier, the presence / absence of coating formation, and the selection of the material.
  • Rh is supported by impregnating an aqueous solution of a water-soluble salt of Rh, followed by drying, firing, and hydrogen reduction.
  • Pt is supported by impregnating an aqueous solution of a Pt water-soluble salt, followed by drying, firing, and hydrogen reduction.
  • Simultaneous loading of Ni and CeO 2 is performed by impregnating a mixed aqueous solution of a water-soluble salt of Ni and a water-soluble salt of Ce, followed by drying, firing, and hydrogen reduction.
  • Rh-modified (Ni—CeO 2 ) —Pt catalyst is obtained by the procedure exemplified above.
  • the hydrogen reduction treatment at each stage in the above may be omitted, and the catalyst may be used after hydrogen reduction at a high temperature in actual use.
  • the catalyst can be further reduced with hydrogen at a high temperature before use.
  • FIG. 2 shows an example of a synthesis gas production apparatus according to an embodiment to which the present invention is applied.
  • This apparatus includes a reformer 5, a desulfurizer 6, and a steam generator 15.
  • the reformer 5 is connected to a raw material gas introduction path 4 for introducing a raw material gas on the upstream side, and a reformed gas path 12 for leading the reformed gas to the downstream side.
  • the first heat exchanger 7, the second heat exchanger 8, the third heat exchanger 9, and the fourth heat exchanger are sequentially arranged from the upstream side close to the reformer 5 toward the downstream side. 10 and the 5th heat exchanger 11 is arrange
  • biogas, water vapor, and oxygen gas are introduced as source gases.
  • the biogas is introduced through the biogas introduction path 1, heated by heat exchange with the reformed gas in the third heat exchanger 9, and introduced into the desulfurizer 6.
  • the desulfurizer 6 is filled with a hydrogenation catalyst and a hydrogen sulfide adsorbent for performing the above-described desulfurization step.
  • the biogas desulfurized by the desulfurizer 6 is combined with water vapor and introduced into the mixed gas passage 19.
  • the water vapor is generated from pure water introduced from the pure water introduction path 2.
  • the pure water introduced from the pure water introduction path 2 is heated by heat exchange with the reformed gas in the fourth heat exchanger 10 and introduced into the steam generator 15.
  • the water vapor generator 15 generates water vapor from the introduced pure water.
  • the drain water discharged from the steam generator 15 is heated by heat exchange with the reformed gas in the second heat exchanger 8 and returned to the steam generator 15 again.
  • Water vapor generated from pure water by the water vapor generator 15 is introduced into the mixed gas passage 19 by the water vapor passage 18 and merged with the biogas.
  • Reference numeral 20 denotes a bypass path 20 that joins the mixed gas of biogas and water vapor to the raw material gas introduction path 4 without passing through the first heat exchanger 7.
  • the oxygen gas is introduced through the oxygen gas introduction path 3 and joined to the raw material gas introduction path 4.
  • oxygen gas is mixed with the mixed gas of biogas and water vapor, and here, the raw material gas in which the biogas, water vapor and oxygen gas are mixed is introduced into the reformer 5.
  • the reformer 5 is filled with the above-described Rh-modified (Ni—CeO 2 ) —Pt catalyst, and the combustion reaction and the reforming reaction of the hydrocarbon gas contained in the biogas are simultaneously advanced in the same reaction region. . While the reformed gas obtained by the reformer 5 passes through the reformed gas path 12, the first heat exchanger 7, the second heat exchanger 8, the third heat exchanger 9, and the fourth heat exchanger. 10. Passes through the fifth heat exchanger 11. The heat of the reformed gas is provided for each heat exchange. In the fifth heat exchanger 11, the reformed gas is cooled by the cooling water introduced from the cooling water introduction path 14.
  • the moisture is removed from the reformed gas cooled by the fifth heat exchanger 11 by the gas-liquid separator 13.
  • the reformed gas from which moisture has been removed is used for synthesis of methanol or the like as synthesis gas through the synthesis gas passage 17.
  • the water separated by the gas-liquid separator 13 is drained from the drainage channel 16.
  • Part of the synthesis gas passing through the synthesis gas path 17 is refluxed to the biogas introduction path 1 via the reflux path 21.
  • hydrogen gas required for hydrogenating and desulfurizing the sulfur component in the raw material biogas is supplied.
  • installation of the reflux path 21 is not essential.
  • the composition of the reformed gas obtained by the method and apparatus of the above embodiment is H 2 , CO, CH 4 , CO 2 , H 2 O.
  • the composition of the raw material gas used for the reforming reaction, the reforming temperature, and the reforming ratio are such that the ratio of hydrogen and carbon monoxide in the syngas, which is advantageous for methanol synthesis and FT synthesis, is theoretically about 2. Quality pressure was set based on the results of equilibrium calculations.
  • the above composition shows the molar ratio as follows.
  • CO 2 / C (carbon dioxide gas in raw material gas [mol]) / (carbon in raw material biogas [mol])
  • S / C (water content in raw material gas [mol]) / (carbon in raw material biogas [mol])
  • O 2 / C (Oxygen in source gas [mol]) / (Carbon in source biogas [mol])
  • synthesis gas mainly composed of carbon monoxide and hydrogen is obtained.
  • the resultant synthesis gas can be used for methanol synthesis or FT synthesis after it is further cooled and gas-liquid separated after using heat for raw material biogas temperature rise and steam production. In this way, a biogas having a high CO 2 concentration can be reformed without removing carbon dioxide in the pretreatment, and a synthesis gas that can be used for methanol synthesis or FT synthesis can be produced.
  • the composition of the reformed gas obtained by the method of the present embodiment is as follows.
  • CH 4 1.2%
  • CO 2 15.1%
  • H 2 O 20.8%
  • Table 1 shows the results of a case simulation in which the temperature at the inlet of the reformer 5 is 400 ° C. and the pressure at the outlet of the reformer 5 is 80 kPaG, 800 kPaG, and 2000 kPaG. In either case, the carbon activity value is 1 or less. That is, it was confirmed that the operation was possible without causing carbon deposition.
  • the carbon activity value is used as an index indicating the likelihood of carbon precipitation from the reformed gas.
  • the carbon activity value is a value calculated using an equilibrium constant determined from the partial pressure of CO, H 2 , CO 2 , and H 2 O and the temperature for each precipitation reaction. If the carbon activity value does not exceed 1, no carbon deposition occurs on equilibrium.
  • the reactions represented by the formulas (A) and (B) are equilibrium reactions, and whether or not carbon is precipitated depends on the partial pressure of CO, CO 2 , H 2 , and H 2 O in the reaction gas. It can be assumed from the temperature of the reaction gas.
  • A1 (carbon activity value with respect to reaction formula (A)) K1 ⁇ ( ⁇ CO) 2 / ( ⁇ CO 2 ) (formula (C))
  • A2 (carbon activity value with respect to reaction formula (B)) K2 ⁇ ( ⁇ CO) ⁇ ( ⁇ H 2 ) / ( ⁇ H 2 O)
  • K1 and K2 are equilibrium constants determined from the temperature.
  • Reference 1 Riki Oki, NTN TECHNICICAL REVIEW, N0.74, p. 42-49, 2006
  • Reference 2 Ishigami Yasuo, Osaka Prefectural Industrial Technology Research Institute report, No. 21, p. 9-16, 2007)
  • the reforming pressure was set.
  • synthesis gas for reforming biogas mainly composed of methane and carbon dioxide.
  • the synthesis gas was obtained by direct reforming without going through the step of previously removing CO 2 in the biogas.
  • Syngas could be generated at a ratio advantageous for methanol synthesis and FT synthesis.

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PCT/JP2016/066110 2015-06-17 2016-06-01 合成ガスの製造方法および装置 WO2016203944A1 (ja)

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