JP5072004B2 - Method for producing unleaded gasoline composition - Google Patents

Description

The present invention relates to a method for producing an unleaded gasoline composition as a fuel for automobiles, and in particular, from the viewpoint of diversifying supply sources, contains an FT synthetic base material and is excellent in exhaust gas purification performance, fuel consumption performance, and driving performance. Relates to the manufacturing method .

Conventionally, gasoline is produced by blending one or more kinds of gasoline fraction base materials obtained by treating crude oil with various refining apparatuses such as a catalytic reforming apparatus and a catalytic cracking apparatus.
In recent years, gasoline automobiles have been required to reduce both harmful substances in exhaust gases for improving the air environment and to reduce CO ₂ emissions of greenhouse gases from the viewpoint of controlling global warming. As well as improving vehicle and engine technology including exhaust aftertreatment devices, it is also important to optimize gasoline quality. Gasoline needs quality that draws out the excellent exhaust gas purification performance, fuel efficiency performance, and driving performance of gasoline automobiles.

Demand for crude oil, which is the raw material for gasoline, has continued to increase against the background of the increase in the number of cars owned, and considering that crude oil is a finite resource, diversification of gasoline supply sources, that is, There is a demand to produce gasoline from resources other than crude oil and to improve the yield of gasoline that can be produced from crude oil.
Moreover, the quality of gasoline obtained when diversifying these supply sources needs to be excellent in exhaust gas purification performance, fuel efficiency performance, and drivability.

  As a result of diligent research to solve the above-mentioned problems, the present inventors have mixed FT synthesis base materials capable of using a wide range of carbon-containing materials as raw materials, and specified the gasoline composition obtained to have specific properties. As a result, it has been found that the gasoline supply source can be diversified, and at the same time, the exhaust gas purification performance, the fuel efficiency performance, and the driving performance of the gasoline automobile can be derived, and the present invention has been completed.

That is, this invention includes the process of mixing the FT synthetic base material which is all or a part of the fraction whose distillation temperature range is 25 degreeC-220 degreeC, The research method of the composition obtained Octane number is 96.0 or more, motor method octane number is 84.0 or more, sulfur content is 10 mass ppm or less, 10 vol % distillation temperature is 35 ° C or more and 70 ° C or less, 30 vol% distillation temperature is 55 ° C or more 77 % or less, 50% by volume distillation temperature is 75 ° C or more and 110 ° C or less, 70% by volume distillation temperature is 95 ° C or more and 135 ° C or less, 90% by volume distillation temperature is 115 ° C or more and 180 ° C or less, and distillation end point is 220. ° C. or less, Reid vapor pressure less 93kPa than 44 kPa, a density (15 ° C.) is 0.690 g / cm ³ or more 0.783g / cm ³ or less, oxidation stability is 240 minutes or more, a copper plate corrosion (50 ° C., 3 hours) 1 or less, washed existent gum 5 mg / 100 ml or less, unwashed actual gum 30 mg / 100 ml or less, a process for producing benzene content is free of lead gasoline composition Ru der than 1% by volume.

  According to the present invention, gasoline excellent in exhaust gas purification performance, fuel consumption performance, and drivability can be obtained using an FT synthetic base material.

Hereinafter, the present invention will be described in detail.
The gasoline obtained by the production method of the present invention (hereinafter simply referred to as “the gasoline of the present invention”) needs to contain an FT synthesis base material.
Here, the FT synthesis base material is a naphtha, kerosene obtained by applying a Fischer-Tropsch (FT) reaction to a mixed gas containing hydrogen and carbon monoxide as main components (sometimes referred to as synthesis gas), A liquid fraction corresponding to light oil, and a hydrocarbon mixture obtained by hydrorefining and hydrocracking them, and a liquid fraction and FT wax are produced by FT reaction, which are hydrorefined and hydrocracked. The base material which consists of a hydrocarbon mixture obtained by this is shown.

The mixed gas used as the raw material of the FT synthesis base material is obtained by oxidizing a carbon-containing substance using oxygen and / or water and / or carbon dioxide as an oxidizing agent, and further using a shift reaction using water as necessary. It is obtained by adjusting to a predetermined hydrogen and carbon monoxide concentration.
Substances containing carbon include natural gas, petroleum liquefied gas, methane gas, etc., gas components consisting of hydrocarbons that are gaseous at room temperature, petroleum asphalt, biomass, coal, waste such as building materials and garbage, sludge, In addition, mixed gas obtained by exposing heavy crude oil, unconventional petroleum resources, etc. that are difficult to process by ordinary methods to high temperatures is common, but mixed gas mainly composed of hydrogen and carbon monoxide As long as is obtained, the present invention does not limit the raw materials.

  A Fischer-Tropsch reaction requires a metal catalyst. Preferably, the method uses a group 8 metal of the periodic table, for example, cobalt, ruthenium, rhodium, palladium, nickel, iron, etc., more preferably a group 8 group 4 metal as the active catalyst component. Moreover, the metal group which mixed these metals in an appropriate amount can also be used. These active metals are generally used in the form of a catalyst obtained by being supported on a support such as silica, alumina, titania or silica alumina. Further, by using these catalysts in combination with a second metal in addition to the above active metal, the catalyst performance can be improved. Examples of the second metal include zirconium, hafnium, titanium and the like in addition to alkali metals and alkaline earth metals such as sodium, lithium and magnesium. It is used appropriately according to the purpose, such as an increase in growth probability (α).

  The Fischer-Tropsch reaction is a synthesis method that generates a liquid fraction and FT wax using a mixed gas as a raw material. In order to efficiently perform this synthesis method, it is generally preferable to control the ratio of hydrogen to carbon monoxide in the mixed gas. The molar mixing ratio of hydrogen to carbon monoxide (hydrogen / carbon monoxide) is preferably 1.2 or more, more preferably 1.5 or more, and even more preferably 1.8 or more. The ratio is preferably 3 or less, more preferably 2.6 or less, and even more preferably 2.2 or less.

  When performing the Fischer-Tropsch reaction using the catalyst, the reaction temperature is preferably 180 ° C. or higher and 320 ° C. or lower, and more preferably 200 ° C. or higher and 300 ° C. or lower. When the reaction temperature is less than 180 ° C., carbon monoxide hardly reacts and the hydrocarbon yield tends to be low. On the other hand, when the reaction temperature exceeds 320 ° C., the amount of gas such as methane increases, and the production efficiency of the liquid fraction and FT wax decreases.

No particular restriction on the gas hourly space velocity relative to the catalyst, but preferably 500h ^-1 or more 4000h ^-1 or less, 1000h ^-1 or more 3000h ^-1 or less is more preferable. If the gas space velocity is less than 500 h ⁻¹ , the productivity of the liquid fuel tends to decrease. If the gas space velocity exceeds 4000 h ⁻¹ , the reaction temperature must be increased, and gas generation increases, resulting in a yield of the target product. It will decline.

  The reaction pressure (partial pressure of synthesis gas composed of carbon monoxide and hydrogen) is not particularly limited, but is preferably 0.5 MPa or more and 7 MPa or less, and more preferably 2 MPa or more and 4 MPa or less. If the reaction pressure is less than 0.5 MPa, the yield of the liquid fuel tends to decrease, and if it exceeds 7 MPa, the amount of capital investment tends to increase, which is uneconomical.

  The FT synthesis substrate is prepared by hydrorefining or hydrocracking the liquid fraction and FT wax produced by the above FT reaction by any method as necessary to adjust the distillation properties, composition, etc. according to the purpose. It is also possible. Hydrorefining and hydrocracking may be selected in accordance with the purpose, and selection of only one or a combination of both methods is not limited in any way as long as the fuel composition of the present invention can be produced. .

The catalyst used for hydrorefining is generally a catalyst in which a hydrogenation active metal is supported on a porous carrier, but the present invention does not limit the form of the catalyst as long as the same effect can be obtained.
An inorganic oxide is preferably used as the porous carrier. Specific examples include alumina, titania, zirconia, boria, silica, zeolite, and the like.
Zeolite is a crystalline aluminosilicate, and includes faujasite, pentasil, mordenite, etc., preferably faujasite, beta, mordenite, particularly preferably Y type and beta type. Of these, the Y type is preferably ultra-stabilized.

As the active metal, the following two types (active metal A type and active metal B type) are preferably used.
The active metal A type is at least one metal selected from Group 8 metals of the Periodic Table. Preferably, it is at least one selected from Ru, Rh, Ir, Pd and Pt, and more preferably Pd or / and Pt. The active metal may be a combination of these metals. For example, Pt—Pd, Pt—Rh, Pt—Ru, Ir—Pd, Ir—Rh, Ir—Ru, Pt—Pd—Rh, Pt—Rh— Ru, Ir-Pd-Rh, Ir-Rh-Ru, and the like. When using a noble metal catalyst composed of these metals, it can be used after pre-reduction treatment in a hydrogen stream. In general, when a gas containing hydrogen is circulated and heat of 200 ° C. or higher is applied according to a predetermined procedure, the active metal on the catalyst is reduced, and hydrogenation activity is exhibited.
Further, as the active metal B type, it contains at least one metal selected from Group 6A and Group 8 metals of the periodic table, and preferably contains two or more metals selected from Groups 6A and 8 What you are doing can also be used. For example, Co-Mo, Ni-Mo, Ni-Co-Mo, and Ni-W can be mentioned. When using a metal sulfide catalyst made of these metals, it is necessary to include a preliminary sulfidation step.

  As the metal source, a general inorganic salt or a complex salt compound can be used, and as a supporting method, any method of a supporting method used in an ordinary hydrogenation catalyst such as an impregnation method or an ion exchange method can be used. When a plurality of metals are supported, they may be supported simultaneously using a mixed solution, or may be sequentially supported using a single solution. The metal solution may be an aqueous solution or an organic solvent.

The reaction temperature when hydrotreating using a catalyst composed of an active metal A type is preferably 180 ° C. or higher and 400 ° C. or lower, more preferably 200 ° C. or higher and 370 ° C. or lower, and 250 ° C. or higher and 350 ° C. or lower. More preferably, the temperature is 280 ° C. or lower and even more preferably 280 ° C. or higher and 350 ° C. or lower. If the reaction temperature in hydrorefining exceeds 370 ° C., side reactions that decompose into naphtha fractions increase, and the yield of middle fractions is extremely undesirably reduced. On the other hand, when the reaction temperature is lower than 270 ° C., the alcohol component cannot be completely removed and is not preferable.
The reaction temperature when hydrotreating using a catalyst comprising an active metal B type is preferably 170 ° C. or higher and 320 ° C. or lower, more preferably 175 ° C. or higher and 300 ° C. or lower, and 180 ° C. or higher and 280 ° C. More preferably, it is not higher than ° C. If the reaction temperature in the hydrorefining exceeds 320 ° C., side reactions that decompose into naphtha fractions increase, and the yield of middle fractions is extremely undesirably reduced. On the other hand, when the reaction temperature is lower than 170 ° C., the alcohol component cannot be completely removed and is not preferable.

The hydrogen pressure when hydrotreating using a catalyst composed of an active metal A type is preferably 0.5 MPa or more and 12 MPa or less, and more preferably 1.0 MPa or more and 5.0 MPa or less. The higher the hydrogen pressure, the more hydrogenation reaction is promoted, but generally there is an optimal point economically.
The hydrogen pressure when hydrotreating using a catalyst composed of an active metal B type is preferably 2 MPa or more and 10 MPa or less, more preferably 2.5 MPa or more and 8 MPa or less, and 3 MPa or more and 7 MPa or less. More preferably. The higher the hydrogen pressure, the more hydrogenation reaction is promoted, but generally there is an optimal point economically.

The liquid hourly space velocity which hydrorefining is carried out using a catalyst composed of the active metal A type (LHSV) is preferably at 0.1 h ^-1 or more 10.0H ^-1 or less, 0.3h ^-1 or 3 More preferably, it is 5 h ⁻¹ or less. The lower the LHSV, the more advantageous for the reaction. However, if the LHSV is too low, an extremely large reaction tower volume is required, resulting in excessive capital investment, which is not economical.
The liquid hourly space velocity which hydrorefining is carried out using a catalyst composed of the active metal B type (LHSV) is preferably at 0.1 h ^-1 or more ^{2h -1} or less, 0.2 h ^-1 or more 1.5h more preferably ^{1 or} less, and more preferably 0.3h ^-1 or 1.2 h ^-1. The lower the LHSV, the more advantageous for the reaction. However, if the LHSV is too low, an extremely large reaction tower volume is required, resulting in excessive capital investment, which is not economical.

The hydrogen / oil ratio is preferably 50 NL / L or more and 1000 NL / L or less, more preferably 70 NL / L or more and 800 NL / L or less when hydrotreating using a catalyst composed of an active metal A type. preferable. The higher the hydrogen / oil ratio, the more hydrogenation reaction is promoted, but generally there is an optimal point economically.
The hydrogen / oil ratio when hydrotreating using a catalyst composed of an active metal B type is preferably 100 NL / L or more and 800 NL / L or less, more preferably 120 NL / L or more and 600 NL / L or less. Preferably, it is 150 NL / L or more and 500 NL / L or less. The higher the hydrogen / oil ratio, the more hydrogenation reaction is promoted, but generally there is an optimal point economically.

The catalyst used for hydrocracking is generally one in which a hydrogenation active metal is supported on a carrier having a solid acid property, but the present invention does not limit the form of the catalyst as long as the same effect can be obtained. Absent.
Supports having a solid acid property include amorphous and crystalline zeolites. Specific examples include amorphous silica-alumina, silica-magnesia, silica-zirconia, silica-titania and zeolite faujasite type, beta type, MFI type, and mordenite type. Preferred are faujasite type, beta type, MFI type, and mordenite type zeolite, and more preferred are Y type and beta type. The Y type is preferably ultra-stabilized.

As the active metal, the following two types (active metal A type and active metal B type) are preferably used.
The active metal A type is at least one metal selected from Group 6A and Group 8 metals in the periodic table. Preferably, it is at least one metal selected from Ni, Co, Mo, Pt, Pd and W. When using a noble metal catalyst composed of these metals, it can be used after pre-reduction treatment in a hydrogen stream. In general, when a gas containing hydrogen is circulated and heat of 200 ° C. or higher is applied according to a predetermined procedure, the active metal on the catalyst is reduced, and hydrogenation activity is exhibited.
The active metal B type may be a combination of these metals, and examples thereof include Pt—Pd, Co—Mo, Ni—Mo, Ni—W, and Ni—Co—Mo. Moreover, when using the catalyst which consists of these metals, it is preferable to use after pre-sulfiding.

  As the metal source, a general inorganic salt or a complex salt compound can be used, and as a supporting method, any method of a supporting method used in an ordinary hydrogenation catalyst such as an impregnation method or an ion exchange method can be used. When a plurality of metals are supported, they may be supported simultaneously using a mixed solution, or may be sequentially supported using a single solution. The metal solution may be an aqueous solution or an organic solvent.

  The reaction temperature when performing hydrocracking using a catalyst comprising an active metal A type and an active metal B type is preferably 200 ° C. or higher and 450 ° C. or lower, more preferably 250 ° C. or higher and 430 ° C. or lower. More preferably, the temperature is 300 ° C. or more and 400 ° C. or less. If the reaction temperature in the hydrocracking exceeds 450 ° C., side reactions that decompose into a naphtha fraction increase and the yield of the middle fraction is extremely reduced, which is not preferable. On the other hand, when the temperature is lower than 200 ° C., the activity of the catalyst is remarkably lowered, which is not preferable.

  The hydrogen pressure when hydrocracking using a catalyst comprising an active metal A type and an active metal B type is preferably 1 MPa or more and 20 MPa or less, more preferably 4 MPa or more and 16 MPa or less, and 6 MPa or more and 13 MPa. More preferably, it is as follows. The higher the hydrogen pressure is, the more hydrogenation reaction is promoted. However, the decomposition reaction rather slows down and the progress of the reaction needs to be adjusted by increasing the reaction temperature, leading to a decrease in catalyst life. For this reason, there is generally an economical optimum for the reaction temperature.

The liquid hourly space velocity which hydrocracking is carried out using a catalyst composed of the active metal A type (LHSV) is preferably at 0.1 h ^-1 or more ^{10h -1} or less, 0.3h ^-1 over 3.5h ^-More preferably, it is ¹ or less. The lower the LHSV, the more advantageous for the reaction. However, if the LHSV is too low, an extremely large reaction tower volume is required, resulting in excessive capital investment, which is not economical.
The liquid hourly space velocity which hydrocracking is carried out using a catalyst composed of the active metal B type (LHSV) is preferably at 0.1 h ^-1 or more ^{2h -1} or less, 0.2 h ^-1 or 1. It is more preferably 7h- ¹ or less, and further preferably 0.3h- ¹ or more and 1.5h- ¹ or less. The lower the LHSV, the more advantageous for the reaction. However, if the LHSV is too low, an extremely large reaction tower volume is required, resulting in excessive capital investment, which is not economical.

The hydrogen / oil ratio is preferably 50 NL / L or more and 1000 NL / L or less, more preferably 70 NL / L or more and 800 NL / L or less when hydrocracking using a catalyst composed of an active metal A type. Preferably, it is 400 NL / L or more and 1500 NL / L or less. The higher the hydrogen / oil ratio, the more hydrogenation reaction is promoted, but generally there is an optimal point economically.
The hydrogen / oil ratio is preferably 150 NL / L or more and 2000 NL / L or less, more preferably 300 NL / L or more and 1700 NL / L or less when hydrocracking using a catalyst composed of an active metal B type. Preferably, it is 400 NL / L or more and 1500 NL / L or less. The higher the hydrogen / oil ratio, the more hydrogenation reaction is promoted, but generally there is an optimal point economically.

The apparatus for hydrotreating may be of any configuration, the reaction towers may be used alone or in combination, hydrogen may be additionally injected between the reaction towers, gas-liquid separation operation, hydrogen sulfide removal equipment, hydrogen It may have a distillation column for fractionating the chemical product and obtaining the desired fraction.
The reaction format of the hydrotreating apparatus can take a fixed bed system. Hydrogen can take either a countercurrent or a cocurrent flow with respect to the feedstock, and may have a plurality of reaction towers and a combination of countercurrent and cocurrent flow. The general format is downflow, and there is a gas-liquid twin parallel flow format. Hydrogen gas may be injected into the middle stage of the reaction tower as a quench for the purpose of removing reaction heat or increasing the hydrogen partial pressure.

The FT synthesis base material contained in the gasoline of the present invention needs to be all or a part of a fraction having a distillation temperature range of 25 ° C to 220 ° C.
Examples of the fraction range include a light fraction of 25 ° C to 70 ° C, an intermediate fraction of 70 ° C to 160 ° C, and a heavy fraction of 160 ° C to 220 ° C. In addition, the remainder obtained by removing a part of the fraction range from the 25 ° C. to 220 ° C. fraction can be used.

  The normal paraffin content in the FT synthetic base contained in the gasoline of the present invention is preferably 75% by volume or less, more preferably 60% by volume or less, and further preferably 50% by volume or less. If the amount of normal paraffin exceeds 75% by volume, the octane number may decrease, causing knocking resistance, acceleration, and drivability to decrease. May not be possible.

  The isoparaffin content in the FT synthesis base material contained in the gasoline of the present invention is preferably 20% by volume or more, more preferably 40% by volume or more, further preferably 50% by volume or more, 60 Most preferably, it is at least volume%. If the amount of normal paraffin is less than 20% by volume, the octane number may decrease, causing a decrease in knocking resistance, acceleration, and driving performance. There is a possibility that it cannot be achieved.

  As the FT synthesis base material contained in the gasoline of the present invention, those having an olefin content of 5% by volume or more can be preferably used. When the olefin is 5% by volume or more, there is a possibility that the knocking resistance, acceleration, and operability can be improved.

  In the gasoline of the present invention, the content of the FT synthetic base material consisting of all or part of the fraction having a distillation temperature range of 25 ° C. to 220 ° C. is 3% of the total amount of gasoline from the viewpoint of diversification of supply sources. It is preferably at least volume%, more preferably at least 5 volume%. On the other hand, from the viewpoint of fuel efficiency, the content of the base material is preferably 30% by volume or less, more preferably 25% by volume or less, and further preferably 20% by volume or less with respect to the total amount of gasoline. preferable.

The gasoline of the present invention is not particularly limited as long as it satisfies the properties defined in the present invention except for the FT synthetic base material, and it can be produced by any conventionally known method. More than one kind of gasoline base material can be blended.
Specifically, for example, a straight-run propane fraction centered on propane obtained from a crude oil distillation apparatus, a naphtha reformer, an alkylation apparatus, etc., a straight-run butane fraction centered on butane, and desulfurizing them. Straight-run desulfurized propane fraction obtained by treatment, straight-run desulfurized butane fraction, cracked propane fraction centered on propane / propylene obtained from catalytic cracker etc., cracked system centered on butane / butene Butane fraction, naphtha fraction obtained by atmospheric distillation of crude oil (hole range naphtha), naphtha light fraction, naphtha heavy fraction, desulfurization whole range naphtha, desulfurized whole range naphtha, light naphtha Desulfurized light naphtha, desulfurized heavy naphtha obtained by desulfurizing heavy naphtha, isomerized gasoline obtained by converting light naphtha into isoparaffin using an isomerizer, isobutane, etc. Alkylate obtained by addition (alkylation) of lower olefin to hydrogen, reformed gasoline obtained by catalytic reforming method, raffinate which is a residue extracted from aromatics from reformed gasoline, lightness of reformed gasoline Light reformed gasoline that is a fraction, medium reformed gasoline that is a medium fraction of reformed gasoline, medium heavy reformed gasoline that is a medium heavy fraction of reformed gasoline, and heavy fraction of reformed gasoline Heavy reformed gasoline, a mixture of two or more of each reformed gasoline, catalytic cracked gasoline obtained by catalytic cracking (hole range cracked gasoline), light cracked gasoline that is a light fraction of catalytic cracked gasoline, contact Heavy cracked gasoline, which is a heavy fraction of cracked gasoline, hydrocracked gasoline obtained by hydrocracking method, polymerized gasoline obtained by polymerization of olefin, propylene or Olefin fraction obtained by dimerization of butene, paraffin fraction obtained by hydrogenation of olefin fraction obtained by dimerization of propylene or butene, denormalized paraffin oil, aromatic hydrocarbon compound (toluene, carbon number 8 Aromatic (xylenes), aromatics having 9 carbon atoms, etc.).

The blending amounts of these base materials are arbitrary as long as the gasoline of the present invention is adjusted so as to have a necessary property range, but typical examples of the blending ranges of base materials are shown below.
(1) Reformed gasoline: 0 to 80% by volume
(2) Cracked gasoline: 0-60% by volume
(3) Alkylate: 0 to 40% by volume
(4) Isomerized gasoline: 0-30% by volume

Moreover, the gasoline of the present invention may contain an oxygen-containing compound.
Examples of the oxygen-containing compound include alcohols having 2 to 4 carbon atoms and ethers having 4 to 8 carbon atoms. Specific examples of oxygen-containing compounds include ethanol, methyl tert-butyl ether (MTBE), ethyl tert-butyl ether (ETBE), tert-amyl methyl ether (TAME), and tert-amyl ethyl ether. it can. Of these, ethanol, MTBE, and ETBE are preferable. From the viewpoint of suppressing carbon dioxide emission, ethanol derived from biomass and ETBE produced using biomass-derived ethanol as a raw material can be particularly preferably used. Methanol is not detected when tested in accordance with JIS K 2536 “Petroleum product-component test method” (0.5% by volume) because it is corrosive and may increase the concentration of aldehyde in the exhaust gas. It is preferable that
The oxygen-containing compound content in the gasoline of the present invention is preferably 3.8% by mass or less in terms of oxygen atom from the viewpoint of compatibility with automobile fuel system members and suppression of increase in NOx in exhaust gas. 3.5 mass% or less, more preferably 2.7 mass% or less, and most preferably 1.3 mass% or less.

The gasoline research octane number (RON) of the present invention is 96 in order to maximize the knocking resistance, acceleration and drivability when the gasoline of the present invention is mainly used in premium gasoline specification vehicles. 0.0 or more is necessary, preferably 98.0 or more, more preferably 99.5 or more, and even more preferably 100.0 or more.
Further, from the viewpoint of preventing deterioration of the anti-knocking performance at high speed, the gasoline motor octane number (MON) of the present invention needs to be 84.0 or more, preferably 86.0 or more, preferably 87.0. More preferably, it is more preferably 87.5 or more, still more preferably 88.0 or more, and most preferably 88.5 or more.
The research method octane number (RON) and the motor method octane number (MON) as used herein mean the research method octane number and the motor method octane number measured by JIS K 2280 “Testing method for octane number and cetane number”.

The sulfur content of the gasoline of the present invention needs to be 10 mass ppm or less, preferably 8 mass ppm or less, and more preferably 5 mass ppm or less. If the sulfur content exceeds 10 ppm by mass, the performance of the exhaust gas purification catalyst may be adversely affected, the concentration of NOx, CO, and HC in the exhaust gas may increase, and the amount of benzene emitted may increase. This is not preferable.
The sulfur content here means a value measured according to JIS K 2541 “Crude oil and petroleum products—Sulfur content test method”.

The gasoline of the present invention needs to be unleaded. The term “lead-free” as used herein means that an alkyl lead compound such as tetraethyl lead is not substantially added. Even when a very small amount of lead compound is contained, the content is JIS K 2255 “in gasoline. It means that it is not more than the application category lower limit value (0.001 g / l) of “lead content test method”.

The distillation initial boiling point (IBP) of the gasoline of the present invention is preferably 20 ° C. or higher, more preferably 23 ° C. or higher. When IBP is less than 20 ° C., hydrocarbons in the exhaust gas may increase. On the other hand, IBP is preferably 37 ° C. or lower, more preferably 35 ° C. or lower. When IBP exceeds 37 ° C., low temperature drivability may be reduced.
The 10 vol% distillation temperature (T10) of the gasoline of the present invention is preferably 35 ° C or higher, more preferably 40 ° C or higher. When T10 is less than 35 ° C., hydrocarbons in the exhaust gas may increase, and high temperature operability may decrease due to vapor lock. On the other hand, T10 needs to be 70 ° C. or lower, and preferably 60 ° C. or lower. When T10 exceeds 70 ° C, the low temperature startability may be reduced.
The 30 vol% distillation temperature (T30) of the gasoline of the present invention is preferably 55 ° C or higher, more preferably 60 ° C or higher. If T30 is less than 55 ° C., fuel consumption may be deteriorated. On the other hand, T30 is preferably 77 ° C or lower, more preferably 75 ° C or lower, and further preferably 70 ° C or lower. When T30 exceeds 77 ° C, the medium / low temperature drivability may be lowered.
The 50 volume% distillation temperature (T50) of the gasoline of the present invention needs to be 75 ° C. or higher, and preferably 80 ° C. or higher, from the viewpoint of preventing deterioration of fuel consumption. On the other hand, from the viewpoint of preventing deterioration in normal temperature drivability, T50 needs to be 110 ° C. or lower, preferably 105 ° C. or lower, and more preferably 100 ° C. or lower.
The 70 vol% distillation temperature (T70) of the gasoline of the present invention is preferably 95 ° C or higher. When T70 is less than 95 ° C., fuel consumption may be deteriorated. On the other hand, T70 is preferably 135 ° C. or lower, more preferably 130 ° C. or lower. When T70 exceeds 135 ° C., the medium / low temperature operability during cold operation may decrease, and there may be an increase in hydrocarbons in exhaust gas, an increase in intake valve deposits, and an increase in combustion chamber deposits. .
The 90 vol% distillation temperature (T90) of the gasoline of the present invention is preferably 115 ° C or higher, more preferably 120 ° C or higher. When T90 is less than 115 ° C., fuel consumption may be deteriorated. On the other hand, T90 is 180 from the viewpoint of preventing deterioration of low temperature and normal temperature drivability during cold operation, increase in dilution of engine oil with gasoline, increase in hydrocarbon exhaust gas, deterioration of engine oil and generation of sludge. It is necessary that the temperature is not higher than ℃, preferably 175 ° C. or lower, more preferably 170 ° C. or lower, and further preferably 165 ° C. or lower.
The distillation end point (EP) of the gasoline of the present invention is preferably 150 ° C. or higher. Further, the EP needs to be 220 ° C. or lower, preferably 215 ° C. or lower, more preferably 200 ° C. or lower, and further preferably 195 ° C. or lower. If EP exceeds 220 ° C., intake valve deposits and combustion chamber deposits may increase, and spark plug smoldering may occur.
Here, IBP, T10, T30, T50, T70, T90, and EP mean values (° C.) measured by JIS K 2254 “Petroleum products—distillation test method”.

  The lead vapor pressure (RVP) of the gasoline of the present invention needs to be 44 kPa or more and 93 kPa or less. The gasoline of the present invention is preferably adjusted according to the season and region where it is used. Specifically, for warm seasons and regions, 44 to 72 kPa is preferable, 44 to 65 kPa is more preferable, 50 to 65 kPa is further preferable, and 55 to 65 kPa is most preferable. On the other hand, for cold seasons and regions, 60 to 93 kPa is preferable, 65 to 93 kPa is more preferable, 70 to 93 kPa is further preferable, and 70 to 88 kPa is most preferable. If the RVP is high, there may be a problem in drivability due to vapor lock or the like, and if the RVP is low, the startability in the cold state may be deteriorated. The vapor pressure (RVP) here refers to a value (kPa) measured by JIS K 2258 “Crude oil and fuel oil vapor pressure test method (Lead method)”.

The density at 15 ° C. of the gasoline of the present invention needs to be 0.690 g / cm ³ or more, preferably 0.700 g / cm ³ or more, from the viewpoint of suppressing deterioration of fuel consumption. 710 g / cm ³ or more, more preferably, 0.720 g / cm ³ or more, and even more preferably 0.730 g / cm ³ or more. On the other hand, the density at 15 ° C. needs to be 0.783 g / cm ³ or less, preferably 0.770 g / cm ³ or less, from the viewpoint of preventing deterioration of acceleration and smoldering of the plug, preferably 0.760 g / cm ³ or less. / Cm ³ or less is more preferable.
Here, the density at 15 ° C. means a value (g / cm ³ ) measured according to JIS K 2249 “Density test method and density / mass / capacity conversion table for crude oil and petroleum products”.

The oxidation stability of the gasoline of the present invention needs to be 240 minutes or more from the viewpoint of suppressing the formation of gum during storage, preferably 480 minutes or more, more preferably 960 minutes or more, Even more preferably, it is 1440 minutes or longer.
The oxidation stability here means a value (minutes) measured by JIS K 2287 “Gasoline oxidation stability test method (induction period method)”.

The gasoline of the present invention must have a copper plate corrosion (50 ° C., 3 hours) of 1 or less, and is preferably 1a. If the copper plate corrosion exceeds 1, the fuel system conduit may corrode.
The copper plate corrosion here means a value measured according to JIS K 2513 “Petroleum products—copper plate corrosion test method” (test temperature 50 ° C., test time 3 hours).

The actual gum amount of the gasoline of the present invention needs to be 5 mg / 100 ml or less, preferably 3 mg / 100 ml or less, more preferably 1 mg / 100 ml or less. Moreover, the unwashed actual gum amount of the gasoline of the present invention needs to be 30 mg / 100 ml or less, and preferably 20 mg / 100 ml or less. When the unwashed actual gum amount and the washed actual gum amount exceed the above values, there is a concern that precipitates are generated in the fuel introduction system or the suction valve is stuck.
As used herein, the amount of washed actual gum and the amount of unwashed actual gum mean values (mg / 100 ml) measured according to JIS K 2261 “Petroleum products—automobile gasoline and aviation fuel oil—existing gum test method—injection evaporation method”. To do.

The benzene content in the gasoline of the present invention needs to be 1% by volume or less, preferably 0.5% by volume or less. If the benzene content exceeds 1% by volume, the concentration of benzene in the exhaust gas may increase.
The benzene content here means the benzene content (volume%) measured according to JIS K 2536 “Petroleum products—component test method—aromatic test method by gas chromatography”.

The amount of kerosene mixed in the gasoline of the present invention is preferably 4% by volume or less. If the amount of kerosene mixed exceeds 4% by volume, the startability of the engine may deteriorate.
Here, the amount of kerosene mixed is determined by the content of normal paraffin hydrocarbons having 13 and 14 carbon atoms on the basis of the total amount of gasoline, and the converted value of kerosene obtained according to the provisions of JIS K 2536 “Petroleum products-component test method” Is 4% by volume or less.

The aromatic content in the gasoline of the present invention is preferably 45% by volume or less, more preferably 42% by volume or less, and still more preferably 40% by volume or less. When the aromatic content is large, there is a possibility that intake valve deposits and combustion chamber deposits may increase, smoldering of spark plugs may occur, and the concentration of benzene in the exhaust gas may increase. On the other hand, the aromatic content is preferably 10% by volume or more, more preferably 15% by volume or more, still more preferably 20% by volume or more, still more preferably 25% by volume or more, and more preferably 30% by volume or more. Particularly preferred. If the aromatic content is low, the fuel consumption may deteriorate.
The aromatic content here means the aromatic content (volume%) in gasoline measured by JIS K 2536 “Petroleum products—component test method—fluorescent indicator adsorption method”.

The olefin content in the gasoline of the present invention is preferably 35% by volume or less, and more preferably 25% by volume or less. When the olefin content exceeds 35% by volume, there is a possibility that the oxidation stability of gasoline is deteriorated and the intake valve deposit is increased.
The olefin content here means the olefin content (volume%) in gasoline measured by JIS K 2536 “Petroleum products—component test method—fluorescent indicator adsorption method”.

  The sensitivity of the present invention (difference between RON and MON; RON-MON) is preferably 12.5 or less, more preferably 12.0 or less, and even more preferably 11.5 or less, Even more preferably, it is 11.0 or less. If the sensitivity is small, knock resistance at high speeds and high engine speeds may be deteriorated.

2 mass ppm or less is preferable and, as for content of manganese in the gasoline of this invention, 1 mass ppm or less is more preferable. The content of iron in the gasoline of the present invention is preferably 2 ppm by mass or less, and more preferably 1 ppm by mass or less. The content of sodium in the gasoline of the present invention is preferably 2 ppm by mass or less, and more preferably 1 ppm by mass or less. The potassium content in the gasoline of the present invention is preferably 2 ppm by mass or less, and more preferably 1 ppm by mass or less. The phosphorus content in the gasoline of the present invention is preferably 2 ppm by mass or less, more preferably 1 ppm by mass or less, and even more preferably 0.2 ppm by mass or less. If the contents of manganese, iron, sodium, potassium, and phosphorus exceed the above values, the efficiency of the exhaust gas purification system will increase due to an increase in the amount accumulated on the exhaust gas purification catalyst, deterioration of the catalyst carrier, deterioration of the air-fuel ratio sensor, etc. May decrease.
The manganese, iron, and sodium contents here are “combustion ashing-inductively coupled plasma emission method”, the potassium content is “combustion ashing-atomic absorption method”, and the phosphorus content is ASTM D3231 “Standard Test Method”. for Phosphorus in Gasoline ”.

Hereinafter, measurement methods of “combustion ashing-inductively coupled plasma emission method” and “combustion ashing-atomic absorption method” will be described in detail.
(1) Collect 20 g of a sample in a platinum dish.
(2) In order to suppress the volatilization of the component elements, 0.4 g of powdered sulfur is added, and the volatile matter is removed every 1 hour at 150 ° C. on a sand bath.
(3) Burn the residue.
(4) Ash in an electric furnace at 500 ° C. for 2 to 3 hours.
(5) Dissolve in 2 to 3 mL of concentrated sulfuric acid and make up to 20 mL.
(6) Manganese, iron, and sodium contents were measured using an inductively coupled plasma emission spectrometer (ICPS-8000, manufactured by Shimadzu Corporation), and phosphorus contents were measured using an atomic absorption photometer (made by Hitachi, Ltd., Z6100). analyse.

  The gasoline of the present invention preferably contains an antioxidant and a metal deactivator for storage stability. Specifically, examples of the antioxidant include phenylenediamines such as N, N′-diisopropyl-p-phenylenediamine and N, N′-diisobutyl-p-phenylenediamine, and 2,6-di-t-butyl. Known compounds can be used as alkylphenol-based antioxidants such as hindered phenols represented by -4-methylphenol, and N, N'-disalicylidene-1,2 is used as a metal deactivator. -Known compounds can be used as metal deactivators such as amine carbonyl condensation compounds such as diaminopropane.

  There are no particular restrictions on the amount of antioxidant or metal deactivator added, but the aforementioned oxidation stability is a preferred value, and the amount of unwashed real gum in the gasoline composition after addition including other additives is It is preferable to set the above-mentioned preferable value. Specifically, the antioxidant is preferably 5 to 100 mg / l, more preferably 10 to 50 mg / l. Moreover, 0.5-10 mg / l is preferable and, as for a metal deactivator, 1-5 mg / l is more preferable.

The gasoline of the present invention preferably contains a cleaning dispersant in order to prevent deposits such as intake valves from being deposited. As the cleaning dispersant, compounds known as gasoline cleaning dispersants such as succinimide, polyalkylamine, and polyetheramine can be used. Among these, those having no residue when pyrolysis is performed at 300 ° C. in air are desirable. More preferably, polyisobutenylamine and / or polyetheramine is used.
The content of the cleaning dispersant is preferably 25 to 1000 mg per liter of gasoline of the present invention, more preferably 50 to 500 mg from the viewpoint of preventing intake valve deposits and further reducing combustion chamber deposits, ˜300 mg is most preferred. In the cleaning dispersant, an active ingredient that contributes to cleanliness may be diluted with an appropriate solvent. In such a case, the above-mentioned addition amount means an addition amount as an active ingredient.

  The gasoline of the present invention can contain a friction modifier in order to improve lubricity. Examples of the main friction modifier include, for example, alcohol; alcohol compound having 1 to 30 carbon atoms having 1 to 4 hydroxyl groups; carboxylic acid; hydroxyl group which is a reaction product of monocarboxylic acid and glycol or trihydric alcohol Containing ester; ester of polycarboxylic acid and polyhydric alcohol; and> NR (R is a hydrocarbon group having 5 to 40 carbon atoms), showing at least one nitrogen having one or more substituents Examples include esters of polyhydric alcohols in combination with compounds; amide compounds of carboxylic acids and alcohol amines, and the like. These can be used alone or as a mixture. Among these, a hydroxyl group-containing ester which is a reaction product of a monocarboxylic acid having 10 to 25 carbon atoms and glycol or a trihydric alcohol and / or an amide compound of a carboxylic acid having 5 to 25 carbon atoms and an alcohol amine are included. More preferably, an amide compound of a monocarboxylic acid having 10 to 25 carbon atoms and glycerin ester and / or a monocarboxylic acid having 5 to 25 carbon atoms and diethanolamine is more preferable.

The addition amount of the friction modifier is not particularly limited, but it may be added together with other additives so that the unwashed actual gum amount of the gasoline composition after the addition satisfies the above-mentioned preferable range. In addition, from the viewpoint that sufficient fuel economy and output improvement effect can be exhibited, while improvement of the effect cannot be expected even if more is added, preferably 10 to 300 mg, more preferably 30 per liter of gasoline of the present invention. It is good to add so that it may become a content rate of -250 mg.
In addition, since a product marketed as a friction modifier is sometimes diluted with an appropriate solvent for an active ingredient that contributes to wear resistance, such a commercial product is added to the gasoline of the present invention. Means the addition amount as an active ingredient.

Other fuel oil additives that can be added to the gasoline of the present invention include surface ignition preventives such as organophosphorus compounds, anti-icing agents such as polyhydric alcohols or ethers thereof, alkali metal salts or alkalis of organic acids. Auxiliary agents such as earth metal salts, higher alcohol sulfates, anionic surfactants, cationic surfactants, antistatic agents such as amphoteric surfactants, colorants such as azo dyes, organic carboxylic acids or their derivatives Rust inhibitors such as alkenyl succinic acid esters, draining agents such as sorbitan esters, discriminating agents such as kilyzanine and coumarin, and odorants such as natural essential oil synthetic fragrances.
One or two or more of these additives can be added, and the total addition amount is preferably 0.1% by mass or less based on the total amount of gasoline.

  EXAMPLES The present invention will be specifically described below with reference to examples, but the present invention is not limited to these examples.

[Examples 1 to 4 and Comparative Examples 1 and 2]
A Fischer-Tropsch (FT) reaction was applied to a mixed gas containing hydrogen and carbon monoxide as main components to obtain an FT synthesis substrate A having a distillation temperature range of 35 ° C. to 165 ° C. The FT synthetic substrate A contains a normal paraffin content of 73.6% by volume, an isoparaffin content of 2.5% by volume, and an olefin content of 23.9% by volume. 5% by volume of this FT synthetic base A, gasoline base such as reformed gasoline, catalytic cracking gasoline, alkylate, toluene, normal butane, antioxidant, metal deactivator, detergent dispersant, friction modifier Was blended to prepare the gasoline composition of Example 1.

  FT synthesis base material having a distillation temperature range of 35 ° C. to 80 ° C. by hydrotreating a naphtha fraction obtained by applying an FT reaction to a mixed gas mainly composed of hydrogen and carbon monoxide B was obtained. The FT synthesis base material B contains a normal paraffin content of 90.7% by volume and an isoparaffin content of 9.3% by volume. 6% by volume of this FT synthetic base material B, gasoline base materials such as reformed gasoline, catalytic cracking gasoline, alkylate, toluene, normal butane, antioxidants, metal deactivators, detergent dispersants, friction modifiers Was added to prepare the gasoline composition of Example 2.

  Distillation as a naphtha of a side reaction product when hydrotreating an intermediate fraction at 150 ° C. to 360 ° C. obtained by applying an FT reaction to a mixed gas containing hydrogen and carbon monoxide as main components FT synthetic substrate C having a temperature range of 35 ° C to 165 ° C was obtained. The FT synthetic substrate C contains a normal paraffin content of 59.6% by volume and an isoparaffin content of 40.4% by volume. 6% by volume of this FT synthetic base material C, gasoline base materials such as reformed gasoline, catalytic cracking gasoline, alkylate, toluene, normal butane, antioxidants, metal deactivators, detergent dispersants, friction modifiers Was added to prepare the gasoline composition of Example 3.

  FT synthesis substrate D having a distillation temperature range of 35 ° C. to 165 ° C. by hydrocracking FT wax obtained by applying an FT reaction to a mixed gas mainly composed of hydrogen and carbon monoxide. Got. The FT synthetic substrate D contains a normal paraffin content of 22.1% by volume and an isoparaffin content of 77.9% by volume. 7 volume% of this FT synthetic base D, gasoline base such as reformed gasoline, catalytic cracking gasoline, alkylate, toluene, normal butane, antioxidant, metal deactivator, detergent dispersant, friction modifier Was added to prepare a gasoline composition of Example 4.

FT synthetic base D 32% by volume, gasoline base such as reformed gasoline, catalytic cracking gasoline, alkylate, toluene, normal butane, antioxidant, metal deactivator, detergent dispersant, friction modifier oxidation The gasoline composition of Comparative Example 1 was prepared by blending the inhibitor.
Comparative Example 2 is a commercially available premium gasoline.

  Table 1 shows various properties of the gasolines of Examples 1 to 4 and Comparative Examples 1 and 2.

(Property measurement)
The properties of the substrate and the properties of the test gasoline in the examples and comparative examples were measured by the following methods.
The research method octane number and the motor method octane number are values based on the research method octane number and the motor method octane number measured according to JIS K 2280 “Testing method for octane number and cetane number”.
The sulfur content was measured according to JIS K 2541 “Crude oil and petroleum products—sulfur content test method”.
The lead content was measured according to JIS K 2255 “Test method for lead content in gasoline”.
The distillation properties (IBP, T10, T30, T50, T70, T90, EP) were all measured according to JIS K 2254 “Petroleum products—Distillation test method—Atmospheric pressure method”.
The vapor pressure (@ 37.8 ° C.) was measured according to JIS K 2258 “Crude oil and fuel oil vapor pressure test method (Lead method)”.
The density (@ 15 ° C.) was measured according to JIS K 2249 “Crude oil and petroleum product density test method and density / mass / capacity conversion table”.
The oxidation stability was measured according to JIS K 2287 “Gasoline Oxidation Stability Test Method (Induction Period Method)”.
Copper plate corrosion was measured in accordance with JIS K 2513 “Petroleum products—Copper plate corrosion test method” (test temperature 50 ° C., test time 3 hours).
The unwashed actual gum amount and the washed actual gum amount were measured according to JIS K 2261 “Petroleum products—Automotive gasoline and aviation fuel oil—Real gum test method—Jet evaporation method”.
Benzene was measured according to JIS K 2536 “Petroleum products—component test method—aromatic test method using gas chromatography”.
The aromatic content and olefin content were measured according to JIS K 2536 “Petroleum products—component test method—fluorescent indicator adsorption method”.
The kerosene content was measured in accordance with the provisions of JIS K 2536 “Petroleum product-component test method”.
Manganese, iron and sodium contents are “combustion ashing-inductively coupled plasma emission method”, potassium content is “combustion ashing-atomic absorption method”, and phosphorus content is ASTM D3231 “Standard Test Method for Phosphorus in Measured by “Gasoline”.

(Gasoline supply source diversification index)
For the gasolines of Examples and Comparative Examples, the diversification index of the supply source as the blending ratio of the base material that can be used as a raw material other than crude oil from the blending amount of the FT synthetic base material and the blending amount of the gasoline base material using crude oil as the raw material Asked.

(Acceleration performance evaluation)
The acceleration performance was evaluated using the following test vehicle on a chassis dynamometer maintained at an environmental temperature of 25 ° C. and an environmental humidity of 50%. In the test, after the test vehicle is sufficiently warmed up, the full acceleration from 50 km / h to 110 km / h is performed 10 times in the D range (OD is on), and it is necessary to reach 60 km to 100 km / h. The time was measured, and the average value of the seven required times excluding the first three times was defined as the acceleration time.
[Test vehicle]
Engine: Inline 4 cylinder (Premium gasoline specification, with supercharger)
Displacement: 1998cc
Injection system: Multi-point system Mission: Automatic transmission Exhaust gas purification system: Three-way catalyst, air-fuel ratio feedback control Complies with 2000 exhaust gas regulations

(Exhaust gas test)
In the exhaust gas test, the emissions of CO and NOx contained in the exhaust gas were measured using the above-described test vehicle in accordance with the technical guidelines of the gasoline automobile 10.15 mode exhaust gas measurement by the Ministry of Land, Infrastructure, Transport and Tourism.

(Fuel consumption test)
The fuel consumption test was measured using the above-described test vehicle according to the gasoline automobile 10.15 mode fuel consumption test method by the Ministry of Land, Infrastructure, Transport and Tourism.

  As shown in Table 2, the gasolines of the present invention (Examples 1 to 4) contain a base material derived from FT synthesis, thereby diversifying the supply source, as well as good acceleration performance, low exhaust gas (CO, It can be seen that NOx) level and good fuel efficiency can be realized.

Claims (13)

The research method octane number of the obtained composition is 96.0 or more , comprising the step of mixing an FT synthesis base material that is all or part of a fraction having a distillation temperature range of 25 ° C. to 220 ° C. , Motor method octane number 84.0 or more, sulfur content 10 mass ppm or less, 10% by volume distillation temperature 35 ° C. or more and 70 ° C. or less, 30% by volume distillation temperature 55 ° C. or more and 77 ° C. or less, 50 volumes % Distillation temperature is 75 ° C. or more and 110 ° C. or less, 70 vol% distillation temperature is 95 ° C. or more and 135 ° C. or less, 90 vol % distillation temperature is 115 ° C. or more and 180 ° C. or less, distillation end point is 220 ° C. or less, Reed vapor pressure Is 44 kPa to 93 kPa, density (15 ° C.) is 0.690 g / cm ^{3 to} 0.783 g / cm ³ , oxidation stability is 240 minutes or more, copper plate corrosion (50 ° C., 3 hours) is 1 or less, actual cleaning Ga There 5 mg / 100 ml or less, unwashed actual gum 30 mg / 100 ml or less, the preparation of non-lead gasoline composition benzene content of Ru der than 1% by volume. 2. The method for producing an unleaded gasoline composition according to claim 1, wherein the normal paraffin content in the FT synthetic base contained in the gasoline is 75% by volume or less. The method for producing an unleaded gasoline composition according to claim 1 or 2, wherein the content of isoparaffin in the FT synthetic base contained in gasoline is 20% by volume or more. The method for producing an unleaded gasoline composition according to any one of claims 1 to 3, wherein the olefin content in the FT synthetic base contained in gasoline is 5% by volume or more. The content of the FT synthetic base material that is all or part of a fraction having a distillation temperature range of 25 ° C. to 220 ° C. is 3% by volume to 30% by volume with respect to the total amount of gasoline. The manufacturing method of the unleaded gasoline composition in any one of Claims 1-4. The method for producing an unleaded gasoline composition according to any one of claims 1 to 5, wherein kerosene is not contained. The method for producing an unleaded gasoline composition according to any one of claims 1 to 6, wherein the aromatic content is 10 vol% or more and 45 vol% or less. The method for producing an unleaded gasoline composition according to any one of claims 1 to 7, wherein the olefin content is 35% by volume or less. Sensitivity is 12.5 or less, The manufacturing method of the unleaded gasoline composition in any one of Claims 1-8 characterized by the above-mentioned. Manganese content is 2 mass ppm or less, iron content is 2 mass ppm or less, sodium content is 2 mass ppm or less, potassium content is 2 mass ppm or less, and phosphorus content is 2 mass ppm or less. The method for producing an unleaded gasoline composition according to any one of claims 1 to 9, wherein: The method for producing an unleaded gasoline composition according to claim 1, comprising an antioxidant and a metal deactivator. The manufacturing method of the unleaded gasoline composition in any one of Claims 1-11 containing a cleaning dispersant. The method for producing an unleaded gasoline composition according to any one of claims 1 to 12, further comprising a friction modifier.