JP2006219590A - Method for producing gasoline base - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a method for producing a gasoline base by which the gasoline base can be obtained by effectively utilizing a 4C olefin fraction, and the gasoline base capable of being mixed with other gasoline base without problem is produced while keeping the appropriate properties. <P>SOLUTION: The method for producing the gasoline base comprises a first distillation step for collecting a fraction [fraction (I)] having the boiling point of ≥100°C and ≤160°C from a liquid formed by a polymerization reaction of a butane-butene mixed fraction, a second distillation step for collecting a part [fraction (II)] of a fraction having the boiling point of >160°C and ≤200°C from the fraction from which the fraction (I) has been collected, a hydrogenation step for hydrogenating a mixed fraction of other parts of the fraction from which the fraction (II) has been collected, and a fraction having the boiling point of >200°C, and a third distillation step for collecting a fraction [fraction (III)] having the boiling point of >160°C and ≤200°C from the mixed fraction converted to paraffin. The fractions (I) to (III) are used as the gasoline base singly or by mixing them. <P>COPYRIGHT: (C)2006,JPO&NCIPI

Description

  The present invention relates to a method for producing a gasoline base material, in which a fraction useful as a gasoline base material is recovered from a polymerization reaction product liquid of a butane-butene mixed fraction by a multistage distillation process.

  With the development of technological development such as steam cracking and catalytic cracking of naphtha and light oil, C4 fraction containing components having 4 carbon atoms such as n-butene, isobutene, n-butane and isobutane (hereinafter simply referred to as “ “C4 fraction”) can be easily manufactured and is available on the market. On the other hand, due to the widespread use of C4 fractions, methods for effectively using C4 olefin fractions obtained by extracting and removing diene components (butadiene and the like) have been studied.

  Against this background, in recent years, various methods for producing a gasoline base material by polymerizing a C4 olefin fraction derived from cracking have been provided (for example, Patent Documents 1 to 3). In the method for producing a gasoline base material disclosed in Patent Documents 1 to 3, after separation of an unreacted C4 fraction from a dimer or trimer of a C4 olefin fraction obtained by polymerization, A fraction useful as a gasoline base material is recovered by one-stage distillation.

JP 54-133502 A Japanese Patent Laid-Open No. 56-40618 JP-A-57-96087

  However, in the above-described one-stage distillation means, since only one type of gasoline base material can be obtained from the C4 olefin fraction, there are limitations on the type of gasoline base material obtained, and the C4 olefin fraction can be reduced. It could not be used effectively.

  In addition, the gasoline base material can be used alone or mixed with other base materials to produce a quality-adjusted gasoline product. When recovering materials, RON (octane number by research method) is high (for example, about 99) and only one kind of base material with high sulfur content is recovered. Depending on the properties of the regular gasoline, it may be impossible to mix the whole amount of the obtained base material as a base material of regular gasoline.

  Therefore, an object of the present invention is to obtain a gasoline base material by effectively using a C4 olefin fraction, and to maintain an appropriate property and to mix with other gasoline base materials without any problem. It is providing the manufacturing method of a gasoline base material.

  In order to achieve the above-described object, the method for producing a gasoline base material according to the first aspect of the present invention includes a fractionation step of fractionating an unreacted component from a polymerization reaction product solution of a butane-butene mixed fraction, and the unreacted product. A first distillation step of collecting a fraction having a boiling point of 100 ° C. or higher and 160 ° C. or lower as a fraction (I) from a fraction obtained by fractional removal of the component, and a boiling point of 160 for recovering the fraction (I). A second distillation step of recovering a fraction having a boiling point exceeding 160 ° C. and not more than 200 ° C. as a fraction (II) from the fraction exceeding Hydrogenation in which the other part of the fraction whose boiling point exceeds 160 ° C. and below 200 ° C. and the mixed fraction of the fraction whose boiling point exceeds 200 ° C. are hydrotreated, and the olefin content in the mixed fraction is converted to paraffin. Treatment step and mixed distillate converted to paraffin by the hydrotreatment step The fraction (I), the fraction (II) and the fraction obtained by the third distillation step in which a fraction having a boiling point exceeding 160 ° C. and not more than 200 ° C. is recovered as a fraction (III). (III) is a gasoline base material.

In the method for producing a gasoline base material according to the first aspect of the present invention, as a fraction to be mixed, a fraction having a boiling point of 100 ° C. or higher and 160 ° C. or lower is a fraction (I), and a boiling point exceeds 160 ° C. and is 200 ° C. or lower. A fraction of this fraction is designated as fraction (II), and the fraction having the boiling point from which fraction (II) is recovered exceeds 160 ° C. and other fractions having a boiling point of more than 200 ° C. The olefin is converted to paraffin by hydrotreating the mixed fraction of water, and the fraction having a boiling point exceeding 160 ° C. and lower than 200 ° C. is recovered as a fraction (III) from the paraffin-converted mixed fraction. These fractions (I), fractions (II) and fractions (III) are used as gasoline base materials, respectively.
In the first invention of the present invention, since the fraction obtained in each step from the mixed reaction polymerization reaction product liquid through the multistage distillation step is a gasoline base, Therefore, it is possible to obtain various types of gasoline base materials, and efficiently provide gasoline base materials according to the purpose. Moreover, since the gasoline base material is obtained from the C4 olefin fraction by multi-stage distillation, the residue can be reduced as much as possible, and the C4 olefin fraction can be used effectively.

  The method for producing a gasoline base material according to the second aspect of the present invention includes a fractionation step of fractionating unreacted components from a polymerization reaction product liquid of a butane-butene mixed fraction, and a fraction obtained by fractional removal of the unreacted components. From the first distillation step in which a fraction having a boiling point of 100 ° C. or more and 160 ° C. or less is recovered as a fraction (I), and a fraction in which the boiling point from which the fraction (I) is recovered exceeds 160 ° C. A second distillation step of recovering a part of a fraction of more than 160 ° C. and not more than 200 ° C. as a fraction (II), and the boiling point at which the fraction (II) was collected exceeds Hydrotreating the mixed fraction of the fraction having a boiling point of more than 200 ° C. with the other portion of the fraction below ℃, and converting the olefin content in the mixed fraction to paraffin, and the hydrotreatment The boiling point exceeds 160 ° C from the mixed fraction converted to paraffin by the process. The fraction (I), the fraction (II) and the fraction (III) obtained by the third distillation step for recovering a fraction of 200 ° C. or less as the fraction (III) are mixed to form a gasoline base. It is characterized by using a material.

As described above, the gasoline base material is generally used alone or mixed with other base materials to produce gasoline as a product. However, in the case of a gasoline base material with a high RON, Depending on the properties of the other base material to be mixed, there may be a case where the whole amount of the base material cannot be mixed due to the standard of regular gasoline.
On the other hand, the method for producing a gasoline base material of the second invention of the present invention employs a butane-butene mixed fraction as the C4 fraction, as in the first invention, and generates a polymerization reaction of the mixed fraction. Through a multi-stage distillation process from the liquid, a gasoline base material is obtained by mixing the fractions obtained in each process (fraction (I), fraction (II) and fraction (III)). Yes.

  Among these, the fraction (I) and the fraction (II) are fractions showing a high RON, and the fraction (III) is a fraction showing a low RON, but in the second invention of the present invention. Has a moderate value (89 to 96) of RON of the entire gasoline base material by mixing the fraction (III) with a relatively low RON into the fraction (I) and the fraction (II) with a high RON. In addition to being able to be used alone as regular gasoline as a product, it can be mixed with other gasoline bases without problems.

In the method for producing a gasoline base material of the second invention of the present invention, the content of the fraction (III) is preferably 10 to 40% by mass relative to the whole base material.
According to the present invention, the gasoline base material is constituted, and the content of the fraction (III) having a relatively low RON is 10 to 40% by mass with respect to the whole base material. It is possible to reliably and efficiently obtain a gasoline base material that has no RON.

In the method for producing a gasoline base material of the second invention of the present invention, as the fraction (II), more than 60% and more than 60% of a fraction having a boiling point exceeding 160 ° C. and not exceeding 200 ° C. is recovered. Is preferred.
According to the present invention, the fraction (II) obtained by recovering more than 0% and more than 60% of the fraction having a boiling point exceeding 160 ° C. and not exceeding 200 ° C. obtained in the second distillation step is obtained. Therefore, the RON of the gasoline base material can be kept relatively low, and the above-described effects can be reliably achieved.

An embodiment of the method for producing a gasoline base material according to the present invention will be described with reference to FIG. FIG. 1 is a schematic view showing an embodiment of a flow of a method for producing a gasoline base material according to the present invention.
As shown in FIG. 1, in the method for producing a gasoline base material of the present invention, an unreacted component is fractionated from a polymerization reaction product obtained by polymerizing a butane-butene mixed fraction, and the unreacted component is separated. A first distillation step in which a fraction having a boiling point of 100 ° C. or higher and 160 ° C. or lower is recovered as a fraction (I) from a fraction that has been removed by distillation; A second distillation step in which a fraction having a boiling point exceeding 160 ° C. and not more than 200 ° C. is recovered as a fraction (II), and the boiling point at which the fraction (II) is recovered is 160 ° C. A hydrotreating step of hydrotreating the other fraction of the fraction exceeding 200 ° C. and the fraction having a boiling point exceeding 200 ° C. to convert the olefin in the mixed fraction into paraffin; From the mixed fraction converted into paraffin by the process, the boiling point exceeds 160 ° C. and 20 Fraction (I), fraction (II), and fraction (III) obtained by the third distillation step for recovering a fraction of 0 ° C. or less as fraction (III) To do.

[Raw oil]
In the method for producing a gasoline base material of the present invention, a polymerization reaction product liquid of a butane-butene fraction obtained mainly by petroleum cracking or the like is used as a raw material. As this butane-butene fraction, for example, a mixture comprising a mixed fraction containing 10 to 60% of a butane component, 30 to 40% of an n-butene component, and 10 to 50% of an isobutene component can be used. Diene component may be included.

On the other hand, it is preferable to previously remove diene components such as butadiene contained in the butane-butene fraction by a hydrogenation removal treatment.
The hydrogenation removal treatment for removing the diene is usually performed using palladium / alumina as a catalyst, the treatment conditions are 30 ° C. to 150 ° C., the pressure is 0.1 to 1 MPa, and the SV (Space Velocity) is 0.1. -10 hr ^-1 may be carried out in a known fixed bed reactor or the like. The treatment conditions are particularly preferably a reaction temperature of 50 to 100 ° C., a pressure of 0.3 to 0.5 MPa, and an SV of 1 to 5 hr−1.

[Polymerization reaction]
In order to obtain a polymerization reaction product liquid of the butane-butene fraction, it is necessary to polymerize the fraction. The polymerization reaction may be carried out using silica alumina, zeolite, aluminum chloride or the like as a catalyst, with polymerization temperature of 20 to 180 ° C., pressure of 1 to 10 MPa, and SV of 0.01 to 50 hr ^−1. . The treatment conditions are particularly preferably 50 to 150 ° C. for the reaction temperature, 2 to 6 MPa for the reaction pressure, and 0.1 to 10 hr ⁻¹ for the SV.

[Distillation (1) (fractional distillation)]
First, unreacted components (mainly butane and butene) are fractionated and removed from the polymerization reaction product liquid of the butane-butene fraction (distillation step).
The fractionation step uses a fractionation tower (distillation tower), for example, under the operating conditions in which the top pressure is 0.3 to 0.5 MPa and the bottom temperature is 200 to 250 ° C., the unreacted C4 component is removed. What is necessary is just to remove by distillation. The fractional distillation may be single-column distillation or double-column distillation without any problem.

[Distillation (2) (first distillation step)]
The polymerization reaction product liquid from which the unreacted C4 component has been removed by fractional distillation is sent to a first distillation column (not shown), and a distillation mainly composed of a dimer of C4 component having a boiling point of 100 ° C. or higher and 160 ° C. or lower. The fraction may be recovered from the top of the first distillation column (first distillation step). The first distillation step may be performed by using a known distillation column, for example, operating conditions with a column top pressure of 60 to 80 kPa and a column bottom temperature of 170 to 210 ° C.
The component recovered in this manner is designated as fraction (I). This fraction (I) becomes a gasoline base having a RON (octane number by research method) of about 95-100.

[Distillation (3) (second distillation step)]
The bottom fraction of the first distillation column from which the fraction (I) has been recovered in this way is sent to a second distillation column (not shown). In this second distillation column, a fraction mainly composed of C4 trimer having a boiling point of more than 160 ° C. and not more than 200 ° C. is partially recovered from the top of the second distillation column (the second distillation column). Distillation step). A 2nd distillation process should just be made into the operating conditions which used the well-known distillation tower, for example, made tower top pressure 20-40kPa and tower bottom temperature 180-210 degreeC.
The fraction collected in this way is designated as fraction (II). This fraction (II) is a gasoline base material having a RON of about 95-100.

  Here, the fraction (II) is 0% of the top fraction of the second distillation column (fraction having a boiling point of more than 160 ° C. and not more than 200 ° C., mainly consisting of C4 trimer). It is preferable to recover 60% or less, more preferably 20 to 40%, and particularly preferably 20 to 30%. By collecting more than 0% of the top fraction and not more than 60% as fraction (II), it is possible to obtain suitable properties when mixing with other gasoline bases to produce gasoline.

[Hydrogenation]
The fraction (II) recovered and removed, the residue having a boiling point exceeding 160 ° C. and not more than 200 ° C. (unrecovered fraction at the top of the second distillation column), and the boiling point exceeding 200 ° C. The mixed fraction of the fraction (the bottom fraction of the second distillation column) is hydrotreated by a hydrotreating tower (not shown), and the olefin content in the fraction is converted into a paraffin (hydrotreating step). ). As conditions for the hydrotreatment, a nickel-based catalyst, a palladium-based catalyst or the like is used as a catalyst, the reaction temperature is 150 to 200 ° C., the pressure is 2 to 3 MPa, and the SV is about 0.01 to 50 hr ^−1. .

  When a nickel-based catalyst is used as the catalyst, the sulfur content in the recovered mixed fraction is adsorbed and removed by the nickel catalyst, and in the palladium-based catalyst, the sulfur in the recovered mixed fraction is Converted to hydrogen sulfide. And this hydrogen sulfide is isolate | separated in the following distillation (3rd distillation process). As described above, the sulfur concentration in the fraction is lowered by the catalyst used in the hydrotreating step.

[Distillation (4) (Third distillation step)]
The paraffinized mixed fraction obtained by the hydrotreating step is sent to a third distillation tower (not shown). In the third distillation column, a fraction mainly composed of C4 trimer having a boiling point of more than 160 ° C. and not more than 200 ° C. is recovered from the top of the third distillation column (third distillation step). ). A 3rd distillation process should just be made into the operating conditions which used the well-known distillation tower, for example, the tower top pressure was 20-40 kPa, and the tower bottom temperature was 180-210 degreeC.
The fraction collected in this manner is designated as fraction (III). This fraction (III) has a RON of about 80 to 85, and is lower than the RON of the fraction (I) and the fraction (II) described above.
Of the fractions collected from the top of the third distillation column, the remaining fraction not used as fraction (III) and the bottom fraction of the third distillation tower having a boiling point exceeding 200 ° C. May be removed separately.

[mixture]
In the method for producing a gasoline base material of the present invention, the fraction (I), the fractions (II) and (III) obtained in each of the above steps are mixed to obtain a gasoline base material.
Here, as described above, the RON of the fraction (I) and the fraction (II) among these three fractions is relatively high (the fraction (I) is about 95 to 100, the fraction (II) On the other hand, the fraction (III) is as low as about 80 to 85.

  And in this invention, since it will exceed a regular gasoline specification only by making it the mixed fraction of a fraction (I) and a fraction (II), a part of fraction (II) is hydrotreated. Then, as a fraction having a relatively low RON (fraction (III)), this fraction (III) is blended into the fraction (I) and the fraction (II), so that RON is a standard for regular gasoline. It is intended to obtain a gasoline base material that enters.

  The blending ratio of the fraction (III) is appropriately determined depending on the required RON of the gasoline base material, but is preferably 10 to 40% by weight based on the whole gasoline base material, and 15 to 35% by weight. It is particularly preferable that By setting the blending ratio of the fraction (III) to 10 to 40% by mass with respect to the entire base material, the RON of the entire gasoline base material becomes an appropriate value (85 to 95), and is used alone as gasoline as a product. In addition, it can be mixed with other gasoline base materials without any problem.

  The blending ratio of the fraction (I) and the fraction (II) is not particularly limited, but the fraction (I) / fraction (II) may be about 2/1 to 3/1.

  According to the method for producing a gasoline base material of the present invention carried out in this way, a butane-butene mixed fraction is adopted as the C4 fraction, and a multistage distillation process is performed from the polymerization reaction product liquid of the mixed fraction. Then, as a fraction obtained in each step, a fraction (III) having a relatively low RON is mixed with a fraction (I) and a fraction (II) having a high RON, so that RON becomes an appropriate value (85 to 95), and can be used alone as gasoline as a product, and can be mixed with other gasoline base materials without any problem.

  The aspect described above shows one aspect of the present invention, and the present invention is not limited to the above-described embodiment, and is within the scope of achieving the object and effect of the present invention. Needless to say, modifications and improvements are included in the content of the present invention. Further, the specific structure, shape, and the like in carrying out the present invention are not problematic as other structures, shapes, and the like as long as the objects and effects of the present invention can be achieved.

For example, in the embodiment described above, a gasoline base material is obtained by mixing the fraction (I), the fraction (II), and the fraction (III) obtained by the multistage distillation step shown in FIG. However, in the present invention, each of fraction (I), fraction (II) or fraction (III) may be used alone as a gasoline base material.
In this way, it is possible to obtain various types of gasoline base materials from the C4 olefin fraction, and it is possible to efficiently provide a gasoline base material according to the purpose and to suppress the residue as much as possible. The olefin fraction can be used effectively.

Moreover, in the above-mentioned aspect, although the processing conditions in processes, such as superposition | polymerization, distillation, and hydroprocessing, were shown concretely, it is not limited to this, If the desired fraction etc. can be obtained, the conditions There is no problem as optional.
In addition, the specific structure, shape, and the like in the implementation of the present invention may be other structures as long as the object of the present invention can be achieved.

  EXAMPLES Hereinafter, although an Example and a reference example are given and this invention is demonstrated more concretely, this invention is not limited to the content of an Example etc. at all.

[Example 1]
A gasoline base material was produced according to the schematic diagram shown in FIG. 1 and specifically according to the following contents.

(1) Preparation of butane-butene polymerization reaction product liquid:
C4 fraction obtained by distilling a fraction with a lighter carbon number than 3 and a fraction with a heavier carbon number than 5 among light components obtained by cracking vacuum gas oil with a fluid catalytic cracking unit (FCC unit) Was used as a raw material oil. The amount of feedstock used was 130 t / h, and the composition was 53% butane, 37% n-butene, and 10% isobutene. The sulfur concentration was 10 ppm.
This C4 fraction was supplied to a fixed bed reactor, a silica alumina catalyst (N633HN: manufactured by JGC Chemical Co., Ltd.) was used as a catalyst, the reaction temperature was 50 to 150 ° C., the pressure was 5 MPa, and the SV was 0.3 hr ^−1. As a result, a butane-butene polymerization reaction product liquid containing C4 dimer and trimer was obtained.

(2) Removal of unreacted C4 component:
The polymerization reaction product liquid obtained in (1) is supplied to the fractionation column, and the column top pressure is 0.35 to 0.45 MPa, the column bottom temperature is 230 to 240 ° C., and unreacted from the column top. Ingredients (butane, butene) were recovered. On the other hand, the bottom fraction (polymerized product) was supplied to the first distillation column.

(3) First distillation step:
In the first distillation step, the top column pressure of the first distillation column is 65 to 75 KPa and the column bottom temperature is 180 to 200 ° C., and a dimer of mainly C4 having a boiling point of 100 to 160 ° C. from the column top. Was recovered (fraction (I)). On the other hand, the bottom fraction was supplied to the next second distillation column. The sulfur concentration of the fraction (I) is 4 ppm, the RON is 97, and the recovery rate of the fraction (I) is 38 with respect to 100% by mass of the polymerization reaction product liquid obtained by fractionating unreacted components. It was mass%.

(4) Second distillation step:
In the second distillation step, the top pressure of the second distillation column is 25 to 35 KPa and the bottom temperature is 180 to 200 ° C. From the top of the distillation column, the boiling point is mainly 160 to 200 ° C. A part of the trimer (55% of the total) was recovered (fraction (II). On the other hand, the mixed fraction of the remaining fraction and the bottom fraction was supplied to the hydrotreating tower. ) Was 1 ppm, and RON was 97. The fraction (II) recovery rate was 17% by mass with respect to 100% by mass of the polymerization reaction product obtained by fractionating unreacted C4. there were.

(5) Hydrogenation process:
In the hydrotreating step of hydrotreating the mixed fraction obtained in (4), the hydrotreating tower is used as a fixed bed reactor and 0.5% by mass of palladium (Pd) is used as a catalyst. The reaction temperature is 150 to 250 ° C., the pressure is 2 MPa, the SV is 1.0 hr ⁻¹ , the hydrogen / oil ratio is 200 Nm ³ / m ³ , and the olefin content of the mixed fraction is converted into the total paraffin content. Feeded to the third distillation column. The sulfur concentration of the fraction at the hydrotreating outlet was 0.1 ppm.

(6) Third distillation step:
In the third distillation step, the top pressure of the third distillation column is 25 to 35 KPa, the bottom temperature is 180 to 200 ° C., and mainly C4 trimer having a boiling point of 160 to 200 ° C. from the top. A part was collected (referred to as fraction (III)). The sulfur concentration in the column top fraction was 0.1 ppm or less, and RON was 83. Further, the fraction (III) recovery rate was 13% by mass with respect to 100% by mass of the polymerization reaction product liquid obtained by fractional distillation of unreacted components.

(7) Mixing process:
The fraction (I), fraction (II) and fraction (III) obtained in (1) to (6) were mixed to obtain a gasoline base material. The mixing ratio was fraction (I) / fraction (II) / fraction (III) = 56/24/20. The recovery rate of the gasoline base material was 60 to 75% by mass with respect to 100% by mass of the polymerization reaction product liquid obtained by fractionating unreacted components.

  And the RON of the obtained gasoline base material was 94, and the sulfur concentration was 2.5 ppm. Therefore, the gasoline base material can be used alone as regular gasoline.

[Reference Example 1]
The polymerization reaction product liquid of the butane-butene fraction obtained in Example 1 (1) was introduced into a known distillation column, and the column top pressure was 10 to 20 KPa and the column bottom temperature was 180 to 200 ° C. The gasoline base material was obtained by operating and recovering mainly C4 dimers and trimers having a boiling point of 100 to 120 ° C. from the top of the column.

The recovery rate of the gasoline base material obtained in Reference Example 1 was 60 to 70% by mass with respect to 100% by mass of the polymerization reaction product liquid obtained by fractional distillation of unreacted components. Moreover, RON was 99 and the sulfur concentration was 4 ppm.
On the other hand, since this gasoline base material has a high RON value and exceeds the regular gasoline standard value, it can only be mixed with other gasoline base materials up to 50% by mass with respect to the whole gasoline.

  The present invention can be advantageously used as a method for producing a gasoline base material such as regular gasoline.

It is the schematic which showed the one aspect | mode of the flow of the manufacturing method of the gasoline base material of this invention.

Claims (4)

A fractionation step of fractionating unreacted components from the polymerization reaction product of the butane-butene mixed fraction;
A first distillation step of recovering a fraction having a boiling point of 100 ° C. or higher and 160 ° C. or lower as a fraction (I) from a fraction obtained by fraction-removing the unreacted component;
A second distillation step in which a fraction having a boiling point exceeding 160 ° C. and not higher than 200 ° C. is recovered as a fraction (II) from a fraction having a boiling point exceeding 160 ° C. from which the fraction (I) has been recovered. When,
The other fraction of the fraction (II) from which the fraction (II) has been recovered exceeds 160 ° C. and not more than 200 ° C. and the mixed fraction of the fraction whose boiling point exceeds 200 ° C. are hydrotreated to produce a mixed fraction. A hydrotreating process for converting the olefin content in to paraffin content;
Obtained by a third distillation step in which a fraction having a boiling point exceeding 160 ° C. and not higher than 200 ° C. is recovered as a fraction (III) from the mixed fraction converted into the paraffin component by the hydrotreating step, A method for producing a gasoline base material, wherein the fraction (I), the fraction (II) and the fraction (III) are a gasoline base material. A fractionation step of fractionating unreacted components from the polymerization reaction product of the butane-butene mixed fraction;
A first distillation step of recovering a fraction having a boiling point of 100 ° C. or higher and 160 ° C. or lower as a fraction (I) from a fraction obtained by fraction-removing the unreacted component;
A second distillation step in which a fraction having a boiling point exceeding 160 ° C. and not higher than 200 ° C. is recovered as a fraction (II) from a fraction having a boiling point exceeding 160 ° C. from which the fraction (I) has been recovered. When,
The other fraction of the fraction (II) from which the fraction (II) has been recovered exceeds 160 ° C. and not more than 200 ° C. and the mixed fraction of the fraction whose boiling point exceeds 200 ° C. are hydrotreated to produce a mixed fraction. A hydrotreating process for converting the olefin content in to paraffin content;
Obtained by a third distillation step in which a fraction having a boiling point exceeding 160 ° C. and not higher than 200 ° C. is recovered as a fraction (III) from the mixed fraction converted into the paraffin component by the hydrotreating step, A method for producing a gasoline base material comprising mixing a fraction (I), a fraction (II) and a fraction (III) to form a gasoline base material. In the manufacturing method of the gasoline base material according to claim 2,
The gasoline base material production method, wherein the content of the fraction (III) is 10 to 40% by mass with respect to the whole base material. In the manufacturing method of the gasoline base material of Claim 2 or Claim 3,
A method for producing a gasoline base material, wherein, as the fraction (II), a fraction having a boiling point exceeding 160 ° C and not exceeding 200 ° C is recovered from exceeding 0% to 60% or less.

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