JP2008138187A - Method for producing gasoline composition - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a method for producing a gasoline composition which has a low olefin content, a low sulfur content, excellent storage stability and environmental protection, high RON without increasing aromatic hydrocarbons, and sufficient practical performances. <P>SOLUTION: This method for producing a gasoline composition is characterized by hydrocracking a hydrocarbon fraction having a 10 vol.% distillation temperature of ≥180°C and a 90 vol.% distillation temperature of ≤350°C in a distillation property to convert ≥50% of a fraction having a boiling point of ≥215°C into a fraction having a boiling point of <215°C, obtaining a selectively hydrocracked product oil having a hydrocrack product oil aromatic ring-composing carbon content/hydrocarbon fraction aromatic ring-composing carbon content ratio (aromatic ring carbon residue ratio) of ≥0.5, fractionally distilling the selectively hydrocracked product oil, and then mixing the obtained selectively hydrocracked gasoline base material with one or more other gasoline base materials. <P>COPYRIGHT: (C)2008,JPO&INPIT

Description

  The present invention relates to a method for producing a gasoline composition having excellent driving characteristics while considering environmental conservation.

  In order to reduce the emission of carbon dioxide, which is considered to be one of the global warming gases, it is effective to increase the gasoline research octane number (RON). JIS K 2202 stipulates No. 1 automobile gasoline with RON of 96.0 or more and No. 2 automobile gasoline with 89.0 or more. The former is marketed as high-performance premium gasoline and the latter as regular gasoline. Yes. Conventionally, premium gasoline has a catalytic reforming gasoline base, a base with more than 100 RON such as methyl-t-butyl ether (MTBE), an alkylate gasoline base, a catalytic cracking gasoline lighter than 93 Manufactured by blending various gasoline base materials, centering on base materials with RON. Further, regular gasoline is produced by adding aromatic hydrocarbons, desulfurized straight naphtha having a low RON, etc. mainly on catalytic cracking gasoline bases (see Non-Patent Document 1).

  On the other hand, the need for increased production of petrochemical products has increased due to the increase in overseas demand for petrochemical products, and the operation of catalytic reforming gasoline production equipment has increased to produce aromatic hydrocarbons as petrochemical raw materials. Along with this, heavy aromatic hydrocarbons, which are by-products, are also produced in large quantities. This heavy aromatic hydrocarbon is effective as a gasoline base material because it contains almost no sulfur and has a high RON. However, when using a heavy base material with such a high boiling point, there is a restriction on the mixing balance that it is necessary to mix a light hydrocarbon base material with a certain ratio or more to keep the volatility after gasoline preparation within a certain range. In addition, if the amount of heavy aromatic hydrocarbons in the gasoline is too large, there are problems such as the acceleration of the gasoline engine and the deterioration of the exhaust gas characteristics, and it cannot be used much.

A method for improving the wear resistance and lubricity by specifying a specific aromatic hydrocarbon content of 9 carbon atoms is disclosed (see Patent Document 1). A method for improving exhaust gas characteristics by reducing aromatic hydrocarbons is also disclosed (see Patent Document 2). However, since the heavy aromatic hydrocarbon fraction with high RON is reduced, RON, vapor pressure, distillation properties (10, 50, 90 vol% distillation temperature, etc.) can be maintained in an appropriate range. Further, there is no disclosure regarding a specific manufacturing method.
Furthermore, a gasoline composition having improved exhaust gas characteristics by reducing the content of aromatic hydrocarbons having 9 or more carbon atoms is also disclosed (see Patent Document 3), but it is also a heavy aromatic having a high RON. Since the hydrocarbon fraction is reduced, RON, vapor pressure, etc. cannot be maintained in an appropriate range, and there is no disclosure regarding a specific production method.

  Olefins that contribute greatly to the improvement of RON together with aromatic hydrocarbons and are widely used are generally contained in catalytic cracked gasoline and other various cracked gasolines (see Non-Patent Document 2). However, olefinic compounds have disadvantages such as photochemical instability and precipitation of solid compounds such as sludge, which causes problems in storage stability. Further, among olefin compounds having relatively low molecular weight, although RON is high, the vapor pressure tends to be high, and as a base material for summer gasoline, a base having a low vapor pressure is used to offset the high vapor pressure. Not much can be used because the material is required. Further, most of the aromatic hydrocarbons have 100 or more RON, whereas olefin compounds have a range from about 70 to about 110, and it is necessary to select and use an appropriate fraction.

  In addition to olefins, isoparaffins may be mentioned as compounds with high RON. As a method for selectively producing isoparaffin to improve RON, skeletal isomerization of hydrocarbons is known (see Non-Patent Document 3). However, such a skeletal isomerization reaction has not yet reached the production of a gasoline base of more than 90 as RON, and it is difficult to replace it with an aromatic compound-based gasoline base.

  Similar to the isomerization reaction, there is a process using an alkylation reaction as a method for selectively producing isoparaffin. The alkylation reaction is a reaction in which an acid catalyst such as sulfuric acid is used to react mainly with an olefin having 4 carbon atoms and isoparaffin to produce an isoparaffin having 8 carbon atoms. Many processes have already been operated all over the world. (See Non-Patent Document 4). However, alkylate gasoline has a RON slightly higher than that of isomerized gasoline, but is about 95, and is not at a level that can be replaced with an aromatic base material. In addition, since a relatively expensive hydrocarbon compound having 4 carbon atoms must be used as a raw material, it cannot be produced in large quantities due to supply and cost constraints.

Looking at the actual situation of gasoline production in consideration of the above situation, as a method for producing aromatic hydrocarbons having a high RON, straight-line desulfurization obtained through atmospheric distillation equipment and hydrodesulfurization equipment of crude oil Processes for catalytic reforming heavy naphtha fractions have been widely used. However, as mentioned above, the demand for aromatic hydrocarbons as a petrochemical feedstock is increasing, so a new route to produce aromatic gasoline bases is desired. It is desired to selectively produce aromatic hydrocarbons from heavy hydrocarbons that are expected to be.
On the other hand, a gasoline composition having a high RON and sufficient practical performance without increasing the content of heavy aromatic hydrocarbons and olefins, and a low sulfur content of 10 ppm by mass or less, and its production A method is desired.
Japanese Patent Laid-Open No. 2001-226683 JP 2003-253276 A JP 2004-244532 A SAE Paper No. 930143, March, 1993, “Heavy Hydrocarbon / Volatility Study: Fuel Blending And Analysis for the Auto / Oil Air Quality Improvement Research”. Nisseki Review, “Market Survey Results on Gasoline Quality”, Volume 40, Issue 3, p26-52, August 1998 Edited by Petroleum Society, “Petroleum Refining Process”, p235-245, Kodansha Scientific, 1998 Edited by Petroleum Society, “Petroleum Refining Process”, p209-216, Kodansha Scientific, 1998

  The present invention uses a specific hydrocracked gasoline base material, has a low olefin content and sulfur content, has excellent storage stability, environmental conservation, and without specially increasing aromatic hydrocarbons, It is an object of the present invention to provide a method for producing a gasoline composition having a high RON and sufficient practical performance.

As a result of diligent research to solve the above problems, the present inventors have conducted hydrocracking of polycyclic aromatic hydrocarbons contained in heavy oil and selectively selectively produce one ring. Gasoline blended with product oil obtained by selective hydrocracking to produce aromatic hydrocarbons has good operability, acceleration and exhaust gas characteristics. In addition, high RON improves fuel efficiency and impacts on the environment. It was found to be reduced. Furthermore, the improvement in the properties of gasoline is due to the aromatic hydrocarbons having 9 carbon atoms such as 1,3,5-trimethylbenzene and 1,2,4-trimethylbenzene contained in the selective hydrocracking product oil. I found it.
Generally, aromatic hydrocarbons having 9 carbon atoms are said to deteriorate exhaust gas properties (Patent Documents 1 to 3). However, among aromatic hydrocarbons having 9 carbon atoms, 1,3,5-trimethylbenzene (135TMB) and 1,2,4-trimethylbenzene (124TMB) have extremely high RON values of 120 and 111, respectively, and low leads. It has a vapor pressure (RVP). That is, these gasoline compositions having a higher content of specific aromatic hydrocarbons maintain an excellent balance between distillation properties and Reed vapor pressure (RVP), while maintaining olefins and aromatic hydrocarbons, and further having 9 carbon atoms. A high RON, low sulfur environment-friendly gasoline composition can be prepared without increasing the total amount of aromatic hydrocarbons.
That is, the RON is 90 or more, the sulfur content is 10 mass ppm or less, the aromatic content is 20 to 40% by volume, the olefin content is 20.0% by volume or less, and the content of the aromatic hydrocarbon having 9 carbon atoms is 10 volume% or less, the ratio (capacity) of the total content of 1,2,4-trimethylbenzene and 1,3,5-trimethylbenzene to the content of aromatic hydrocarbon having 9 carbon atoms is 0.46 or more, and A gasoline composition having an oxygen-containing compound content of 0 to 15% by volume can be prepared as a low-sulfur environment-friendly gasoline composition. Preferably, the ratio (capacity) of the content of 1,3,5-trimethylbenzene to the content of aromatic hydrocarbon having 9 carbon atoms is 0.10 or more, and the sulfur content is 1 mass ppm or less. It was found that a gasoline composition having a reed vapor pressure of 44 to 65 kPa and an olefin content of 5.0% by volume or less is excellent.
Thus, the present inventors have found a specific hydrocarbon compound having a high RON, a low RVP, and a preferable distillation property, and controlling the content thereof, thereby maintaining a high RON and a sulfur content. The present inventors have found that a gasoline composition having sufficient practical performance can be prepared in addition to excellent storage stability and environmental conservation, and the present invention has been completed based on such knowledge.

That is, this invention is a manufacturing method of the gasoline composition shown below.
(1) Hydrocracking a hydrocarbon fraction having a 10% by volume distillation temperature of 180 ° C. or higher and a 90% by volume distillation temperature of 350 ° C. or lower in distillation properties to obtain a boiling point of 215 ° C. or higher and a fraction of 50% or higher. Ratio of the carbon ratio constituting the aromatic ring of the hydrocracked product oil to the carbon ratio constituting the aromatic ring of the hydrocarbon fraction and converted to a fraction lower than 215 ° C. (aromatic ring carbon residual ratio) A hydrocracking product oil having a hydrocracking ratio of 0.5 or more is obtained, and the selective hydrocracking gasoline base material obtained by fractional distillation is mixed with another gasoline base material. A method for producing a gasoline composition.
(2) The gasoline composition according to (1), wherein the hydrocarbon fraction is at least one hydrocarbon fraction obtained from a catalytic cracking device, a thermal cracking device, an ethylene cracker device, and a catalytic reforming device. Production method.
(3) When the catalytic cracking naphtha fraction obtained from the catalytic cracking apparatus and / or the desulfurized catalytic cracking naphtha fraction obtained by desulfurizing it as another gasoline base material is mixed, the blending amount is 10% by volume or less. The manufacturing method of the gasoline composition as described in (1).
(4) The above-mentioned selective hydrocracking catalyst in which the catalyst used for hydrocracking is a support comprising a composite oxide supporting at least one metal selected from Group 6 and Group 8 of the periodic table ( The manufacturing method of the gasoline composition as described in 1)-(3).

The gasoline composition obtained by the production method of the present invention is a 1-ring aromatic hydrocarbon obtained by the selective hydrocracking reaction of a polycyclic aromatic hydrocarbon in the presence of a solid acid catalyst, particularly a high RON 1 Since it is a gasoline composition containing 1,2,4-trimethylbenzene and 1,3,5-trimethylbenzene, it maintains a high RON while reducing the content of aromatic hydrocarbons and olefins. Therefore, it is possible to reduce sulfur content and olefin content while maintaining high RON, and to provide a gasoline composition having sufficient practical performance in addition to excellent storage stability and environmental conservation. it can.
Moreover, according to the production method of the present invention, the gasoline composition contains a high concentration of monocyclic aromatic hydrocarbons obtained by selective hydrocracking reaction of polycyclic aromatic hydrocarbons in the presence of a solid acid catalyst. It can be easily prepared by using hydrocracked product oil.

[Method for producing gasoline composition]
The method for producing the gasoline composition of the present invention will be described in detail below.

[Selective hydrocracking process]
In the method for producing a gasoline composition of the present invention, a hydrocracking product oil containing hydrocracking polycyclic aromatic hydrocarbons in a hydrocracking feedstock and selectively containing high concentrations of monocyclic aromatic hydrocarbons In particular, a hydrocracked gasoline base material that is a fraction having an increased concentration of the desired monocyclic aromatic hydrocarbon is used. In normal hydrocracking, aromatic hydrocarbons, including polycyclic aromatic hydrocarbons, are converted to naphthenes, olefins, or paraffins, where selective means to leave as much as possible of the single ring aromatic hydrocarbon. It means hydrogenolysis. Further, as the monocyclic aromatic hydrocarbon, toluene and xylenes are preferable in addition to alkylbenzene having 9 carbon atoms such as 135TMB and 124TMB having high RON.
Hereinafter, regarding the selective hydrocracking, the feedstock oil, the selective hydrocracking catalyst, the reaction conditions, the properties of the reaction product oil, and the separation step will be described in the following order.

[Raw oil used for selective hydrocracking]
The hydrocarbon fraction used as the feedstock for selective hydrocracking needs to have suitable distillation properties in order to obtain a high RON gasoline fraction. That is, a raw material oil having a distillation property of 10% distillation temperature of 180 ° C. or higher and 90% distillation temperature of 350 ° C. or lower is used. Preferably, the 10% distillation temperature is 190 to 240 ° C, and the 90% distillation temperature is 260 to 320 ° C. On the basis of these criteria, a raw material that has a large amount of bicyclic aromatic hydrocarbons and does not contain a large amount of tricyclic aromatic hydrocarbons anthracene and phenanthrene (boiling points 339 ° C., 340 ° C.) is selected. Hydrocracking selectively to produce more hydrocarbons.

  Any hydrocarbon fraction may be used as long as it has the above-mentioned distillation properties, for example, a distillate obtained from atmospheric distillation of crude oil, a vacuum gas oil obtained from vacuum distillation of atmospheric residue, and various heavy oils. Distillate obtained from light oil lightening process (catalytic cracker, thermal cracker, etc.), for example, catalytic cracked oil obtained from catalytic cracker, especially heavy cycle oil (HCO) and light cycle oil (LCO) Extraction of pyrolysis oil obtained from pyrolysis equipment (coker, visbreaking, etc.), ethylene cracker heavy residue obtained from ethylene cracker, contact reforming oil obtained from contact reformer, especially contact reformed oil, Aromatic-rich catalytically modified oil obtained by distillation or membrane separation (herein, aromatic-rich catalytically modified oil is an aromatic compound containing 10 or more carbon atoms obtained from a catalytic reformer and containing an aromatic compound) There refers to something more than 50% by volume), an aromatic extraction unit fractions obtained from the manufacture of lubricating base oil, and an aromatic-rich fractions obtained from the solvent dewaxing unit. In addition, a distillate produced from a desulfurization method or a hydroconversion method for purifying an atmospheric distillation residue, a vacuum distillation residue, a dewaxed oil, or the like can also be used. Further, two or more of these hydrocarbon fractions may be mixed and used after adjusting the distillation properties depending on the case. That is, whether it is a single oil or a mixed oil, it may be used after adjusting to a distillation property within a range specified as a raw material oil for hydrocracking. Among the above hydrocarbon fractions, catalytic cracking oil, pyrolysis oil, ethylene cracker heavy residue, and catalytic reforming oil are preferable, and LCO is particularly preferable.

[Selective hydrocracking catalyst]
The catalyst used for the selective hydrocracking reaction carries at least one metal component selected from Groups 6 and 8 of the periodic table on a support containing a composite oxide and a binder that binds the composite oxide. Can be prepared. The selective hydrocracking catalyst has a specific surface area of 100 to 600 m ² / g, a central pore diameter of 4 to 12 nm, and a pore volume in the range of pore diameters of 2 to 60 nm of 0.1 to 1.0 mL / g. Preferably there is.
The specific surface area is a value of a BET specific surface area determined by nitrogen adsorption based on ASTM standard D3663-78, more preferably 150 to 550 m ² / g, and still more preferably 200 to 500 m ² / g. When the BET specific surface area is smaller than the above range, the active metal dispersion is insufficient and the activity is not improved. On the other hand, when the BET specific surface area is too large, sufficient pore volume cannot be maintained, and the diffusion of the reactant becomes insufficient. , Because the progress of the reaction is rapidly inhibited.

  The central pore diameter of the selective hydrocracking catalyst is preferably 4 to 12 nm, more preferably 4.5 to 11 nm, and particularly preferably 5.0 to 10 nm. The pore volume of pores having a pore diameter of 2 to 60 nm is preferably 0.1 to 1.0 mL / g, more preferably 0.15 to 0.8 mL / g, and particularly preferably 0.2 to 0. 0.7 mL / g. The central pore diameter and the pore volume are not preferable because they are too large or too small because there is an appropriate range from the relationship between the size of molecules involved in the reaction and diffusion.

  The pore characteristics of the so-called mesopores, that is, the central pore diameter, the pore diameter, the pore volume, and the relationship between them are measured by the nitrogen gas adsorption method, and the pore volume and the pore diameter by the BJH method or the like. The relationship can be calculated. The central pore diameter is the cumulative volume of each pore diameter when V is the cumulative pore volume of pore diameters of 2 to 60 nm obtained under the condition of a relative pressure of 0.9667 in the nitrogen gas adsorption method. In the cumulative pore volume curve, the pore diameter at which the cumulative pore volume is V / 2.

The composite oxide is selected from silica-alumina, silica-titania, silica-zirconia, silica-magnesia, silica-alumina-titania, silica-alumina-zirconia, tungsten oxide-zirconia, sulfated zirconia, and zeolite. It can also be used individually or in combination of 2 or more types. In particular, when silica-alumina is used as the composite oxide, it is preferably used so that the molar ratio of silica / alumina (SiO ₂ / Al ₂ O ₃ ) is 1 to 20.

As the zeolite, X-type and Y-type zeolites are preferable, and among them, USY zeolite can be suitably used. USY zeolite is ultra-stable Y-type zeolite, and has high resistance to deterioration of crystallinity due to acid treatment, high temperature treatment, steam treatment, etc., and the content of alkali metal ions is less than 4% by mass, Preferably, it is characterized by a lattice constant of less than 1% by mass and 2.46 nm or less, and a silica / alumina (SiO ₂ / Al ₂ O ₃ ) molar ratio of 5 or more.

The USY-type zeolite is preferably a crystalline aluminosilicate having a lattice constant of 2.43 to 2.46 nm. In the case where the lattice constant exceeds 2.46 nm, the crystal structure collapses when it comes into contact with an aqueous solution having a pH of less than 3 during the acid treatment described later, the decomposition activity is lowered, and the yield of the target fraction is reduced. On the other hand, when the lattice constant is less than 2.43 nm, the crystallinity is poor and the amount of acid is small, so that the decomposition activity similarly decreases and the yield of the target fraction decreases. Note that the lattice constant is calculated from the value of the interplanar distance d obtained by the X-ray diffraction method by the following equation.
Lattice constant = d × (h ² + k ² + l ² ) ^1/2
Here, h, k, and l represent Miller indices.

  Various metal ions may be introduced into the crystalline aluminosilicate whose lattice constant has been adjusted in this way to form a transition metal-containing crystalline aluminosilicate or a rare earth-containing crystalline aluminosilicate. When used in the selective hydrocracking reaction described later, the crystalline aluminosilicate, the transition metal-containing crystalline aluminosilicate, or the rare earth-containing crystalline aluminosilicate may be used alone, or two or more of these may be mixed. May be used.

As the binder, porous and amorphous ones such as alumina, silica-alumina, titania-alumina, zirconia-alumina can be suitably used. These inorganic oxides function as a substance that supports an active metal and also serve as a binder that binds the composite oxide, thereby improving the strength of the catalyst. The specific surface area of the binder is desirably 30 m ² / g or more. In addition, powders made of aluminum hydroxide and / or hydrated oxide containing boria (boron oxide), particularly aluminum oxide monohydrate having a boehmite structure such as pseudoboehmite containing boria, are also hydrocracked. Since activity and selectivity can be improved, it can be preferably used.

  The blending ratio of the binder is preferably 5 to 70% by mass, particularly 10 to 60% by mass with respect to the total mass of the composite oxide and the binder constituting the catalyst. If it is less than 5% by mass, the mechanical strength of the catalyst tends to be lowered, and if it exceeds 70% by mass, the hydrocracking activity and selectivity are relatively lowered. When USY zeolite is used as the composite oxide, the mass of USY zeolite relative to the total mass of the composite oxide part and the binder part constituting the catalyst is preferably 1 to 80% by mass, particularly preferably 10 to 70% by mass. If the amount is less than 1% by mass, the effect of improving the decomposition activity due to the use of USY zeolite is hardly exhibited, and if it exceeds 80% by mass, the middle distillate selectivity is relatively lowered.

  The catalyst used in the selective hydrocracking reaction in the present invention preferably contains a metal selected from Groups 6 and 8 of the periodic table as an active component. Among these metals, Group 6 molybdenum, tungsten, and Group 8 iron, ruthenium, osmium, cobalt, rhodium, iridium, nickel, palladium, and platinum are particularly preferably used. These metals can be used alone or in combination of two or more. These metals are added so that the total amount of Group 6 and Group 8 metal elements in the hydrocracking catalyst is 0.05 to 35% by mass, particularly 0.1 to 30% by mass. It is preferable to do. When molybdenum is used as the metal, the content thereof is preferably 5 to 20% by mass, particularly 7 to 15% by mass in the hydrocracking catalyst. When tungsten is used as the metal, the content thereof is preferably 5 to 30% by mass, particularly 7 to 25% by mass in the hydrocracking catalyst. If the addition amount of molybdenum or tungsten is less than the above range, the hydrogenation function of the active metal necessary for the hydrocracking reaction is insufficient, which is not preferable. On the other hand, when the amount is larger than the above range, the added active metal component tends to aggregate and is not preferable.

  When molybdenum or tungsten is used as the metal, it is more preferable to add cobalt or nickel to improve the hydrogenation function of the active metal. In this case, the total content of cobalt or nickel is preferably 0.5 to 10% by mass, particularly 1 to 7% by mass in the hydrocracking catalyst. When one or more of rhodium, iridium, platinum and palladium are used as the metal, the content is preferably 0.1 to 5% by mass, particularly preferably 0.2 to 3% by mass. If it is less than this range, a sufficient hydrogenation function cannot be obtained, and if it exceeds this range, the addition effect is small and it is not economical, which is not preferable.

[Reaction conditions for selective hydrocracking]
In selective hydrocracking, for example, operating conditions such as temperature, pressure, hydrogen flow rate, and liquid space velocity may be appropriately adjusted according to the properties of the raw material, the quality of the product, the production amount, and the capacity of the purification equipment. The raw material for selective hydrocracking reaction and the hydrocracking catalyst are heated in the presence of hydrogen at a temperature of 300 to 480 ° C., more preferably 330 to 450 ° C., still more preferably 340 to 430 ° C., and a pressure of 1 to 10 MPa. More preferably 2 to 8 MPa, liquid space velocity (LHSV) 0.1 to 10.0 h ⁻¹ , more preferably 0.1 to 8.0 h ⁻¹ , still more preferably 0.2 to 5.0 h ⁻¹ , hydrogen / Hydrocarbon (volume ratio) 100 to 5,000 NL / L, preferably 150 to 3,000 NL / L. By the above operation, the polycyclic aromatic hydrocarbon in the raw material for selective hydrocracking reaction is decomposed and converted to a desired monocyclic aromatic hydrocarbon. Outside the range of the above operating conditions, it is not preferable for reasons such as insufficient cracking activity or rapid deterioration of the catalyst.

[Properties of selective hydrocracking oil]
In the present invention, the selective hydrocracking product oil (SHC) is a ratio of the carbon ratio constituting the aromatic ring in the produced oil to the carbon ratio constituting the aromatic ring in the feed oil (aromatic ring carbon). Residual ratio) is 0.5 or more, more preferably 0.6 or more, and particularly preferably 0.7 or more. Here, when the aromatic ring carbon residual ratio is smaller than 0.5, the monocyclic aromatic hydrocarbon produced by hydrogenation of the polycyclic aromatic hydrocarbon is further hydrogenated and the target compound cannot be obtained. Moreover, it is not preferable for reasons such as that coking is promoted due to excessive progress of the decomposition reaction and the catalytic activity is thereby lowered.

  Furthermore, in the selective hydrocracking of the present invention, 50% by volume or more of the fraction having a boiling point of 215 ° C. or higher contained in the feedstock is converted into a fraction having a temperature of less than 215 ° C. The selective hydrocracked product oil preferably has a hydrocarbon content of 50% by volume or more, more preferably 60% by volume, with a hydrocarbon having a boiling point of 215 ° C. or lower, that is, a lighter hydrocarbon than naphthalene (boiling point 218 ° C.). Above, more preferably 70% by volume or more, and most preferably 100%. Further, the content of the polycyclic aromatic hydrocarbon in the hydrocracked oil obtained by hydrocracking treatment is preferably as small as possible, and is 10% by volume or less, more preferably 7% by volume or less.

[Preparation of selective hydrocracked gasoline base]
The selective hydrocracked product oil is then subjected to a separation step so as to be a desired gasoline base (selective hydrocracked gasoline base: SHCG). The separation process is not particularly limited, and any known method such as precision distillation, adsorption separation, sorption separation, extraction separation, membrane separation and the like can be adopted depending on the product properties, but precision distillation is generally preferable. used. Specifically, using a distillation column packed with a filler, the reflux ratio is, for example, 1/1, preferably 3/1, more preferably 5/1, and the more the number of theoretical plates, the more preferable, for example, 15 plates, Precision distillation is performed in 30 or more stages, more preferably 50 or more stages. Distillation temperature and pressure conditions are not limited because they vary depending on the boiling range of the distillation separation, and the feedstock temperature, tower top temperature, reflux temperature, distillation tower What is necessary is just to set a vacuum etc. suitably.

  As the gasoline fraction obtained from the selective hydrocracking used in the present invention and the selective hydrocracked gasoline base (SHCG), the 10% distillation temperature is preferably 90 to 150 ° C, more preferably 100 to 130 ° C. The 90% distillation temperature is preferably 140 to 180 ° C, more preferably 150 to 170 ° C, and the distillation conditions are set so as to obtain such a boiling range. That is, it is preferably set so as not to contain benzene (boiling point 80 ° C.) or C10 aromatic hydrocarbon (boiling point 170-200 ° C.) as much as possible. Specifically, a fraction lighter than the boiling point 80 ° C. It is preferably 5% by volume or less, more preferably 1% by volume or less. Similarly, the fraction heavier than the boiling point of 170 ° C. is preferably 5% by volume or less, more preferably 1% by volume or less. By using a gasoline base having such a boiling range, that is, a gasoline base having a preferable aromatic composition that is neither too light nor too heavy, a product gasoline having appropriate RON, vapor pressure, and distillation properties can be obtained. it can.

[Blend process]
In the present invention, the gasoline composition comprises a gasoline fraction (selective hydrocracked gasoline base: SHCG) of the selective hydrocracked product oil obtained by processing as described above and another gasoline base. It can be produced by blending at an appropriate ratio.
The selective hydrocracked gasoline base material obtained by the treatment as described above is used in an amount of 5% by volume or more, preferably 10% by volume or more and 50% by volume or less, preferably 45% by volume or less based on the gasoline composition. It is preferable. If it is less than 5% by volume, it is difficult to maintain an aromatic hydrocarbon having 9 or less carbon atoms at the above specific composition ratio. Since it gets worse, it is not preferable.

  The other gasoline base refers to various gasoline bases that can be used together with the selective hydrocracked gasoline base in preparing the gasoline composition in the present invention, and the gasoline base used in the conventional gasoline production. Materials. Specifically, after hydrodesulfurization of a straight-run naphtha fraction, desulfurized straight-run light naphtha fraction (DSLG) obtained by distillation separation of the light fraction, isomerized gasoline (ISO) obtained by skeletal isomerization (ISO) ), Alkylate gasoline (ALKG) obtained by alkylating butylene fraction and isobutane fraction, catalytic cracked naphtha fraction (FCCG), or desulfurized catalytic cracked naphtha fraction (DS-FCCG) or heavy light Contains most of the separated catalytic cracked light naphtha fraction (FL), catalytic reformed gasoline obtained by reforming desulfurized heavy naphtha with a solid reforming catalyst, and benzene obtained by distillation of contact reformed gasoline Fractions mainly composed of 7 carbon atoms (AC7), fractions mainly composed of 8 carbon atoms (AC8), fractions mainly composed of 9 carbon atoms (AC9), various petroleum refining processes And oil Examples of the gasoline fraction by-produced from the chemical process include isolated butane and pentane (especially isopentane (iC5)) and aroma compounds such as so-called BTX. Furthermore, so-called “oxygen-containing compounds” such as alcohols such as ethanol, ethers and esters which are derivatives from alcohols can also be used.

The blending amount of the other gasoline base is not particularly limited, but an appropriate blending amount can be selected from the viewpoint of product gasoline characteristics.
FCCG and DS-FCCG are gasoline bases that have a relatively high RON and can be manufactured at low cost, so in many cases they may be used up to about 80% by volume, but the olefin content is slightly higher, so products In order to reduce the olefin content therein, it may be preferable to reduce the blending amount of these base materials. In such a case, the preferred blending amount is 10% by volume or less, particularly 5% by volume or less.

  For catalytically reformed gasoline and AC7, AC8, AC9 derived therefrom, it is preferable that the specific aromatic hydrocarbon constituent ratio having 9 carbon atoms is not controlled as in the gasoline composition of the present invention. Preferably it is 14 volume% or less, Most preferably, it is 10 volume% or less.

  Further, as the oxygen-containing compound, for example, alcohols having 2 to 5 carbon atoms and ethers having 4 to 8 carbon atoms are preferable, and specifically, ethanol (EtOH), propyl alcohols, butyl alcohols and the like are used. Alcohol and ethers and esters which are derivatives from alcohol, for example, ethers such as ethyl isopropyl ether, ethyl tertiary butyl ether (ETBE), ethyl secondary butyl ether (ESBE), diisopropyl ether, tertiary amyl ethyl ether (TAEE), etc. And esters such as ethyl acetate and ethyl propionate.

  These oxygen-containing compounds are blended in an amount of 0 to 15% by volume, preferably 3 to 12% by volume, more preferably 5 to 10% by volume based on the total gasoline composition. If the amount is too small, the effect of addition is small, and if the amount is too large, impurities such as moisture are easily taken in, which may cause troubles such as corrosion of piping and sealing materials. For example, since ethanol dissolves water very well, if it is contained in a large amount in automobile fuel, water may accumulate in the fuel tank, which may have an adverse effect. Furthermore, when the fuel contains a large amount of oxygen-containing compounds, for example, if the amount exceeds 15% by volume, it will deviate from the optimum value of the air / fuel ratio of the existing engine, resulting in an excess of oxygen. There is a tendency for the amount of substances (NOx) to increase. Further, since oxygen-containing compounds generally have a lower calorific value than other gasoline base materials and may reduce fuel consumption, it is not preferable to use too much.

[Gasoline composition]
Of the hydrocarbon compounds contained in the gasoline composition, those having aromatic rings are aromatic hydrocarbons (aromatic), those having unsaturated bonds in a form other than aromatic are olefins, those having naphthene rings are naphthenes, and Other hydrocarbon compounds are paraffin. Moreover, among paraffins, linear paraffins are classified as normal paraffins, and those having branches are classified as isoparaffins.
The gasoline composition obtained by the method for producing a gasoline composition of the present invention will be described in detail below.

[Octane number]
The research method octane number (RON) of the gasoline composition is preferably 90 or more, more preferably 93 or more and less than 96, in particular 95, since it is defined as 90 or more in JIS K2202 “Automobile Gasoline” in the case of regular gasoline. More than 96 is preferable. In the case of premium gasoline, since it is defined as 96 or more, it is preferably at least 96, more preferably 98 or more, and particularly preferably 100 or more. When RON is less than 90, there is a risk of knocking or acceleration failure particularly during hill-climbing acceleration, and it is not preferable because of concern about deterioration of fuel consumption.

[Sulfur content]
The sulfur content of the gasoline composition is 10 mass ppm or less, preferably 5 mass ppm or less, more preferably 1 mass ppm or less as elemental sulfur. The sulfur content in gasoline becomes sulfur oxides in the exhaust gas, poisoning the nitrogen oxide removal catalyst that purifies the engine exhaust gas, and reducing the catalytic activity. The poisoned nitrogen oxide removing catalyst is regenerated in a reducing atmosphere to recover its activity. At this time, fuel is used to form a reducing atmosphere, and fuel consumption is deteriorated accordingly. Therefore, the fuel efficiency improves as the sulfur content in gasoline decreases. Furthermore, since a silver alloy is partially used in a fuel tank level gauge of a gasoline vehicle, it is desirable that the corrosion of the silver plate is 1 or less in order to prevent corrosion due to sulfur compounds and the like.

[Olefin content]
The olefin content in the gasoline composition is preferably smaller from the viewpoint of light stability and storage stability, preferably 20.0% by volume or less, more preferably 15.0% by volume or less, and still more preferably 12.0%. It is not more than volume%, particularly preferably not more than 5.0 volume%.

[Aromatic content]
In the gasoline composition, the aromatic hydrocarbon content is preferably 20% by volume or more and 40% by volume or less, the lower limit is more preferably 22% by volume or more, further 25% by volume or more, and particularly preferably 30% by volume or more, The upper limit is more preferably 39% by volume or less. From the viewpoint of maintaining exhaust gas properties and low-temperature drivability, it is preferable that the aromatic content is small. However, 20% by volume or more is preferable for maintaining RON and preventing deterioration of fuel consumption. Further, when the aromatic content exceeds 40% by volume, the combustion chamber deposit increases, which may cause smoldering of the spark plug and increase the concentration of benzene in the exhaust gas. In order to suppress the diffusion of benzene into the atmosphere, the benzene content itself is preferably 1.0% by volume or less, more preferably 0.1% by volume or less.

[Aromatic hydrocarbon content of 9 carbon atoms]
The gasoline composition preferably has a C9 aromatic hydrocarbon (C9A) content of 10% by volume or less, more preferably 8% by volume or less, still more preferably 7% by volume or less, particularly 6 volumes. % Or less. The capacity ratio of the total of 1,3,5-trimethylbenzene (135TMB) and 1,2,4-trimethylbenzene (124TMB) to C9A ((135TMB + 124TMB) / C9A) is 0. 53 or more is preferable, more preferably 0.58 or more, and particularly preferably 0.60 or more. When RON is 90 to 96, it is preferably 0.46 or more, more preferably 0.48 or more, and particularly preferably 0.50 or more.
The 135TMB / C9A ratio (capacity) is preferably 0.14 or more, more preferably 0.16 or more, and particularly preferably 0.18 or more in the case of RON 96 or more. Moreover, when RON is 90-96, 0.10 or more are preferable, More preferably, it is 0.12 or more, Especially preferably, it is 0.14 or more.
When trying to reduce the total content of C9A, which is not very favorable for the exhaust gas properties, to 10% by volume or less, in the case of RON96 or more, (135TMB + 124TMB) / C9A ratio is 0.53 or more, 135TMB / C9A ratio (capacity) If the RON is 90 to 96, the (135TMB + 124TMB) / C9A ratio is 0.46 or more, and the 135TMB / C9A ratio (capacity) is not as high as 0.10, This is not preferable because gasoline properties such as octane number, distillation properties, and vapor pressure cannot be satisfied.

〔density〕
In gasoline composition according to the present invention, the density is preferably 0.70~0.78g / cm ^3, more preferably 0.71~0.77g / cm ^3, more preferably 0.72～0.76G / cm ³ . When the density is less than 0.70 g / cm ³ , the output is reduced and the gasoline consumption is increased. On the other hand, if it exceeds 0.78 g / cm ³ , acceleration may be deteriorated and plug smoldering may occur.

[Distillation properties]
In the gasoline composition according to the present invention, the 50% distillation temperature is preferably 75 to 100 ° C, more preferably 75 to 98 ° C, and further preferably 75 to 96 ° C. When the 50% distillation temperature is less than 75 ° C., it is not preferable from the viewpoint of fuel consumption, and when it exceeds 100 ° C., the normal temperature drivability may be deteriorated. The 10% distillation temperature is preferably 25 to 60 ° C, more preferably 25 to 50 ° C, and further preferably 26 to 45 ° C. If the 10% distillation temperature is too low, there is a possibility of diffusion of light hydrocarbons into the atmosphere, and if it is too high, the low-temperature startability deteriorates, which is not preferable. The 90% distillation temperature is preferably 135 to 180 ° C, more preferably 140 to 170 ° C, and still more preferably 145 to 165 ° C. If the 90% distillation temperature is too low, fuel consumption may be deteriorated, and if it is too high, the deposit in the intake valve and the combustion chamber will increase and the low-temperature operability will deteriorate.

[Lead vapor pressure]
In the gasoline composition according to the present invention, the lead vapor pressure (RVP) at 37.8 ° C. is 44 to 64 kPa, preferably 44 to 63 kPa. When the RVP is high, problems such as an increase in evaporation loss, a concern about vapor lock, and an increase in danger are likely to occur. Moreover, when RVP is low, low temperature startability deteriorates.

〔Additive〕
In the present invention, the gasoline composition can be blended with known fuel additives as required. Although these compounding quantities can be selected suitably, it is usually preferable to set it as 0.1 mass% or less as a total amount of an additive. Examples of additives that can be used in gasoline compositions include amine-based, phenol-based, aminophenol-based antioxidants, Schiff-type compounds, metal deactivators such as thioamide-type compounds, and organic phosphorus-based compounds. Surface ignition inhibitor, detergent dispersant such as succinimide, polyalkylamine, polyetheramine, anti-icing agent such as polyhydric alcohol and its ether, alkali metal salt of organic acid, alkaline earth metal salt, higher alcohol Auxiliary agents such as sulfate esters, anionic surfactants, cationic surfactants, antistatic agents such as amphoteric surfactants, rust inhibitors such as alkenyl succinates, discriminating agents such as quinizarin and coumarin, azo dyes, etc. Can be mentioned.

  Hereinafter, the present invention will be described more specifically by way of examples. However, the present invention is not limited to these examples.

(Preparation of selective hydrocracking catalyst)
200 g of sodium-type Y-type crystalline aluminosilicate (SiO ₂ / Al ₂ O ₃ ratio 2.9, Na ₂ O content 12.3% by mass, lattice constant 2.460 nm) was added to 50 g with 2 L of 1M aqueous ammonium nitrate solution. After ion exchange to proton type at ° C., filtration and washing were performed. Furthermore, after drying at 130 degreeC for 3 hours, it baked at 450 degreeC for 3 hours. As a result of repeating this series of operations 9 times, the Na ₂ O content is reduced to 0.5% by mass, the SiO ₂ / Al ₂ O ₃ ratio is 5.8, and the lattice constant is 2.455 nm. An aluminosilicate was obtained (hereinafter referred to as “SY”). SY was brought into contact with water vapor at 700 ° C. for 3 hours, immersed in 2 L of nitric acid solution at 50 ° C. adjusted to pH 1.5 for 2 hours, filtered and washed. Next, after drying at 130 ° C. for 3 hours, baking was performed at 450 ° C. for 3 hours (hereinafter referred to as “USY”). The USY thus obtained had a SiO ₂ / Al ₂ O ₃ ratio of 10.5, a lattice constant of 2.438 nm, and a specific surface area of 400 m ² / g.

750 g of this USY was mixed with 1,000 g of alumina powder (Alumina Pural SB manufactured by SASOL), 500 ml of 4.0% by weight dilute nitric acid solution and 875 g of ion-exchanged water were added and kneaded, and the columnar shape (pellet) having a three-leaf cross section Extruded. The pellet was dried at 130 ° C. for 6 hours and then calcined at 600 ° C. for 2 hours to obtain a carrier.
This carrier was spray impregnated with an aqueous ammonium molybdate solution and then dried at 130 ° C. for 6 hours. Thereafter, the nickel nitrate aqueous solution was further spray impregnated and then dried at 130 ° C. for 6 hours. Next, catalyst A was obtained by calcination at 500 ° C. for 30 minutes under an air stream. The composition of catalyst A was Mo: 8.0% by mass, Ni: 3.0% by mass, zeolite: 44.5% by mass, and alumina: 44.5% by mass.

When the pore characteristics of this catalyst A were measured by a nitrogen gas adsorption method, the specific surface area was 387 m ² / g, the pore volume in the pore diameter range of ² to 60 nm was 0.543 mL / g, the center pore diameter Was 9.6 nm. Further, this catalyst A had a stable diameter of 1.2 mm, an average length of 4.0 mm, an average side surface crushing strength of 12.0 kg, and a bulk density of 0.668 g / cm ³ . Here, the stable diameter means the height when the pellet is fixed to a flat plate.

(Selective hydrocracking process)
Under the conditions of using catalyst A as the hydrocracking catalyst, reaction pressure: 7.0 MPa, LHSV: 1.0 hr ⁻¹ , hydrogen / feed oil ratio: 1,400 NL / L, reaction temperature: 400 ° C., feed oil The hydrocracking reaction was carried out using catalytic cracking light cycle oil (LCO). Further, the obtained hydrocracked product oil (SHC) is fractionated by precision distillation so that benzene is not contained on the low boiling point side and aromatic hydrocarbons having 10 carbon atoms are not contained on the high boiling point side. Thus, a selective hydrocracked gasoline base material (SHCG) having a distillation property with a 10% distillation temperature of 111.0 ° C. and a 90% distillation temperature of 163.0 ° C. was obtained. Table 1 shows the properties of the selective hydrocracking feedstock (LCO), the selective hydrocracking product oil (SHC), and the selective hydrocracked gasoline base (SHCG). In Table 1, the conversion rate of 215 ° C. or higher fraction is a value obtained by the following formula.
215 ° C. or higher fraction conversion (%) = 100−215 ° C. or higher fraction in product oil (volume%) / 215 ° C. or higher fraction in feed oil (volume%) × 100
Further, the ratio of the carbon ratio constituting the aromatic ring in the hydrocracked product oil to the carbon ratio constituting the aromatic ring in the hydrocarbon fraction (LCO in this case) before hydrocracking (aromatic ring) The carbon residual ratio is also shown in Table 1.

  The gasoline base material obtained as follows was used for preparation of the gasoline composition of an Example and a comparative example. Table 2 shows the properties of these gasoline base materials.

Isopentane fraction (iC5)
This fraction is mainly composed of 5 carbon atoms rich in isopentane. By distilling off a light fraction by-produced by catalytic reforming of desulfurized heavy naphtha, a desulfurized light naphtha fraction, etc., an isoparaffin fraction having a carbon number of 5 with a purity of 95% or more was obtained.

Desulfurized straight run light gasoline (DSLG)
The naphtha fraction of Middle Eastern crude oil was hydrodesulfurized and then subjected to distillation treatment to separate it into desulfurized straight-run light gasoline and desulfurized straight-run heavy gasoline.

Isomerized gasoline (ISO)
An isomerized gasoline having a high isoparaffin content was obtained by skeletal isomerization reaction of desulfurized straight-run light gasoline (DSLG) in the presence of a solid acid catalyst.

Catalytic cracking light naphtha fraction (FL)
Desulfurized light oil or desulfurized heavy oil is used as a raw material, and in the presence of a solid catalyst, a catalytic cracking reaction in a fluidized bed reactor is used to obtain a catalytically cracked naphtha fraction (FCCG) having a high olefin content. This FCCG is divided into a light fraction and a heavy fraction. It is a light fraction (FL) obtained by distillation separation into a fraction.

Desulfurization catalytic cracking naphtha fraction (DS-FCCG)
Use desulfurized gas oil or desulfurized heavy oil as a raw material, and obtain a catalytic cracking naphtha fraction (FCCG) having a high olefin content by catalytic cracking reaction in a fluidized bed reactor in the presence of a solid catalyst. As a result, a hydrocarbon oil having a low sulfur content was obtained. After sulfiding a catalyst having 20% by mass of nickel supported on alumina, the reaction temperature was 250 ° C., the reaction pressure was normal pressure, the LHSV was 4 h ⁻¹ , and the H ₂ / oil ratio was 340 NL / L. Diene reduction treatment was carried out by passing the catalytic cracked naphtha fraction. Furthermore, after reducing the copper zinc aluminum composite oxide (copper content 35 mass%, zinc content 35 mass%, aluminum content 5 mass%) prepared by the coprecipitation method, , Reaction temperature: 100 ° C., reaction pressure: normal pressure, LHSV: 2.0 h ⁻¹ , H ₂ / oil ratio: 0.06 NL / L -FCCG).

Alkylate gasoline (ALKG)
A fraction containing butylene as a main component and a fraction containing isobutane as a main component were reacted with a sulfuric acid catalyst to obtain a hydrocarbon having a high C8 isoparaffin content.

Reformed gasoline (AC7)
Desulfurized heavy naphtha is reacted with a noble metal-based solid reforming catalyst using a moving bed reactor to reform the hydrocarbon into a high aroma content to obtain a reformed gasoline. The reformed gasoline can be used as it is, but here AC7 containing approximately 7% C7 aromatic hydrocarbons as a main component by distillation separation (about 6% C6 aromatic hydrocarbons, carbon number) 7 aromatic hydrocarbons (about 7% by volume), aromatic hydrocarbons having 8 carbon atoms (about 9% by volume), and olefins (about 0.3% by volume).

Reformed gasoline (AC9)
As with AC7, the reformed gasoline is separated by distillation to provide AC9 containing approximately 9% of C9 aromatic hydrocarbons (approximately 8% by volume of C8 aromatic hydrocarbons and 9 hydrocarbons). About 80% by volume, about 2% by volume of C10 aromatic hydrocarbon, and about 0.1% by volume of olefin).

Ethanol (EtOH)
Commercially available fermented ethanol (99 degrees first grade, manufactured by Nippon Alcohol Sales Co., Ltd.) was used.

Ethyl tertiary butyl ether (ETBE)
Ethanol and isobutylene were reacted using an ion exchange resin catalyst (Amberlyst-15) and then purified by distillation to obtain ETBE having a purity of 95% or more.

  These gasoline base materials were blended at the blending ratio shown in the upper part of Tables 3 to 8 to prepare gasoline compositions of Examples 1 to 18 and Comparative Examples 1 to 18. The properties of the gasoline compositions obtained in Examples and Comparative Examples are shown in Table 3 for Examples 1-4 and Comparative Examples 1-4, in Table 4 for Examples 5-7 and Comparative Examples 5-7, Table 8 for Examples 8-9 and Comparative Examples 8-9, Table 6 for Examples 10-13 and Comparative Examples 10-13, and Table 7 for Examples 14-16 and Comparative Examples 14-16 Examples 8 to 18 and Comparative Examples 17 to 18 are shown in Table 8, respectively.

In the above Examples and Comparative Examples, the properties of the raw material oils, product oils, various gasoline base materials and gasoline compositions used were analyzed by the following methods.
The density was measured by the vibration type density test method of JIS K 2249, the Reed method vapor pressure (RVP) was measured by the Reed method vapor pressure test method of JIS K 2258, and the distillation property was measured by the atmospheric pressure distillation test method of JIS K 2254.

  The sulfur content was measured using a fluorescent X-ray method in the high concentration region and a microcoulometric titration method in the low concentration region according to the sulfur content test method of JIS K2541. Silver plate corrosion is the cylinder method (jet fuel) of JIS K2513 (Petroleum products-Copper plate corrosion test method: corresponding ASTM D130). Instead of the copper plate, “14. The silver plate used in the “corrosion test method” was evaluated. The nitrogen content was measured using a chemiluminescence method according to the nitrogen content test method of JIS K 2609.

  The component composition of various hydrocarbon compounds such as aroma, olefin, and paraffin was measured by the all component test method based on the gas chromatograph method of JIS K2536. The research method octane number (RON) was measured by a gas chromatograph method using a PIONA manufactured by Hured Packard.

The type analysis (ring analysis) of aromatic compounds was measured using a high-performance liquid chromatograph apparatus according to the Petroleum Institute method JPI-5S-49-97, and PARTISIL 5 PAC (column size: 25 cm × 4.6 mmφ) and AgNO ₃ -1071Y (7 cm × 4.6 mmφ), normal hexane for mobile phase, and RI method for detection.

The measurement of the aromatic constituent carbon ratio was carried out using deuterated chloroform as a solvent and tetramethylsilane as an internal standard, using a JSX GSX270 nuclear magnetic resonance apparatus. Quantification of aromatic ring carbon and aliphatic carbon for each carbon species classification uses ¹ H-gated decoupling method (SGNNE mode), data points 32,768 points, observation frequency region width 27,027 Hz, pulse width The measurement was performed at 2 μs, a pulse waiting time of 30 s, and an integration number of 2,000 times, and was calculated from the integration ratio of the signal of the Fourier transformed spectrum. In the obtained spectrum shift value, those in the range of 120 to 150 ppm were attributed to aromatic carbon and expressed as mol% with respect to the total carbon.

  As shown in Tables 3 to 8, the gasoline composition obtained by using the production method of Examples 1 to 18 and the conventional gasolines of Comparative Examples 1 to 18 have gasoline compositions in which the olefin content is reduced to 20% by volume or less. However, in the examples, by using selective hydrocracked gasoline (SHCG) as compared with the comparative example, 1,2,4-trimethylbenzene and 1,3 with respect to the aromatic hydrocarbon content of 9 carbon atoms. The ratio of the total content of 1,5-trimethylbenzene ((124TMB + 135TMB) / C9A) is high, and the content ratio of 1,3,5-trimethylbenzene to the aromatic hydrocarbon content of 9 carbon atoms (135TMB / C9A) Since it is high, RON is high even though the olefin content is reduced. In other words, the gasolines of Examples 1 to 9 have good distillation properties and RVP and high RON even if the sulfur content, olefin content and aroma content are the same as those of Comparative Examples 1 to 9, and excellent practical use. It can be seen that it has performance.

Claims (4)

  In the distillation properties, hydrocracking a hydrocarbon fraction having a 10 vol% distillation temperature of 180 ° C or higher and a 90 vol% distillation temperature of 350 ° C or lower to produce a boiling point of 215 ° C or higher and a fraction of 50% or higher below 215 ° C The ratio of the carbon ratio constituting the aromatic ring of the hydrocracked product oil to the carbon ratio constituting the aromatic ring of the hydrocarbon fraction (aromatic ring carbon residual ratio) is 0. A gasoline composition characterized by mixing a selective hydrocracked gasoline base obtained by fractionating a selective hydrocracked product oil of 5 or more with another gasoline base Manufacturing method.   The method for producing a gasoline composition according to claim 1, wherein the hydrocarbon fraction is at least one hydrocarbon fraction obtained from a catalytic cracking device, a thermal cracking device, an ethylene cracker device, and a catalytic reforming device.   When the catalytic cracking naphtha fraction obtained from the catalytic cracking apparatus and / or the desulfurized catalytic cracking naphtha fraction obtained by desulfurizing it as another gasoline base material is mixed, the blending amount is 10% by volume or less. 3. A method for producing a gasoline composition according to 2.   The catalyst for use in hydrocracking is a selective hydrocracking catalyst in which at least one metal selected from Groups 6 and 8 of the periodic table is supported on a support made of a complex oxide. The manufacturing method of the gasoline composition in any one of.