WO2011024997A1 - 航空燃料油組成物 - Google Patents
航空燃料油組成物 Download PDFInfo
- Publication number
- WO2011024997A1 WO2011024997A1 PCT/JP2010/064700 JP2010064700W WO2011024997A1 WO 2011024997 A1 WO2011024997 A1 WO 2011024997A1 JP 2010064700 W JP2010064700 W JP 2010064700W WO 2011024997 A1 WO2011024997 A1 WO 2011024997A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- oil
- fuel oil
- aviation fuel
- base material
- hydrogen
- Prior art date
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- 238000003918 potentiometric titration Methods 0.000 description 1
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- 239000002244 precipitate Substances 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 238000011027 product recovery Methods 0.000 description 1
- AOHJOMMDDJHIJH-UHFFFAOYSA-N propylenediamine Chemical compound CC(N)CN AOHJOMMDDJHIJH-UHFFFAOYSA-N 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 238000006057 reforming reaction Methods 0.000 description 1
- 229930195734 saturated hydrocarbon Natural products 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 239000003549 soybean oil Substances 0.000 description 1
- 235000012424 soybean oil Nutrition 0.000 description 1
- 238000007655 standard test method Methods 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 238000000629 steam reforming Methods 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 239000003760 tallow Substances 0.000 description 1
- 238000004227 thermal cracking Methods 0.000 description 1
- 150000003573 thiols Chemical class 0.000 description 1
- 229930192474 thiophene Natural products 0.000 description 1
- 150000003577 thiophenes Chemical class 0.000 description 1
- 229910000348 titanium sulfate Inorganic materials 0.000 description 1
- XJDNKRIXUMDJCW-UHFFFAOYSA-J titanium tetrachloride Chemical compound Cl[Ti](Cl)(Cl)Cl XJDNKRIXUMDJCW-UHFFFAOYSA-J 0.000 description 1
- UFTFJSFQGQCHQW-UHFFFAOYSA-N triformin Chemical compound O=COCC(OC=O)COC=O UFTFJSFQGQCHQW-UHFFFAOYSA-N 0.000 description 1
- ZXAUZSQITFJWPS-UHFFFAOYSA-J zirconium(4+);disulfate Chemical compound [Zr+4].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O ZXAUZSQITFJWPS-UHFFFAOYSA-J 0.000 description 1
Classifications
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, 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
- C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/50—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids in the presence of hydrogen, hydrogen donors or hydrogen generating compounds
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- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
- B01J23/42—Platinum
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- B01J27/186—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J27/188—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium with chromium, molybdenum, tungsten or polonium
- B01J27/19—Molybdenum
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
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- C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
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- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
- C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
- C10G65/043—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a change in the structural skeleton
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- 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
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/30—Physical properties of feedstocks or products
- C10G2300/308—Gravity, density, e.g. API
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- 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
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4018—Spatial velocity, e.g. LHSV, WHSV
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- 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
- C10G2300/80—Additives
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- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/08—Jet fuel
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, 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
- C10L2200/0407—Specifically defined hydrocarbon fractions as obtained from, e.g. a distillation column
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, 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
- C10L2200/0407—Specifically defined hydrocarbon fractions as obtained from, e.g. a distillation column
- C10L2200/043—Kerosene, jet fuel
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2230/00—Function and purpose of a components of a fuel or the composition as a whole
- C10L2230/22—Function and purpose of a components of a fuel or the composition as a whole for improving fuel economy or fuel efficiency
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2270/00—Specifically adapted fuels
- C10L2270/04—Specifically adapted fuels for turbines, planes, power generation
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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
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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 an aviation fuel oil composition.
- biomass energy derived from plants can effectively use carbon immobilized from carbon dioxide in the atmosphere by photosynthesis during the growth process of plants, so it does not lead to an increase in carbon dioxide in the atmosphere from the viewpoint of the life cycle, so-called It has the property of being carbon neutral.
- Biomass fuel is also very promising as an alternative energy for oil from the viewpoint of depletion of petroleum resources and rising crude oil prices.
- FAME fatty acid methyl ester oils
- triglyceride which is a general structure of animal and vegetable oils
- This FAME is considered to be used not only for diesel fuel but also for aviation fuel oil, so-called jet fuel.
- Airplanes are heavily fueled and have been greatly affected by the recent rise in crude oil prices. Under such circumstances, biomass fuel is attracting attention as an important item that plays a role as an alternative to petroleum as well as preventing global warming.
- biomass fuel is attracting attention as an important item that plays a role as an alternative to petroleum as well as preventing global warming.
- airlines are experimenting with the use of mixed FAMEs in petroleum-based jet fuel.
- FAME has concerns about low temperature performance and oxidation stability.
- aviation fuel is exposed to extremely low temperatures when flying at high altitudes, so extremely strict low-temperature performance standards have been established.
- FAME mixing with petroleum-based jet fuel is unavoidable. In fact, the mixing amount is inevitably low.
- oxidation stability the addition of antioxidants is stipulated in the aviation fuel standard, but considering the stability as a base material, the mixing ratio must be limited to a low concentration as well as low temperature performance. I don't get it.
- hydrocarbons obtained by this method does not contain oxygen or unsaturated bonds, and has the same properties as petroleum hydrocarbon fuel, so that it can be used at a higher concentration than FAME.
- the hydrocarbons obtained by these methods are generally low in density, and even when used as aviation fuel, there are concerns about a decrease in density when mixed at a high concentration and a resulting deterioration in fuel consumption.
- the present invention has been made in view of the above circumstances, and an object thereof is to provide an aviation fuel composition that has excellent life cycle characteristics and realizes an excellent fuel consumption rate.
- the present invention is obtained by refining a first raw material oil containing a sulfur-containing hydrocarbon compound and an oxygen-containing hydrocarbon compound derived from animal or vegetable oils or fats and the first raw material oil and crude oil.
- a first base material which is a fraction having a boiling point range of 140 to 280 ° C., obtained through a process of hydrotreating a second raw material oil which is a mixed oil with a petroleum base material, and a heavy oil cracking device
- an aviation fuel oil composition characterized by comprising a second base material having a boiling point range of 140 to 280 ° C. obtained from the above.
- the density at 15 ° C. of the second base material is preferably 800 kg / m 3 or more and 840 kg / m 3 or less.
- the first base material is periodically formed on a support made of a porous inorganic oxide containing two or more elements selected from aluminum, silicon, zirconium, boron, titanium, and magnesium in the presence of hydrogen.
- Table 1 Uses a catalyst carrying one or more metals selected from Group 6A and Group 8 elements, hydrogen pressure 2-13 MPa, liquid space velocity 0.1-3.0 h -1 , hydrogen / oil ratio It is preferably obtained through a step of hydrotreating the first or second feedstock under conditions of 150 to 1500 NL / L and reaction temperature of 150 to 480 ° C.
- the first base material is obtained by treating the hydrotreated oil obtained by the hydrotreating process of the first or second raw material oil with aluminum, silicon, zirconium, boron, titanium, magnesium in the presence of hydrogen.
- a catalyst comprising a porous inorganic oxide composed of a substance selected from zeolite and a metal selected from Group 8 elements on a periodic table, a hydrogen pressure of 2 to 13 MPa, a liquid space velocity of 0 It is preferably obtained through a further isomerization process under the conditions of 1 to 3.0 h ⁇ 1 , hydrogen / oil ratio of 250 to 1500 NL / L, and reaction temperature of 150 to 380 ° C.
- the aviation fuel oil composition of the present invention can further contain a third substrate which is an aviation fuel oil substrate obtained by refining crude oil, a synthetic aviation fuel oil substrate or a mixture thereof. .
- the aviation fuel oil composition of the present invention may further contain one or more additives selected from an antioxidant, an antistatic agent, a metal deactivator and an antifreezing agent.
- the aviation fuel oil composition of the present invention preferably satisfies the standard value of JIS K2209 “aviation turbine fuel oil”.
- the environmentally low load type aviation fuel oil composition which can make the outstanding life-cycle characteristic acquired from a carbon neutral characteristic and the outstanding fuel consumption rate compatible, and contributes to primary energy diversification is provided.
- a feedstock oil (first feedstock oil) containing a sulfur-containing hydrocarbon compound and an oxygen-containing hydrocarbon compound derived from animal and vegetable oils or fats, or petroleum obtained by refining the first feedstock oil and crude oil
- a raw material oil (second raw material oil) containing a base material is used.
- first and second feedstocks are sometimes collectively referred to as “feedstocks”.
- Examples of animal and vegetable oils and fats include beef tallow, rapeseed oil, camelina oil, soybean oil, palm oil, oils and fats produced by specific microalgae, hydrocarbons, and the like.
- Specific microalgae means algae that have the property of converting a part of nutrients in the body into hydrocarbon or oily form, for example, chlorella, squid damo, spirulina, euglena, botriococcus brownie, pseudocollistis Ellipsoidia can be mentioned.
- Chlorella, squid damo, spirulina and euglena are known to produce oils and fats
- Botriococcus brownie and pseudocollistis ellipsoidia are known to produce hydrocarbons.
- any oil or fat may be used as the animal or vegetable oil or fat, and waste oil after using these oils or fats may be used.
- wax esters extracted from microalgae and free fatty acids produced as a by-product in oil refining can also be used. That is, the animal and vegetable fats and oils according to the present invention include the above-mentioned waste oils of fats and oils, wax esters extracted from microalgae, free fatty acids produced as a by-product in the purification of fats and oils, and the like.
- the constituent ratio of each fatty acid group having a fatty acid carbon chain of 10 to 14 (fatty acid composition)
- the vegetable oils and fats considered from this viewpoint include coconut oil, palm kernel oil and camelina oil, and the oils and fats produced by specific microalgae include the oils and fats produced by Euglena. It is done. In addition, you may use said fats and oils individually by 1 type or in mixture of 2 or more types.
- the fatty acid composition is methyl prepared according to the standard oil analysis method (established by the Japan Oil Chemists' Society) (1991) “2.4.20.2-91 Preparation of fatty acid methyl ester (boron trifluoride-methanol method)”. Establish the ester oil analysis test method (established by the Japan Oil Chemists' Society) (1993) “2.4.21.3-77 fatty acid composition (FID temperature rising gas romatograph) using a temperature rising gas chromatograph equipped with a flame ionization detector (FID). It is a value obtained according to “method)” and indicates the constituent ratio (% by mass) of each fatty acid group constituting the oil or fat.
- FID flame ionization detector
- the sulfur-containing hydrocarbon compound contained in the raw material oil is not particularly limited, and specific examples include sulfides, disulfides, polysulfides, thiols, thiophenes, benzothiophenes, dibenzothiophenes, and derivatives thereof.
- the sulfur-containing hydrocarbon compound contained in the feedstock oil may be a single compound or a mixture of two or more. Further, a petroleum hydrocarbon fraction containing a sulfur content may be used as the sulfur-containing hydrocarbon compound.
- the sulfur content contained in the raw material oil is preferably 1 to 50 mass ppm, more preferably 5 to 30 mass ppm, still more preferably 10 to 20 mass ppm in terms of sulfur atoms, based on the total amount of the raw material oil. .
- the sulfur content in the present invention means the mass content of the sulfur content measured according to the method described in JIS K 2541 “Sulfur Content Test Method” or ASTM-5453.
- the sulfur-containing hydrocarbon compound contained in the raw material oil may be mixed in advance with the oxygen-containing hydrocarbon compound derived from the animal and plant oil and fat, and the mixture may be introduced into the reactor of the hydrorefining device, or derived from the animal and vegetable oil and fat.
- the oxygen-containing hydrocarbon compound to be introduced into the reactor it may be supplied before the reactor.
- the petroleum base material obtained by refining crude oil contained in the second feedstock is a fraction obtained by atmospheric distillation or vacuum distillation of crude oil, hydrodesulfurization, hydrocracking, fluid catalytic cracking. And a fraction obtained by a reaction such as catalytic reforming. One or more of these fractions can be contained in the feedstock.
- the petroleum base material obtained by refining crude oil may be a chemical-derived compound or a synthetic oil obtained via a Fischer-Tropsch reaction.
- the content ratio of the petroleum base material obtained by refining crude oil or the like in the second raw material oil is not particularly limited, but is preferably 20 to 70% by volume, more preferably 30 to 60% by volume.
- the first base material according to the present invention is a fraction having a boiling point range of 140 to 280 ° C. obtained through a process of hydrotreating a raw material oil (first or second raw material oil).
- the hydrotreatment preferably includes the following hydrotreatment steps.
- the hydrotreating conditions are as follows: the hydrogen pressure is 2 to 13 MPa, the liquid space velocity is 0.1 to 3.0 h ⁇ 1 , and the hydrogen / oil ratio is 150 to 1500 NL / L. More preferably, the hydrogen pressure is 2 to 13 MPa, the liquid space velocity is 0.1 to 3.0 h ⁇ 1 , the hydrogen / oil ratio is 150 to 1500 NL / L, and the hydrogen pressure is 3 Even more desirable are conditions of ⁇ 10.5 MPa, liquid hourly space velocity of 0.25 ⁇ 1.0 h ⁇ 1 , and hydrogen / oil ratio of 300 ⁇ 1000 NL / L. All of these conditions are factors that influence the reaction activity.
- the reaction temperature can be arbitrarily set in order to obtain the target decomposition rate or the target fraction yield of the heavy feed oil heavy fraction.
- the average temperature of the entire reactor is generally preferably in the range of 150 to 480 ° C., desirably 200 to 400 ° C., and more desirably 260 to 360 ° C.
- the reaction temperature is lower than 150 ° C, the reaction may not proceed sufficiently.
- the reaction temperature exceeds 480 ° C, the decomposition proceeds excessively, and the liquid product yield tends to decrease.
- a support made of a porous inorganic oxide containing two or more elements selected from aluminum, silicon, zirconium, boron, titanium and magnesium is used as a catalyst for the hydrogenation treatment.
- a catalyst carrying a metal selected from these elements is used as a catalyst for the hydrogenation treatment.
- a porous inorganic oxide composed of two or more elements selected from aluminum, silicon, zirconium, boron, titanium and magnesium is used.
- it is a porous inorganic oxide containing alumina, and other carrier constituents include silica, zirconia, boria, titania, magnesia and the like.
- it is a complex oxide containing at least one selected from alumina and other constituent components.
- phosphorus may be included as another component.
- the total content of components other than alumina is preferably 1 to 20% by weight, more preferably 2 to 15% by weight.
- the total content of components other than alumina is less than 1% by weight, a sufficient catalyst surface area cannot be obtained and the activity may be lowered.
- the content exceeds 20% by weight the acid content of the carrier Properties may increase, leading to a decrease in activity due to coke formation.
- phosphorus is included as a carrier constituent, its content is preferably 1 to 5% by weight, more preferably 2 to 3.5% by weight in terms of oxide.
- the raw material to be a precursor of silica, zirconia, boria, titania, and magnesia, which are carrier components other than alumina, is not particularly limited, and a solution containing general silicon, zirconium, boron, titanium, or magnesium can be used.
- magnesium magnesium nitrate or the like can be used.
- phosphorus phosphoric acid or an alkali metal salt of phosphoric acid can be used.
- the raw materials for the carrier constituents other than alumina be added in any step prior to the firing of the carrier.
- it may be added to an aluminum aqueous solution in advance and then an aluminum hydroxide gel containing these components, may be added to a prepared aluminum hydroxide gel, or water or an acidic aqueous solution may be added to a commercially available alumina intermediate or boehmite powder.
- a method of coexisting at the stage of preparing aluminum hydroxide gel is more desirable.
- the active metal of the hydrotreating catalyst contains at least one metal selected from Group 6A and Group 8 metals of the periodic table, preferably two or more metals selected from Groups 6A and 8 Contains.
- metals selected from Groups 6A and 8 Contains For example, Co—Mo, Ni—Mo, Ni—Co—Mo, Ni—W and the like can be mentioned. In the hydrogenation treatment, these metals are converted into sulfides and used.
- the content of the active metal is, for example, the total supported amount of W and Mo is preferably 12 to 35% by weight, more preferably 15 to 30% by weight based on the catalyst weight in terms of oxide. If the total supported amount of W and Mo is less than 12% by weight, the activity may decrease due to a decrease in the number of active points. If it exceeds 35% by weight, the metal is not effectively dispersed and is similarly active. May lead to a decrease in The total supported amount of Co and Ni is preferably 1.5 to 10% by weight, more preferably 2 to 8% by weight based on the catalyst weight in terms of oxide. If the total supported amount of Co and Ni is less than 1.5% by weight, a sufficient cocatalyst effect may not be obtained and the activity may be reduced. If it is more than 10% by weight, the metal is effective. In the same manner, there is a possibility of causing activity.
- the method for supporting the active metal on the carrier is not particularly limited, and a known method applied when producing a normal desulfurization catalyst can be used.
- a method of impregnating a catalyst carrier with a solution containing a salt of an active metal is preferably employed.
- an equilibrium adsorption method, a pore-filling method, an incident-wetness method, and the like are preferably employed.
- the pore-filling method is a method in which the pore volume of the support is measured in advance and impregnated with the same volume of the metal salt solution, but the impregnation method is not particularly limited, and the amount of metal supported Further, it can be impregnated by an appropriate method depending on the physical properties of the catalyst support.
- the reactor type of the hydrogenation process may be a fixed bed system. That is, hydrogen can take either a countercurrent or a cocurrent flow with respect to the raw material oil, or a combination of countercurrent and cocurrent flow having a plurality of reaction towers. As a general format, it is a down flow, and a gas-liquid twin parallel flow format can be adopted.
- the reactors may be used singly or in combination, and a structure in which one reactor is divided into a plurality of catalyst beds may be adopted.
- the hydrotreated oil hydrotreated in the reactor is fractionated into predetermined fractions through a gas-liquid separation process, a rectification process, and the like.
- gas-liquid separation equipment and other by-products are formed between the reactors and in the product recovery process.
- a gas removal device may be installed.
- a high-pressure separator or the like can be preferably exemplified.
- hydrogen gas is introduced from the inlet of the first reactor before or after passing through the heating furnace, but separately from this, the temperature in the reactor is controlled and the reactor is as much as possible. It may be introduced between the catalyst beds or between a plurality of reactors in order to maintain the hydrogen pressure throughout.
- the hydrogen thus introduced is referred to as quench hydrogen.
- the ratio of quench hydrogen to hydrogen introduced accompanying the feedstock is preferably 10 to 60% by volume, more preferably 15 to 50% by volume. When the ratio of quench hydrogen is less than 10% by volume, the reaction at the subsequent reaction site may not proceed sufficiently, and when it exceeds 60% by volume, the reaction near the reactor inlet may not proceed sufficiently.
- the raw material oil when hydrotreating the raw material oil, in order to suppress the heat generation amount in the hydrotreating reactor, the raw material oil may contain a specific amount of recycled oil. it can.
- the content of the recycled oil is preferably 0.5 to 5 times by mass with respect to the oxygenated hydrocarbon compound derived from animal and plant oils and fats, and the ratio is appropriately set within the above range according to the maximum use temperature of the hydrotreating reactor. Can be determined. Assuming that the specific heat of both is the same, if the two are mixed one-on-one, the temperature rise is half that of the case where the substance derived from animal and vegetable fats and oils is reacted alone. If it exists, it is because the reaction heat can fully be reduced.
- the content of recycled oil is more than 5 times the mass of the oxygen-containing hydrocarbon compound, the concentration of the oxygen-containing hydrocarbon compound decreases and the reactivity decreases, and the flow rate of piping etc. increases and the load is increased. Increase.
- the content of the recycled oil is less than 0.5 times the mass of the oxygen-containing hydrocarbon compound, the temperature rise cannot be sufficiently suppressed.
- the mixing method of the raw material oil and the recycled oil is not particularly limited.
- the raw material oil may be mixed in advance and the mixture may be introduced into the reactor of the hydrotreating apparatus, or when the raw material oil is introduced into the reactor, the reactor You may supply in the front
- a plurality of reactors can be connected in series and introduced between the reactors, or the catalyst layer can be divided and introduced between the catalyst layers in a single reactor.
- Recycled oil may contain a portion of hydrotreated oil obtained by removing by-product water, carbon monoxide, carbon dioxide, hydrogen sulfide, etc. after hydrotreating the feedstock oil. preferable. Further, a fraction obtained by isomerizing each of the light fraction, middle fraction and heavy fraction fractionated from hydrotreated oil, or fractionated from further isomerized hydrotreated oil. It is preferable to contain a part of the middle distillate.
- the hydrotreating of the present invention preferably includes a step of further isomerizing the hydrotreated oil obtained in the hydrotreating step.
- the sulfur content contained in the hydrotreated oil that is the raw material oil for the isomerization treatment is preferably 1 mass ppm or less, and more preferably 0.5 mass ppm. If the sulfur content exceeds 1 ppm by mass, the progress of hydroisomerization may be hindered. In addition, for the same reason, the reaction gas containing hydrogen introduced together with the hydrotreated oil needs to have a sufficiently low sulfur concentration, and is preferably 1 ppm by volume or less, and 0.5 volume. More preferably, it is ppm or less.
- the isomerization treatment step is preferably performed in the presence of hydrogen under the conditions of a hydrogen pressure of 2 to 13 MPa, a liquid space velocity of 0.1 to 3.0 h ⁇ 1 , and a hydrogen / oil ratio of 250 to 1500 NL / L. More preferably, the hydrogen pressure is 2.5 to 10 MPa, the liquid space velocity is 0.5 to 2.0 h ⁇ 1 , and the hydrogen / oil ratio is 380 to 1200 NL / L. It is more desirable to carry out under the conditions of 8 MPa, the liquid space velocity is 0.8 to 1.8 h ⁇ 1 , and the hydrogen / oil ratio is 350 to 1000 NL / L. All of these conditions are factors that influence the reaction activity.
- the hydrogen pressure and the hydrogen / oil ratio are less than the lower limit values, there is a risk of causing a decrease in reactivity or a rapid decrease in activity.
- the hydrogen / oil ratio exceeds the upper limit, excessive equipment investment such as a compressor may be required.
- the lower the liquid space velocity the more advantageous the reaction.
- a very large reaction tower volume is required, which tends to result in excessive capital investment. Tend not to progress sufficiently.
- the reaction temperature in the isomerization treatment step can be arbitrarily set in order to obtain the desired decomposition rate or the desired fraction yield of the heavy oil feed fraction, but it should be in the range of 150 to 380 ° C. Is preferable, the range of 240 to 380 ° C. is more preferable, and the range of 250 to 365 ° C. is particularly preferable.
- the reaction temperature is lower than 150 ° C., sufficient hydroisomerization reaction may not proceed.
- the reaction temperature is higher than 380 ° C., excessive decomposition or other side reaction proceeds, resulting in a liquid product fraction. There is a risk of lowering.
- a metal selected from elements of Group 8 of the periodic table on a carrier made of a porous inorganic oxide composed of a material selected from aluminum, silicon, zirconium, boron, titanium, magnesium and zeolite A catalyst in which one or more of these are supported is used.
- the porous inorganic oxide used as the support for the isomerization catalyst include alumina, titania, zirconia, boria, silica, and zeolite. In the present invention, among these, among titania, zirconia, boria, silica, and zeolite. What consists of at least 1 type and an alumina is preferable.
- the production method is not particularly limited, but any preparation method can be employed using raw materials in various sols, salt compounds, and the like corresponding to each element.
- the composite hydroxide or composite oxide such as silica alumina, silica zirconia, alumina titania, silica titania, and alumina boria
- the ratio of alumina to other oxides can be any ratio with respect to the support, but preferably alumina is 90% by mass or less, more preferably 60% by mass or less, more preferably 40% by mass or less, preferably Is 10% by mass or more, more preferably 20% by mass or more.
- Zeolite is a crystalline aluminosilicate, such as faujasite, pentasil, mordenite, etc., which is ultra-stabilized by a predetermined hydrothermal treatment and / or acid treatment, or one whose alumina content in the zeolite is adjusted is used. be able to.
- faujasite and mordenite particularly preferably Y type and beta type are used.
- the Y type is preferably ultra-stabilized, and the zeolite that has been super-stabilized by hydrothermal treatment forms new pores in the range of 20 to 100 mm in addition to the original pore structure called micropores of 20 mm or less.
- Known conditions can be used for the hydrothermal treatment conditions.
- the active metal of the isomerization catalyst one or more metals selected from Group 8 elements of the periodic table are used.
- these metals it is preferable to use one or more metals selected from Pd, Pt, Rh, Ir, Au, and Ni, and it is more preferable to use them in combination.
- Suitable combinations include, for example, Pd—Pt, Pd—Ir, Pd—Rh, Pd—Au, Pd—Ni, Pt—Rh, Pt—Ir, Pt—Au, Pt—Ni, Rh—Ir, Rh— Examples thereof include Au, Rh—Ni, Ir—Au, Ir—Ni, Au—Ni, Pd—Pt—Rh, Pd—Pt—Ir, and Pt—Pd—Ni.
- the total content of active metals based on the catalyst mass is preferably 0.1 to 2% by mass, more preferably 0.2 to 1.5% by mass, and 0.5 to 1.3% by mass as the metal. Even more preferred. If the total supported amount of the metal is less than 0.1% by mass, the active sites tend to decrease and sufficient activity cannot be obtained. On the other hand, if it exceeds 2% by mass, the metal is not effectively dispersed and sufficient activity tends not to be obtained.
- the method for supporting the active metal on the support is not particularly limited, and a known method applied when producing a normal desulfurization catalyst can be used.
- a method of impregnating a catalyst carrier with a solution containing a salt of an active metal is preferably employed.
- an equilibrium adsorption method, a pore-filling method, an incident-wetness method, and the like are preferably employed.
- the pore-filling method is a method in which the pore volume of the support is measured in advance and impregnated with the same volume of the metal salt solution, but the impregnation method is not particularly limited, and the amount of metal supported Further, it can be impregnated by an appropriate method depending on the physical properties of the catalyst support.
- the isomerization catalyst used in the present invention is preferably subjected to a reduction treatment of active metal contained in the catalyst before being subjected to the reaction.
- the reduction conditions are not particularly limited, but the reduction is performed by treatment at a temperature of 200 to 400 ° C. in a hydrogen stream.
- the treatment is preferably performed in the range of 240 to 380 ° C.
- the reduction temperature is less than 200 ° C., the reduction of the active metal does not proceed sufficiently and the hydrodeoxygenation and hydroisomerization activity may not be exhibited. Further, when the reduction temperature exceeds 400 ° C., the aggregation of the active metal proceeds, and there is a possibility that the activity cannot be exhibited similarly.
- the reactor type for the isomerization treatment may be a fixed bed system. That is, hydrogen can take either a countercurrent or a cocurrent flow with respect to the raw material oil, or a combination of countercurrent and cocurrent flow having a plurality of reaction towers. As a general format, it is a down flow, and a gas-liquid twin parallel flow format can be adopted.
- the reactors may be used singly or in combination, and a structure in which one reactor is divided into a plurality of catalyst beds may be adopted.
- hydrogen gas is introduced from the inlet of the first reactor before or after passing through the heating furnace, but separately from this, the temperature in the reactor is controlled and the reactor is as much as possible. It may be introduced between the catalyst beds or between a plurality of reactors in order to maintain the hydrogen pressure throughout.
- the hydrogen thus introduced is referred to as quench hydrogen.
- the ratio of quench hydrogen to hydrogen introduced accompanying the feedstock is preferably 10 to 60% by volume, more preferably 15 to 50% by volume. When the ratio of quench hydrogen is less than 10% by volume, the reaction at the subsequent reaction site may not proceed sufficiently, and when it exceeds 60% by volume, the reaction near the reactor inlet may not proceed sufficiently.
- the isomerized oil obtained after the isomerization process may be fractionated into a plurality of fractions in a rectifying column as necessary.
- it may be fractionated into light fractions such as gas and naphtha fractions, middle fractions such as kerosene and diesel oil fractions, and heavy fractions such as residues.
- the cut temperature of the light fraction and the middle fraction is preferably 100 to 200 ° C, more preferably 120 to 180 ° C, further preferably 120 to 160 ° C, and still more preferably 130 to 150 ° C.
- the cut temperature of the middle fraction and the heavy fraction is preferably 250 to 360 ° C, more preferably 250 to 320 ° C, further preferably 250 to 300 ° C, and still more preferably 250 to 280 ° C.
- Hydrogen can be produced by reforming a part of the light hydrocarbon fraction produced in a steam reformer.
- the hydrogen produced in this way has a characteristic of carbon neutral because the raw material used for steam reforming is a biomass-derived hydrocarbon, and can reduce the burden on the environment.
- the middle fraction obtained by fractionating isomerized oil can be suitably used as an aviation fuel oil base material.
- the second base material contained in the aviation fuel oil composition of the present invention is a fraction having a boiling point range of 140 to 280 ° C. obtained from a heavy oil cracker.
- the heavy oil cracking device for obtaining the second base material is a fluid catalytic cracking device using a normal pressure residual oil from the normal pressure distillation device or a vacuum residual oil from the vacuum distillation device as a raw material, or a vacuum distillation device.
- General equipment such as hydrocracking equipment and thermal cracking equipment using a vacuum residue as a raw material can be used, but the density of aviation fuel oil fractions produced therefrom at 15 ° C.
- the aviation fuel oil base material according to the present invention may contain only the first base material and the second base material, but is obtained by refining crude oil as the third base material. It may further contain an aviation fuel oil base, a synthetic aviation fuel base or a mixture thereof.
- the third base material is an aviation fuel oil fraction obtained in a general petroleum refining process, a synthesis gas composed of hydrogen and carbon monoxide as a raw material, and a synthesis obtained via a Fischer-Tropsch reaction, etc. Aviation fuel oil base materials and the like are included. Synthetic aviation fuel base materials contain little aromatics, are characterized by saturated hydrocarbons and have a high smoke point. In addition, a well-known method can be used as a manufacturing method of synthesis gas, and it is not specifically limited.
- the aviation fuel oil composition of the present invention can further contain various additives conventionally added to aviation fuel oil.
- additives one or more additives selected from an antioxidant, an antistatic agent, a metal deactivator and an antifreezing agent are preferable.
- Antioxidants include N, N-diisopropylparaphenylenediamine, 2,6-ditertiary butylphenol 75% or more in a range not exceeding 24.0 mg / l in order to suppress the generation of gum in aviation fuel oil.
- tertiary and tritertiary butylphenol a mixture of 25% or less of tertiary and tritertiary butylphenol, a mixture of 72% or more of 2,4-dimethyl-6-tertiary butylphenol and 28% or less of monomethyl and dimethyl tertiary butylphenol, 2,4-dimethyl-6-tersia
- a mixture of 55% or more of butylphenol and 45% or less of tertiary and ditertiary butylphenol, 2,6-ditertiary butyl-4-methylphenol and the like can be added.
- the range does not exceed 3.0 mg / l in order to increase the electrical conductivity. Then, STADIS 450 manufactured by Octel Co., Ltd. can be added.
- N, N-disalicylidene is used in a range not exceeding 5.7 mg / l so that the free metal component contained in the aviation fuel oil does not react and the fuel becomes unstable. 1,2-propanediamine and the like can be added.
- ethylene glycol monomethyl ether or the like is added in the range of 0.1 to 0.15% by volume in order to prevent a minute amount of water contained in aviation fuel oil from freezing and blocking the piping. be able to.
- optional additives such as an antistatic agent, a corrosion inhibitor and a bactericide can be appropriately blended without departing from the present invention.
- the aviation fuel oil composition of the present invention preferably satisfies the standard value of JIS K2209 “aviation turbine fuel oil”.
- Density at 15 °C aviation fuel oil composition of the present invention is preferably 775 kg / m 3 or more, more preferably 780 kg / m 3 or more. On the other hand, from the viewpoint of flammability, it is preferably 839kg / m 3 or less, more preferably 830 kg / m 3 or less, and more preferably 820 kg / m 3 or less.
- the density at 15 ° C. means a value measured by JIS K2249 “Crude oil and petroleum products—density test method and density / mass / capacity conversion table”.
- the 10% by volume distillation temperature is preferably 204 ° C. or lower, more preferably 200 ° C. or lower, from the viewpoint of evaporation characteristics.
- the end point is preferably 300 ° C. or less, more preferably 290 ° C. or less, and still more preferably 280 ° C. or less from the viewpoint of combustion characteristics (burn-out property).
- the distillation property means a value measured by JIS K2254 “Petroleum products—distillation test method”.
- the actual gum content of the aviation fuel oil composition of the present invention is preferably 7 mg / 100 ml or less, more preferably 5 mg / 100 ml or less, from the viewpoint of preventing problems due to precipitate formation in the fuel introduction system and the like. More preferably, it is 3 mg / 100 ml or less.
- the real gum part here means the value measured by JIS K2261 "Gasoline and aviation fuel oil real gum test method".
- the true calorific value of the aviation fuel oil composition of the present invention is preferably 42.8 MJ / kg or more, and more preferably 45 MJ / kg or more, from the viewpoint of fuel consumption rate.
- the true calorific value here means a value measured by JIS K2279 “Crude oil and fuel oil calorific value test method”.
- the kinetic viscosity of the aviation fuel oil composition of the present invention is such that the kinematic viscosity at ⁇ 20 ° C. is preferably 8 mm 2 / s or less, and 7 mm 2 / s or less, from the viewpoint of fluidity of fuel piping and uniform fuel injection. More preferably, it is 5 mm ⁇ 2 > / s or less.
- kinematic viscosity here means the value measured by JIS K2283 "Kinematic viscosity test method of crude oil and petroleum products".
- the copper plate corrosion of the aviation fuel oil composition of the present invention is preferably 1 or less from the viewpoint of the corrosiveness of the fuel tank and piping.
- the copper plate corrosion here means a value measured by JIS K2513 “Petroleum products—Copper plate corrosion test method”.
- the aromatic content of the aviation fuel oil composition of the present invention is preferably 25% by volume or less, and more preferably 20% by volume from the viewpoint of flammability (preventing soot generation).
- the aromatic content here means a value measured by JIS K2536 “Testing method for fuel oil hydrocarbon components (fluorescence indicator adsorption method)”.
- the smoke point of the aviation fuel oil composition of the present invention is preferably 25 mm or more, more preferably 27 mm or more, and further preferably 30 mm or more from the viewpoint of flammability (preventing soot generation).
- the smoke point here means a value measured by JIS K2537 “Fuel oil smoke point test method”.
- the sulfur content of the aviation fuel oil composition of the present invention is preferably 0.3% by mass or less, more preferably 0.2% by mass or less, and 0.1% by mass or less from the viewpoint of corrosiveness. More preferably. From the same corrosive viewpoint, the mercaptan sulfur content is preferably 0.003% by mass or less, more preferably 0.002% by mass or less, and 0.001% by mass or less. Further preferred.
- the sulfur content mentioned here is the value measured by JIS K2541 “Crude oil and petroleum product sulfur test method”, and the mercaptan sulfur content is measured by JIS K2276 “Mercaptan sulfur content test method (potentiometric titration method)”. Value.
- the flash point of the aviation fuel oil composition of the present invention is preferably 38 ° C. or higher, more preferably 40 ° C. or higher, and further preferably 45 ° C. or higher from the viewpoint of safety.
- the flash point here means a value obtained by JIS K2265 “Crude oil and petroleum products—flash point test method—tag sealed flash point test method”.
- the total acid value of the aviation fuel oil composition of the present invention is preferably 0.1 mgKOH / g or less, more preferably 0.08 mgKOH / g or less, and 0.05 mgKOH / g or less from the viewpoint of corrosivity. More preferably.
- the total acid value here means a value measured by JIS K2276 “Total Acid Value Test Method”.
- the precipitation point of the aviation fuel oil composition of the present invention is preferably ⁇ 47 ° C. or less, preferably ⁇ 48 ° C. or less, from the viewpoint of preventing a decrease in fuel supply due to fuel freezing under low temperature exposure during flight. More preferably, the temperature is ⁇ 50 ° C. or lower.
- the precipitation point here means a value measured by JIS K2276 “Precipitation point test method”.
- the thermal stability of the aviation fuel oil composition of the present invention is such that the pressure difference in method A is 10.1 kPa or less, the preheating tube deposit evaluation value is less than 3, from the viewpoint of preventing fuel filter blockage due to the formation of precipitates at high temperature exposure, It is preferable that the pressure difference in the method B is 3.3 kPa or less and the preheating tube deposit evaluation value is less than 3.
- the thermal stability means a value measured by JIS K2276 “thermal stability test method A method, B method”.
- the water solubility of the aviation fuel oil composition of the present invention is preferably 2 or less in the separated state and 1b or less in the interface state in order to prevent troubles due to precipitation of dissolved water during low temperature exposure.
- the water solubility herein means a value measured by JIS K2276 “Water solubility test method”.
- the aviation fuel oil base material and the aviation fuel oil composition containing the environmentally low load base material manufactured using the animal and vegetable oils and fats of the present invention as raw materials have all of combustibility, oxidation stability, and life cycle CO 2 emission characteristics. It is excellent.
- the obtained kneaded material was extruded into a shape of a cylinder having a diameter of 1.5 mm by an extrusion molding machine, dried at 110 ° C. for 1 hour, and then fired at 550 ° C. to obtain a molded carrier.
- 50 g of the obtained shaped carrier was placed in an eggplant-shaped flask and 17.3 g of molybdenum trioxide, 13.2 g of nickel nitrate (II) hexahydrate, 3.9 g of phosphoric acid (concentration 85%) while degassing with a rotary evaporator. And an impregnation solution containing 4.0 g of malic acid was poured into the flask. The impregnated sample was dried at 120 ° C.
- Catalyst A Table 1 shows the physical properties of Catalyst A.
- Example 1 Dimethyl sulfide was added to vegetable oil 1 having the properties shown in Table 2 so that the sulfur content (sulfur atom conversion) was 10 ppm by mass to prepare a raw material oil A.
- This feedstock A was subjected to a hydrogenation treatment using the catalyst A shown in Table 1 under the condition a shown in Table 3.
- the hydrotreated oil was isomerized using the catalyst B shown in Table 1 under the condition b shown in Table 3.
- the fraction at 140 to 280 ° C. obtained from the isomerized oil after the isomerization was used as the base material 1.
- Table 4 shows the properties of the substrate 1.
- Aviation fuel oil composition 1 was prepared by mixing 30% by volume of catalytic cracking kerosene obtained from a fluid catalytic cracking apparatus having the properties shown in Table 2 with this base material 1.
- Example 2 Dimethyl sulfide was added to vegetable oil 2 having the properties shown in Table 2 so that the sulfur content (sulfur atom conversion) was 10 ppm by mass to prepare a raw material oil B.
- This feedstock B was subjected to hydrogenation treatment using the catalyst A shown in Table 1 under the condition c shown in Table 3.
- the 140-280 ° C. fraction obtained from the hydrotreated oil was subjected to isomerization treatment using the catalyst B shown in Table 1 under the condition b shown in Table 3.
- the isomerized oil after isomerization was cut by distillation into a fraction at 140 to 280 ° C. to obtain a substrate 2.
- Table 4 shows the properties of the substrate 2.
- Aviation fuel oil composition 2 was prepared by mixing 30% by volume of hydrocracked kerosene obtained from the heavy oil hydrocracking apparatus having the properties shown in Table 2 with this base material 2.
- Example 3 30% by volume of petroleum-based aviation fuel base material obtained by refining crude oil having the properties shown in Table 2 to aviation fuel oil composition 2 described in Example 2 was prepared to prepare aviation fuel oil composition 3 did.
- Table 4 also shows the properties of fatty acid alkyl esters obtained by esterifying vegetable fats and oils 1 having the properties shown in Table 2.
- These fatty acid alkyl esters are methyl ester compounds obtained by reaction with methanol. Here, they are stirred at 70 ° C. for about 1 hour in the presence of an alkali catalyst (sodium methylate) to directly react with alkyl alcohol. A transesterification reaction was used to obtain an ester compound.
- Aviation fuel oil composition 4 was prepared by mixing 30% by volume of the catalytically cracked kerosene described in Example 1 with this fatty acid methyl ester compound.
- Comparative Example 2 70% by volume of the base material 1 shown in Example 1 and 30% by volume of a petroleum-based aviation fuel oil base material obtained by refining crude oil having the properties shown in Table 2 were used to prepare an aviation fuel oil composition 5. Prepared.
- Comparative Example 3 As the aviation fuel oil of Comparative Example 3, a conventional representative commercially available petroleum aviation fuel oil was prepared.
- Antioxidant (2,6-ditertiary-butyl-phenol) 20 ppm by mass (based on the total amount of fuel composition)
- Antistatic agent STADIS 450 2.0mg / L (based on the total amount of fuel composition)
- the general properties of raw oil, aviation fuel base and aviation fuel oil shown in Table 2, Table 4 and Table 5 are values measured by the following methods.
- the density at 15 ° C. means a value measured according to JIS K2249 “Crude oil and petroleum products—Density test method and density / mass / capacity conversion table”.
- the kinematic viscosity at 30 ° C. means a value measured by JIS K2283 “Crude oil and petroleum products—Kinematic viscosity test method and viscosity index calculation method”.
- Elemental analysis C (mass%) and H (mass%) mean values measured by the method defined in ASTM D 5291 “Standard Test Methods for Instrumental Determination of Carbon, Hydrogen, and Nitrogen in Petroleum Products and Lubricants”.
- the oxygen content means a value measured by a method such as UOP649-74 “Total Oxygen in Organic Materials by Pyrolysis-Gas Chromatographic Technique”.
- the sulfur content means a value measured according to JIS K2541 “Crude oil and petroleum product sulfur content test method”.
- the acid value means a value measured by the method of JIS K 2501 “Petroleum products and lubricating oils—neutralization number test method”.
- the composition ratio of fatty acid groups in fats and oils is a value determined according to the above-mentioned standard fat analysis method (established by the Japan Oil Chemists' Society) (1993) “2.4.21.3-77 Fatty acid composition (FID temperature rising gas chromatograph method)” Point to.
- Flash point means the value obtained in JIS K2265 “Crude oil and petroleum products-Flash point test method-Tag closed flash point test method”. Distillation properties are measured in accordance with JIS K2254 “Petroleum product-Distillation test method”. Mean value.
- the aromatic content means a value measured by JIS K2536 “Test method for fuel oil hydrocarbon components (fluorescence indicator adsorption method)”.
- the total acid value means a value measured according to JIS K2276 “Petroleum products—Aeronautical fuel oil test method—Total acid value test method”.
- the precipitation point means a value measured according to JIS K2276 “Petroleum products—Aeronautical fuel oil test method—Precipitation point test method”.
- the smoke point means a value measured by JIS K2537 “Fuel oil smoke point test method”.
- the thermal stability means a value measured according to JIS K2276 “Petroleum products—Aeronautical fuel oil test method—Thermal stability test method A method, B method”.
- the true calorific value means a value measured by JIS K2279 “Crude oil and fuel oil calorific value test method”. Fuel consumption refers to a calorific value per unit volume, and means a value calculated by multiplying the true calorific value by the density.
- the life cycle characteristics (life cycle CO 2 calculation) described in this example were calculated by the following method.
- the life cycle CO 2 was calculated by dividing it into CO 2 generated as a result of aircraft flight (fuel combustion) using aviation fuel oil and CO 2 generated from raw material mining to fuel refueling in fuel production.
- the CO 2 generated by combustion (hereinafter referred to as “Tank to Wheel CO 2 ”) uses the value defined by the Ministry of the Environment (jet fuel: 2.5 kg-CO 2 / L), and emissions per unit calorific value Used in conversion.
- CO 2 generated from mining to refueling fuel tanks hereinafter referred to as “Wellto Tank CO 2 ”) is a series of operations from mining, transportation, processing, delivery, and refueling of raw materials and crude oil sources.
- the aviation fuel oil containing the aviation fuel base material obtained by hydrotreating the raw material derived from animal and plant fats and oils is inferior to typical petroleum aviation fuel oils including fuel efficiency. While it has general properties, it is a new aviation fuel oil that is an alternative to petroleum that has excellent life cycle characteristics and contributes to the prevention of global warming.
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Abstract
Description
異性化処理触媒の担体として用いられる多孔性の無機酸化物としては、アルミナ、チタニア、ジルコニア、ボリア、シリカ、あるいはゼオライトが挙げられ、本発明ではこのうちチタニア、ジルコニア、ボリア、シリカおよびゼオライトのうち少なくとも1種類とアルミナによって構成されているものが好ましい。その製造法は特に限定されないが、各元素に対応した各種ゾル、塩化合物などの状態の原料を用いて任意の調製法を採用することができる。さらには一旦シリカアルミナ、シリカジルコニア、アルミナチタニア、シリカチタニア、アルミナボリアなどの複合水酸化物あるいは複合酸化物を調製した後に、アルミナゲルやその他水酸化物の状態あるいは適当な溶液の状態で調製工程の任意の工程で添加して調製してもよい。アルミナと他の酸化物との比率は担体に対して任意の割合を取り得るが、好ましくはアルミナが90質量%以下、さらに好ましくは60質量%以下、より好ましくは40質量%以下であり、好ましくは10質量%以上、より好ましくは20質量%以上である。
なお、ここでいう実在ガム分とは、JIS K2261「ガソリン及び航空燃料油実在ガム試験方法」で測定される値を意味する。
<触媒A>
濃度5質量%のアルミン酸ナトリウム水溶液3000gに水ガラス3号18.0gを加え、65℃に保温した容器に入れた。他方、65℃に保温した別の容器において濃度2.5質量%の硫酸アルミニウム水溶液3000gにリン酸(濃度85%)6.0gを加えた溶液を調製し、これに前述のアルミン酸ナトリウムを含む水溶液を滴下した。混合溶液のpHが7.0になる時点を終点とし、得られたスラリー状の生成物をフィルターに通して濾取し、ケーキ状のスラリーを得た。
このケーキ状のスラリーを還流冷却器を取り付けた容器に移し、蒸留水150mlと27%アンモニア水溶液10gを加え、75℃で20時間加熱攪拌した。該スラリーを混練装置に入れ、80℃以上に加熱し水分を除去しながら混練し、粘土状の混練物を得た。得られた混練物を押出し成形機によって直径1.5mmシリンダーの形状に押し出し、110℃で1時間乾燥した後550℃で焼成し、成形担体を得た。
得られた成形担体50gをナス型フラスコに入れ、ロータリーエバポレーターで脱気しながら三酸化モリブデン17.3g、硝酸ニッケル(II)6水和物13.2g、リン酸(濃度85%)3.9g及びリンゴ酸4.0gを含む含浸溶液をフラスコ内に注入した。含浸した試料は120℃で1時間乾燥した後、550℃で焼成し、触媒Aを得た。触媒Aの物性を表1に示す。
<触媒B>
シリカ-アルミナ比(質量比)が70:30であるシリカアルミナ担体50gをナス型フラスコに入れ、ロータリーエバポレーターで脱気しながらテトラアンミン白金(II)クロライド水溶液をフラスコ内に注入した。含浸した試料は110℃で乾燥した後、350℃で焼成し、触媒Bを得た。触媒Bにおける白金の担持量は、触媒全量を基準として0.5質量%であった。触媒Bの物性を表1に示す。
表2に示す性状を有する植物油脂1に、硫黄分含有量(硫黄原子換算)が10質量ppmとなるようにジメチルサルファイドを添加して原料油Aを調製した。この原料油Aを表1に示す触媒Aを用いて表3に示す条件aで水素化処理を行った。水素化処理した油を表1に示す触媒Bを用いて表3に示す条件bで異性化処理を行った。異性化処理後の異性化処理油から得られる140~280℃の留分を基材1とした。基材1の性状を表4に示す。この基材1に、表2に示す性状を有する流動接触分解装置から得られる接触分解灯油を30容量%混合して航空燃料油組成物1を調製した。
表2に示す性状を有する植物油脂2に、硫黄分含有量(硫黄原子換算)が10質量ppmとなるようにジメチルサルファイドを添加して原料油Bを調製した。この原料油Bを表1に示す触媒Aを用いて表3に示す条件cで水素化処理を行った。水素化処理した油から得られる140~280℃の留分を、表1に示す触媒Bを用いて表3に示す条件bで異性化処理を行った。異性化処理後の異性化処理油を140~280℃の留分に蒸留カットし、基材2を得た。基材2の性状を表4に示す。この基材2に、表2に示す性状を有する重油水素化分解装置から得られる水素化分解灯油を30容量%混合して、航空燃料油組成物2を調製した。
実施例2に記載の航空燃料油組成物2に表2に示す性状を有する原油を精製して得られる石油系航空燃料油基材を30容量%混合して、航空燃料油組成物3を調製した。
表2に示す性状を有する植物油脂1をエステル化して得た脂肪酸アルキルエステルの性状を同じく表4に示す。これらの脂肪酸アルキルエステルはメタノールとの反応により得られたメチルエステル化合物であり、ここではアルカリ触媒(ナトリウムメチラート)の存在下で70℃、1時間程度の撹拌を行い、アルキルアルコールと直接反応させてエステル化合物を得るエステル交換反応を用いた。この脂肪酸メチルエステル化合物に実施例1に記載の接触分解灯油を30容量%混合して航空燃料油組成物4を調製した。
実施例1に示す基材1を70容量%と、表2に示す性状を有する原油を精製して得られる石油系航空燃料油基材を30容量%混合して、航空燃料油組成物5を調製した。
比較例3の航空燃料油として、従来の代表的な市販の石油系航空燃料油を用意した。
酸化防止剤(2,6-ditertiary-butyl-phenol) 20質量ppm(燃料組成物全量基準)
静電気防止剤(STADIS 450) 2.0mg/L(燃料組成物全量基準)
表2、表4および表5に示す原料油、航空燃料油基材および航空燃料油の一般性状は以下の方法により測定された値をいう。
15℃における密度(密度@15℃)は、JIS K2249「原油及び石油製品-密度試験方法並びに密度・質量・容量換算表」で測定される値を意味する。
30℃における動粘度は、JIS K2283「原油及び石油製品-動粘度試験方法及び粘度指数算出方法」で測定される値を意味する。
元素分析C(質量%)、H(質量%)はASTM D 5291 “Standard Test Methods for Instrumental Determination of Carbon,Hydrogen, and Nitrogen in Petroleum Products and Lubricants”で定められる方法で測定される値を意味する。
酸素分は、UOP649-74“TotalOxygen in Organic Materials by Pyrolysis-Gas Chromatographic Technique”等の方法で測定される値を意味する。
硫黄分は、JIS K2541「原油及び石油製品硫黄分試験方法」で測定される値を意味する。
酸価は、JIS K 2501「石油製品及び潤滑油-中和価試験方法」の方法で測定される値を意味する。
油脂中の脂肪酸基の構成比率は、前述の基準油脂分析試験法(日本油化学会制定)(1993)「2.4.21.3-77脂肪酸組成(FID昇温ガスロマトグラフ法)」に準じて求められる値を指す。
引火点は、JIS K2265「原油及び石油製品‐引火点試験方法‐タグ密閉式引火点試験方法」で求めた値を意味する
蒸留性状は、JIS K2254「石油製品-蒸留試験方法」で測定される値を意味する。
芳香族分は、JIS K2536「燃料油炭化水素成分試験方法(けい光指示薬吸着法)」で測定される値を意味する。
全酸価は、JIS K2276「石油製品-航空燃料油試験方法-全酸価試験方法」で測定される値を意味する。
析出点は、JIS K2276「石油製品-航空燃料油試験方法-析出点試験方法」により測定された値を意味する。
煙点は、JIS K2537「燃料油煙点試験方法」で測定される値を意味する。
熱安定度は、JIS K2276「石油製品-航空燃料油試験方法-熱安定度試験方法A法、B法」により測定された値を意味する。
真発熱量は、JIS K2279「原油及び燃料油発熱量試験方法」で測定される値を意味する。
燃費は、単位容積あたりの発熱量を指し、真発熱量に密度を乗じて算出される値を意味する。
本実施例で記載するライフサイクル特性(ライフサイクルCO2算出)は以下の手法によって計算した。
ライフサイクルCO2は、航空燃料油使用による航空機の飛行(燃料の燃焼)に伴い発生したCO2と、燃料製造における原料採掘から燃料給油までに発生したCO2と分けて算出した。
燃焼に伴い発生するCO2(以下、「Tank to Wheel CO2」という)は、環境省の定義値(ジェット燃料:2.5kg‐CO2/L)を使用し、単位発熱量当たりの排出量に換算して使用した。また、採掘から燃料タンクへの燃料給油までに発生したCO2(以下、「WelltoTank CO2」という。)は、原料及び原油ソースの採掘、輸送、加工、配送、車両への給油までの一連の流れにおけるCO2排出量の総和として算出した。なお、「WelltoTank CO2」の算出にあたっては、下記(1B)~(5B)に示す二酸化炭素の排出量を加味して演算を行った。かかる演算に必要となるデータとしては、本発明者らが有する製油所運転実績データを用いた。
(2B)水素を使用する処理においては、水素製造装置における改質反応に伴う二酸化炭素の排出量。
(3B)接触分解装置等の連続触媒再生を伴う装置を経由する場合は、触媒再生に伴う二酸化炭素の排出量。
(4B)航空燃料組成物を、横浜で製造又は陸揚げし、横浜から仙台まで配送し、仙台で燃焼機器に給油したときの二酸化炭素の排出量。
(5B)動植物油脂および動植物油脂由来の成分は原産地をマレーシアおよびその周辺地域とし、製造を横浜で行うとした際の二酸化炭素の排出量。
なお、動植物油脂および動植物油脂由来の成分を使用した場合、いわゆる京都議定書においてはこれらの燃料に起因する二酸化炭素は排出量として計上されないルールが適用される。本計算においては、燃焼時に発生する「Tank to Wheel CO2」に対してこれを適用させた。
Claims (7)
- 含硫黄炭化水素化合物及び動植物油脂に由来する含酸素炭化水素化合物を含有する第1の原料油又は該第1の原料油と原油を精製して得られる石油系基材との混合油である第2の原料油を水素化処理する工程を経て得られる、沸点範囲140~280℃の留分である第1の基材と、
重質油分解装置から得られる、沸点範囲140~280℃の留分である第2の基材と、
を含有することを特徴とする航空燃料油組成物。 - 前記第2の基材の15℃における密度が800kg/m3以上840kg/m3以下であることを特徴とする、請求項1に記載の航空燃料油組成物。
- 前記第1の基材が、水素の存在下、アルミニウム、ケイ素、ジルコニウム、ホウ素、チタン及びマグネシウムから選ばれる2種以上の元素を含んで構成される多孔性無機酸化物からなる担体に周期表第6A族及び第8族の元素から選ばれる1種以上の金属を担持してなる触媒を用い、水素圧力2~13MPa、液空間速度0.1~3.0h-1、水素/油比150~1500NL/L、反応温度150~480℃の条件下で前記第1又は第2の原料油を水素化処理する工程を経て得られるものであることを特徴とする、請求項1又は2に記載の航空燃料油組成物。
- 前記第1の基材が、前記第1又は第2の原料油を水素化処理する工程により得られる水素化処理油を、水素の存在下、アルミニウム、ケイ素、ジルコニウム、ホウ素、チタン、マグネシウム及びゼオライトから選ばれる物質より構成される多孔性無機酸化物からなる担体に周期表第8族の元素から選ばれる金属を担持してなる触媒を用いて、水素圧力2~13MPa、液空間速度0.1~3.0h-1、水素/油比250~1500NL/L、反応温度150~380℃の条件下でさらに異性化処理する工程を経て得られるものであることを特徴とする、請求項1~3のいずれか一項に記載の航空燃料油組成物。
- 原油を精製して得られる航空燃料油基材、合成系航空燃料油基材又はそれらの混合物である第3の基材を更に含有することを特徴とする、請求項1~4のいずれか一項に記載の航空燃料油組成物。
- 酸化防止剤、静電気防止剤、金属不活性化剤および氷結防止剤から選ばれる1種以上の添加剤を更に含有することを特徴とする、請求項1~5のいずれか一項に記載の航空燃料油組成物。
- JIS K2209「航空タービン燃料油」の規格値を満足することを特徴とする、請求項1~6のいずれか一項に記載の航空燃料油組成物。
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BR112012008143A BR112012008143A2 (pt) | 2009-08-31 | 2010-08-30 | composição de óleo combustível para aviação |
CN201080038681.0A CN102482599B (zh) | 2009-08-31 | 2010-08-30 | 航空燃料油组合物 |
SG2012011375A SG178490A1 (en) | 2009-08-31 | 2010-08-30 | Aviation fuel oil composition |
AU2010287445A AU2010287445B2 (en) | 2009-08-31 | 2010-08-30 | Aviation fuel oil composition |
US13/391,891 US20120198757A1 (en) | 2009-08-31 | 2010-08-30 | Aviation fuel oil composition |
EP10812043.7A EP2474598A4 (en) | 2009-08-31 | 2010-08-30 | FUEL COMPOSITION FOR AVIATION |
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EP2699533A4 (en) * | 2011-04-22 | 2015-03-04 | Univ North Dakota | PREPARATION OF AROMATES FROM NON-CATALYTICALLY CRACKED OILS ON FATTY ACID BASIS |
RU2495083C1 (ru) * | 2012-08-22 | 2013-10-10 | Открытое акционерное общество "Всероссийский научно-исследовательский институт по переработки нефти" (ОАО "ВНИИ НП") | Способ получения углеводородного топлива для ракетной техники |
WO2016064695A1 (en) * | 2014-10-21 | 2016-04-28 | Shell Oil Company | Catalyst and process for deoxygenation and conversion of bio-derived feedstocks |
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KR101750230B1 (ko) | 2016-04-08 | 2017-06-23 | 한국에너지기술연구원 | 촉매를 이용하여 비식용 유지로부터 고품질의 탄화수소 제조 방법 |
US20180184601A1 (en) * | 2017-01-03 | 2018-07-05 | Earl Brian Graffius | Self-Watering Insert For A Plant Container |
CN108456562B (zh) * | 2018-04-21 | 2019-05-03 | 东营华亚国联航空燃料有限公司 | 航空活塞式发动机燃料及其制备方法 |
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