WO2014007059A1 - ガソリンを製造するシステム又は方法 - Google Patents
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- WO2014007059A1 WO2014007059A1 PCT/JP2013/066813 JP2013066813W WO2014007059A1 WO 2014007059 A1 WO2014007059 A1 WO 2014007059A1 JP 2013066813 W JP2013066813 W JP 2013066813W WO 2014007059 A1 WO2014007059 A1 WO 2014007059A1
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- 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
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- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/42—Catalytic treatment
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- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
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- 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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- 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
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- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
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- C10L1/00—Liquid carbonaceous fuels
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- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
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- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
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- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/06—Integration with other chemical processes
- C01B2203/061—Methanol production
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- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
- C01B2203/0827—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel at least part of the fuel being a recycle stream
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- 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
- C01B2203/1241—Natural gas or methane
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- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
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- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2200/00—Components of fuel compositions
- C10L2200/04—Organic compounds
- C10L2200/0461—Fractions defined by their origin
- C10L2200/0469—Renewables or materials of biological origin
- C10L2200/0492—Fischer-Tropsch products
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- C10L2270/00—Specifically adapted fuels
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- C10L2270/023—Specifically adapted fuels for internal combustion engines for gasoline engines
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- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/10—Recycling of a stream within the process or apparatus to reuse elsewhere therein
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- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/42—Fischer-Tropsch steps
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- 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 present invention relates to a system or method for producing gasoline, and more particularly to a system or method for producing gasoline from methanol from natural gas.
- JP-B-62-41276 steam-treats natural gas to produce synthesis gas, synthesize methanol from this synthesis gas, and further synthesize gasoline from this methanol
- the method is described.
- a large amount of water is produced in addition to gasoline, but how to use this water has not been studied so far.
- the present invention is a system for producing gasoline from natural gas via methanol, the steam reforming apparatus for steam reforming natural gas using water to produce a reformed gas, and A methanol synthesis apparatus for synthesizing methanol from the reformed gas generated by the steam reforming apparatus, a gasoline synthesis apparatus for generating gasoline and water from methanol synthesized by the methanol synthesis apparatus, and water generated by the gasoline synthesis apparatus And a line for supplying the steam reformer to utilize it for steam reforming of natural gas.
- the system according to the present invention comprises a carbon dioxide recovery device for recovering carbon dioxide from exhaust gas generated by the steam reforming device, and a line for supplying carbon dioxide recovered by the carbon dioxide recovery device to the steam reforming device. You may provide further.
- a method of producing gasoline from natural gas via methanol the step of steam reforming natural gas using water to produce a reformed gas;
- the method according to the present invention may further include the steps of recovering carbon dioxide from the exhaust gas generated in the steam reforming of the natural gas, and adding the recovered carbon dioxide to the steam reforming of the natural gas.
- FIG. 1 is a schematic view showing an embodiment of a system for producing gasoline from methanol according to the present invention via methanol. It is a schematic diagram which shows another embodiment of the system which manufactures gasoline from the natural gas which concerns on this invention via methanol.
- the system includes a boiler 10 for generating steam, a steam reformer 20 for steam reforming natural gas to produce a reformed gas, and a steam reformer.
- a methanol synthesis column 30 which synthesizes methanol from the generated reformed gas
- a gasoline synthesis column 50 which synthesizes gasoline from methanol synthesized in the methanol synthesis column, and water which is generated in the gasoline synthesis column is reused in a steam reformer
- a water recovery line 61 for recovery for recovery.
- the boiler 10 is not particularly limited as long as it is an apparatus for boiling water to steam.
- the boiler 10 includes a water supply line 11 to which water for the boiler is supplied, a drainage line 12 which discharges the wastewater generated in the boiler, and a steam supply line 13 which supplies steam generated in the boiler to the steam reformer 20. Prepare.
- the steam reformer 20 is provided with a reaction tube (not shown) filled with a steam reforming catalyst, and in this reaction tube, hydrogen, carbon monoxide and natural gas containing methane as a main component are produced by the following reaction. Produces carbon dioxide.
- a steam reforming catalyst for example, a known catalyst such as a nickel-based catalyst can be used. CH 4 + H 2 O ⁇ 3H 2 + CO (Equation 1)
- a natural gas supply line 21 to which natural gas is supplied is connected to the inlet side of the reaction tube of the steam reformer 20.
- a reformed gas supply line 22 for supplying a reformed gas containing hydrogen, carbon monoxide and carbon dioxide generated by the steam reforming reaction as main components to the methanol synthesis column 30 is connected to the outlet side of the reaction tube. .
- the reformed gas supply line 22 is provided with a steam return line 23 for returning the water, which is a part of the reformed gas in the line, as steam to the steam reformer 20. Further, the reformed gas supply line 22 is provided with a water recovery line 61a for recovering the condensed water as water.
- the methanol synthesis column 30 is an apparatus for synthesizing methanol from a reformed gas by the following reaction. 3H 2 + CO ⁇ CH 3 OH + H 2 (Equation 2)
- the methanol synthesis column 30 is equipped with a methanol synthesis catalyst packed therein.
- a known catalyst such as a copper-based catalyst can be used as the methanol synthesis catalyst.
- the reformed gas supply line 22 is connected to the inlet side of the methanol synthesis column 30, and the crude methanol supply line 31 for supplying the crude methanol synthesized by the methanol synthesis column 30 to the distillation column 40 is connected to the outlet side.
- Crude methanol contains water in addition to methanol.
- the distillation column 40 is an apparatus for separating water from the crude methanol by distillation.
- the distillation column 40 is connected to a methanol supply line 41 for supplying purified methanol to the gasoline synthesis column 50, and a distilled water recovery line 42 for recovering distilled water separated from the methanol and supplying the distilled water to the steam reformer 30.
- the gasoline synthesis tower 50 is an apparatus for synthesizing gasoline from methanol by the reaction represented by the following equation. nCH 3 OH ⁇ n (CH 2 ) + nH 2 O (Equation 3)
- methanol produces gasoline and water at a molar ratio of 1 to 1 as shown in equation 3.
- the synthesis of gasoline from methanol proceeds through the synthesis of dimethyl ether (DME) from methanol, followed by the synthesis of DME into gasoline. Therefore, in the gasoline synthesis tower 50, two types of catalysts, a DME synthesis catalyst and a gasoline synthesis catalyst, can be provided in two stages, and two reactions can be advanced stepwise.
- a catalyst for DME synthesis for example, a known catalyst such as an aluminosilicate type zeolite catalyst can be used.
- known catalysts such as aluminosilicate type zeolite catalysts can be used as aluminosilicate type zeolite catalysts can be used.
- the gasoline synthesis tower 50 is connected to a gasoline supply line 51 for supplying the gasoline synthesized in the gasoline synthesis tower to a storage facility or the like (not shown).
- LPG supply line 52 may be separately connected since liquefied natural gas (LPG) is by-produced in addition to gasoline.
- LPG liquefied natural gas
- the gasoline synthesis tower 50 as shown in Formula 3, a large amount of water is generated, so the water recovery line 61b for recovering this water is connected.
- the gasoline synthesis tower 50 although a mixture of gasoline and water is obtained, these form two phases of an aqueous phase and an oil phase according to specific gravity, and therefore, by providing an oil / water separator (not shown), it is easily done. It can be separated.
- the property of drainage flowing through the water recovery line 61b is, for example, a methanol concentration of 1 wt% or less, ethanol of 10 wtppm or less, other alcohols of 1 wtppm or less, and an oil component of 1 wt% or less.
- the water recovery line 61b of the gasoline synthesis tower 50 is connected to the demineralizer 60 together with the water recovery line 61a at the rear stage of the steam reformer 20.
- the demineralizer 60 is an apparatus for removing impurities in the recovered water in order to make the recovered water usable in the boiler 10.
- As boiler water it is preferable to make it the composition which satisfy
- the composition is shown in the following table.
- the demineralizer 60 mainly uses activated carbon for removing organic impurities, ion exchange resin for mainly removing ionic impurities, and gas components in the liquid.
- the demineralizer 60 is connected to a water recycling line 62 supplied to the water supply line 11 of the boiler 10 in order to reuse the treated water treated by the demineralizer as steam for steam reforming, as well as desalting.
- the drainage line 63 for discharging the drainage generated by the treatment in the apparatus is connected.
- water is supplied to the boiler 10 via the water supply line 11.
- the steam generated in the boiler 10 is supplied to the steam reformer 20 through the steam supply line 13, and natural gas is supplied to the steam reformer 20 through the natural gas supply line 21.
- the natural gas is steam-reformed by the reaction of the above equation 1 at a predetermined high temperature, and is converted into a reformed gas mainly composed of hydrogen, carbon monoxide and carbon dioxide.
- the reformed gas is supplied to the methanol synthesis column 30 via the reformed gas supply line 22.
- a part of the reformed gas is returned to the steam reformer 20 by the steam return line 23 as steam, and is used for the steam reforming reaction.
- the proportion of water vapor from the water vapor return line 23 to the water vapor supplied to the steam reformer 20 is preferably, for example, 10 to 30%.
- the ratio of steam to methane in natural gas is theoretically 1 to 1 as shown in Formula 1, in order to efficiently carry out the steam reforming reaction, supplying an excess of steam Is preferred.
- 2.5 to 3.5 moles of water vapor can be supplied per mole of carbon in natural gas.
- a part of the reformed gas is supplied as water to the demineralizer 60 via the water recovery line 61a.
- methanol is synthesized from the reformed gas by the reaction of Formula 2 above.
- Methanol synthesized in the methanol synthesis column 30 is supplied to the distillation column 40 via the crude methanol supply line 31 as crude methanol containing water.
- the methanol purified by the distillation column 40 is supplied to the gasoline synthesis column 50 via the methanol supply line 41.
- the distilled water separated from the crude methanol in the distillation column 40 is supplied to the steam reformer 20 through the steam return line 23 through the distilled water recovery line 42.
- gasoline is synthesized from methanol by the reaction of Formula 3 above.
- the gasoline is stored in a predetermined storage facility via a gasoline supply line 51, and the by-product LPG is stored in a predetermined storage facility via an LPG supply line 52. Further, the water generated in the gasoline synthesis tower 50 is supplied to the demineralizer 60 via the water recovery line 61b.
- the water recovered by the water recovery line 61 is treated to remove impurities to a degree that can be used by the boiler 10.
- Treated water is supplied to the boiler 10 through the water supply line 11 via the water reuse line 61. Further, the wastewater generated by the demineralizer 60 is drained through the drainage line 62.
- the amount of water in the input and the amount of water in the output are the same, and gasoline synthesis
- the amount of water is balanced. Therefore, it is difficult to obtain fresh water that can be used for steam reforming in places such as desert and ocean where natural gas is produced, but in the present invention, it is possible to use steam reforming easily in the system. I can drink water.
- FIG. 2 An embodiment shown in FIG. 2 will be described.
- the same components as those of the system shown in FIG. 1 are designated by the same reference numerals and their detailed description will be omitted.
- the system of the present embodiment is the system shown in FIG. 1 with the addition of a configuration for reusing the exhaust gas of the steam reformer 20.
- the steam reformer 20 includes an exhaust gas passage 71 for exhausting the combustion exhaust gas from the combustion device (not shown) for heating to a predetermined temperature to perform steam reforming from the chimney 72. , an exhaust gas extraction line 74 for extracting a part from the exhaust gas passage 71 of the gas, the CO 2 recovery apparatus 73 that collects carbon dioxide in the withdrawn gas, CO 2 reuse adding the recovered carbon dioxide to the natural gas supply line 21 And a line 75.
- the CO 2 recovery device 73 is not particularly limited as long as it can separate and recover carbon dioxide in the combustion exhaust gas, but, for example, a device of a system using a carbon dioxide absorbing liquid can be used.
- the exhaust gas is discharged from the combustion device (not shown) for heating the steam reformer 20 to a predetermined temperature via the exhaust gas passage 71.
- a part of the exhaust gas is supplied to the CO 2 recovery unit 73 through the exhaust gas extraction line 74 to separate and recover carbon dioxide.
- the recovered carbon dioxide is supplied to the steam reformer 20 through the natural gas supply line 21 through the CO 2 recycle line 75.
- the carbon dioxide thus recovered is partially converted to carbon monoxide in the steam reformer 20 and is supplied to the methanol synthesis column 30.
- the reaction of Formula 4 below also occurs due to the presence of carbon dioxide.
- excess hydrogen reacts with carbon dioxide to produce methanol and water. That is, compared to the embodiment shown in FIG. 1, more water can be generated.
- This water is separated from the crude methanol in the distillation column 40 and recycled to the steam reformer 20 through the distilled water recovery line 42.
- the amount of output water is increased compared to the amount of input water, it is also possible to reuse it as make-up water for the boiler 10 in addition to reuse for the steam reformer 20. it can.
- the distillation column 40 is disposed between the methanol synthesis column 30 and the gasoline synthesis column 50, but as shown in equation 3, water is by-produced in gasoline synthesis.
- the crude methanol obtained in the methanol synthesis column 30 may be supplied as it is to the gasoline synthesis column 50 through the crude methanol supply line 22 without being distilled.
- the water balance was simulated for the embodiment shown in FIG. The results are shown in Table 2. In addition, the simulation was performed in the case of 2500 tons of methanol production amount per day. The raw material was used under the condition of using natural gas.
- the steam supplied to the steam reformer needs to be supplied in excess compared to the supply amount of natural gas, and about 200 tons / h of steam (the sum of the steam supply line and the steam return line) Was necessary. About 25% of them return the steam discharged from the steam reformer, and the rest recovers the water generated in the gasoline synthesis tower etc. and uses it to feed most of the steam supplied to the steam reformer from within the system It was possible.
- the production of gasoline was 8135 barrels per day, and the production of LPG was 122 tons per day.
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Abstract
Description
CH4+H2O→3H2+CO・・・(式1)
3H2+CO→CH3OH+H2・・・(式2)
nCH3OH→n(CH2)+nH2O・・・(式3)
3H2+CO→CH3OH+H2・・・(式2)
H2+CO2→CH3OH+H2O・・・(式4)
11 水供給ライン
12 排水ライン
13 水蒸気供給ライン
20 スチームリフォーマ
21 天然ガス供給ライン
22 改質ガス供給ライン
23 水蒸気戻りライン
30 メタノール合成塔
31 粗メタノール供給ライン
40 蒸留塔
41 メタノール供給ライン
42 蒸留水回収ライン
50 ガソリン合成塔
51 ガソリン供給ライン
52 LPG供給ライン
60 脱塩装置
61 水回収ライン
62 水再利用ライン
63 排水ライン
71 排ガス路
72 煙突
73 CO2回収装置
74 排ガス抽出ライン
75 CO2再利用ライン
Claims (4)
- 天然ガスからメタノールを経由してガソリンを製造するシステムであって、
水を利用して天然ガスを水蒸気改質して改質ガスを生成する水蒸気改質装置と、
前記水蒸気改質装置で生成した改質ガスからメタノールを合成するメタノール合成装置と、
前記メタノール合成装置で合成したメタノールからガソリンと水を生成するガソリン合成装置と、
前記ガソリン合成装置で生成した水を、天然ガスの水蒸気改質に利用するために前記水蒸気改質装置に供給するラインと
を備えるシステム。 - 前記水蒸気改質装置で発生する排ガスから二酸化炭素を回収する二酸化炭素回収装置と、前記二酸化炭素回収装置で回収した二酸化炭素を前記水蒸気改質装置に供給するラインとを更に備える請求項1に記載のシステム。
- 天然ガスからメタノールを経由してガソリンを製造する方法であって、
水を利用して天然ガスを水蒸気改質して、改質ガスを生成するステップと、
前記改質ガスからメタノールを合成するステップと、
前記メタノールからガソリンと水を生成するステップと、
前記ガソリン合成の際に生成した水を、前記天然ガスの水蒸気改質に再利用するステップと
を含む方法。 - 前記天然ガスの水蒸気改質で発生する排ガスから二酸化炭素を回収するステップと、この回収した二酸化炭素を前記天然ガスの水蒸気改質に加えるステップとを更に含む請求項
3に記載の方法。
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DE112013003409.3T DE112013003409B4 (de) | 2012-07-06 | 2013-06-19 | System oder Verfahren zur Herstellung von Benzin |
US14/406,668 US20150184082A1 (en) | 2012-07-06 | 2013-06-19 | System and method for producing gasoline |
BR112014031631-7A BR112014031631A2 (pt) | 2012-07-06 | 2013-06-19 | sistema ou método para produzir gasolina |
AU2013284667A AU2013284667B2 (en) | 2012-07-06 | 2013-06-19 | Gasoline manufacturing system or method |
RU2014152636/04A RU2599629C2 (ru) | 2012-07-06 | 2013-06-19 | Система и способ для производства бензина |
CA2876050A CA2876050C (en) | 2012-07-06 | 2013-06-19 | System or method for producing gasoline |
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JP2012152451A JP6016486B2 (ja) | 2012-07-06 | 2012-07-06 | ガソリンを製造するシステム又は方法 |
JP2012-152451 | 2012-07-06 |
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US (1) | US20150184082A1 (ja) |
JP (1) | JP6016486B2 (ja) |
AU (1) | AU2013284667B2 (ja) |
BR (1) | BR112014031631A2 (ja) |
CA (1) | CA2876050C (ja) |
DE (1) | DE112013003409B4 (ja) |
RU (1) | RU2599629C2 (ja) |
WO (1) | WO2014007059A1 (ja) |
Citations (3)
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JP2001097906A (ja) * | 1998-12-07 | 2001-04-10 | Mitsubishi Heavy Ind Ltd | メタノールの製造方法 |
JP2005336076A (ja) * | 2004-05-25 | 2005-12-08 | Mitsubishi Heavy Ind Ltd | 液体燃料製造プラント |
JP2009179591A (ja) * | 2008-01-30 | 2009-08-13 | Mitsubishi Chemicals Corp | メタノールの製造方法 |
Family Cites Families (9)
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US4048250A (en) * | 1975-04-08 | 1977-09-13 | Mobil Oil Corporation | Conversion of natural gas to gasoline and LPG |
DE2846693A1 (de) * | 1978-10-26 | 1980-05-08 | Metallgesellschaft Ag | Verfahren zur erzeugung von benzin aus synthesegas |
PE115299A1 (es) * | 1997-09-25 | 1999-12-16 | Shell Int Research | Procedimiento para la produccion de hidrocarburos liquidos |
RU2143417C1 (ru) * | 1998-07-27 | 1999-12-27 | Институт катализа им.Г.К.Борескова СО РАН | Способ получения моторных топлив из углеродсодержащего сырья |
DK1008577T4 (da) * | 1998-12-07 | 2006-06-06 | Mitsubishi Heavy Ind Ltd | Fremgangsmåde til fremstilling af methanol |
JP4959074B2 (ja) * | 2001-07-19 | 2012-06-20 | 三菱重工業株式会社 | メタノールの製造方法 |
CA2523219C (en) * | 2003-05-02 | 2012-06-12 | Johnson Matthey Plc | Production of hydrocarbons by steam reforming and fischer-tropsch reaction |
JPWO2007114250A1 (ja) * | 2006-03-30 | 2009-08-13 | 新日鉄エンジニアリング株式会社 | 液体燃料合成システム |
US8677762B2 (en) * | 2007-09-14 | 2014-03-25 | Haldor Topsoe A/S | Combined production of hydrocarbons and electrical power |
-
2012
- 2012-07-06 JP JP2012152451A patent/JP6016486B2/ja active Active
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2013
- 2013-06-19 BR BR112014031631-7A patent/BR112014031631A2/pt not_active Application Discontinuation
- 2013-06-19 AU AU2013284667A patent/AU2013284667B2/en active Active
- 2013-06-19 CA CA2876050A patent/CA2876050C/en active Active
- 2013-06-19 WO PCT/JP2013/066813 patent/WO2014007059A1/ja active Application Filing
- 2013-06-19 US US14/406,668 patent/US20150184082A1/en not_active Abandoned
- 2013-06-19 DE DE112013003409.3T patent/DE112013003409B4/de not_active Expired - Fee Related
- 2013-06-19 RU RU2014152636/04A patent/RU2599629C2/ru active
Patent Citations (3)
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JP2001097906A (ja) * | 1998-12-07 | 2001-04-10 | Mitsubishi Heavy Ind Ltd | メタノールの製造方法 |
JP2005336076A (ja) * | 2004-05-25 | 2005-12-08 | Mitsubishi Heavy Ind Ltd | 液体燃料製造プラント |
JP2009179591A (ja) * | 2008-01-30 | 2009-08-13 | Mitsubishi Chemicals Corp | メタノールの製造方法 |
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Also Published As
Publication number | Publication date |
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CA2876050A1 (en) | 2014-01-09 |
JP6016486B2 (ja) | 2016-10-26 |
RU2014152636A (ru) | 2016-08-27 |
BR112014031631A2 (pt) | 2021-08-24 |
DE112013003409T5 (de) | 2015-04-09 |
CA2876050C (en) | 2017-01-03 |
JP2014015508A (ja) | 2014-01-30 |
DE112013003409B4 (de) | 2018-03-15 |
AU2013284667A1 (en) | 2015-01-22 |
US20150184082A1 (en) | 2015-07-02 |
RU2599629C2 (ru) | 2016-10-10 |
AU2013284667B2 (en) | 2016-03-17 |
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