JP6609749B2 - Method for producing light oil composition - Google Patents

Description

The present invention relates to a manufacturing method of the gas oil compositions used in diesel engines or the like.

  Petroleum products generally called white oil such as gasoline, light oil, and kerosene are in greater demand than heavy oil consisting of heavy oil, and this trend has become more prominent due to the conversion of industrial heavy oil to natural gas. It's getting on. As petroleum products are called co-products, heavy oil components are also produced in the process of producing white oil. Therefore, in order to increase production of white oil, the heavy oil content is decomposed into a white oil base (upgrading). Process) is generally performed. However, some white oil bases obtained by decomposing heavy oil do not meet the required standards, and some have problems in practical performance even if they meet the standards. Some are restricted in use. One of them is a cracked light oil fraction obtained from a heavy oil cracking apparatus, and there is a problem in oxidation stability in order to use it as a base material for light oil.

  The oxidation stability of light oil is one of the important properties affecting the use state and practical performance, and many proposals have been made so far for improving the oxidation stability of light oil. And the light oil in which the oxidation stability was improved is also disclosed in which a base material is desulfurized light oil obtained by desulfurizing a cracked light oil fraction.

  For example, Japanese Patent Application Laid-Open No. 2008-144156 discloses a light oil composition whose oxidation stability is improved mainly by controlling the content of a styrene compound or a diene compound within a predetermined range. The thing containing the desulfurized light oil obtained by desulfurizing a light oil fraction as a base material is disclosed.

  Japanese Patent Application Laid-Open No. 2013-203752 discloses a light oil composition whose oxidation stability is improved mainly by controlling the content of benzoanthracenes within a predetermined range, wherein a cracked gas oil fraction is The thing containing the desulfurized light oil obtained by desulfurization as a base material is disclosed.

JP 2008-144156 A JP2013-203752A

However, as described above, the cracked gas oil fraction has a problem in oxidation stability in order to be used as a gas oil base material. On the other hand, in diesel vehicles, the injection pressure into the engine combustion cylinder has been increasing year by year due to the impact of stricter exhaust gas regulations, and the fuel in the fuel injection pumps and injectors has been exposed to high pressure and high temperature. It is desired to provide a light oil composition having excellent stability. Then, an object of this invention is to provide the manufacturing method of the light oil composition which is excellent in oxidation stability using the cracked-type light oil fraction as raw material oil.

The present invention, a total aromatic content from 20.0 to 25.0% by volume, bicyclic aromatic content of from 1.0 to 3.0% by volume, tricyclic or more aromatics of from 0.2 to 1.2 volume %, 13.0 to 18.0 mass % of naphthenobenzenes , and 10 mass ppm or less of sulfur content, a density (15 ° C.) of 0.8200 to 0.8600 g / cm ³ , and an ASTM color of 0 A method for producing a light oil composition of 2 to 2.0 , comprising:
This is a method for producing a gas oil composition in which the following raw material oil containing a cracked gas oil fraction is hydrodesulfurized.
Feedstock: total aromatic content of 25.0 to 35.0 volume%, the total naphthene content from 15.0 to 25.0 wt%, a bicyclic naphthenes 4.0 to 7.0 wt%, tricyclic naphthenes min 1.0 to 2.5 wt%, and a sulfur content viewed contains 0.50 to 1.60 wt%, a 90% distillation temperature of 340.0 ~380.0 ℃.

ADVANTAGE OF THE INVENTION According to this invention, the manufacturing method of the light oil composition which is excellent in oxidation stability using the cracked-type light oil fraction as raw material oil can be provided.

It is a conceptual diagram which shows the correlation of the outlet temperature of a desulfurization apparatus, and the polycyclic aromatic and sulfur content of desulfurization light oil.

The raw oil used in the present invention has a total aromatic content of 25. 0 to 35.0% by volume der is, more preferably 25.0 to 30.0% by volume. If the aromatic content is small, the exothermic reaction may not be sufficient and the oxidation stability after desulfurization may be insufficient, and if it is too large, the cetane index after desulfurization may be low, causing problems such as poor ignition at low temperatures. is there. As for the aromatic component, for example, the monocyclic aromatic component is 16.0 to 22.0% by volume, the bicyclic aromatic component is 5.0 to 10.0% by volume, the tricyclic or higher aromatic component is 1 0.0 to 4.0% by volume.

All naphthene content of the feedstock is 1 5.0 to 25.0 wt%, more preferably 17.0 to 25.0 wt%, more preferably from 21.0 to 25.0 wt%. One part naphthene content is 10.0-17.0 mass%, for example. Bicyclic naphthene content is 4.0-7.0 mass % , Preferably it is 5.0-7.0 mass%. Tricyclic naphthene content is from 1.0 to 2.5 wt%, preferably from 1.5 to 2.5 wt%. If the naphthene content is low, the oxidation stability of the light oil after desulfurization will be poor, and if it is too high, the cetane index after desulfurization will be low, which may cause poor ignition at low temperatures.

The sulfur content of the feedstock is 0 . 50 to 1.60% by mass is, more preferably 0.80 to 1.50 wt%, more preferably from 1.00 to 1.50 wt%. The higher the sulfur content, the easier the exothermic reaction will occur and the easier it will be to obtain light oil with the desired oxidation stability. Concerned.

The 10% distillation temperature of the raw material oil is, for example, 210.0 to 270.0 ° C, and the 50% distillation temperature is, for example, 280.0 to 310.0 ° C. 90% distillation temperature is 3 from 40.0 to 380.0 ° C., more preferably 340.0-370.0 ° C., further preferably from 350.0 to 370.0 ° C.. The higher the 90% distillation temperature, the higher the reaction temperature in order to achieve the desired sulfur content of 10 mass ppm, and it is easy to obtain light oil with good oxidation stability. As a result, it becomes difficult to obtain a desired pour point or clogging point value.

The density (15 degreeC) of raw material oil can be 0.8400-0.8600g / cm < ³ >, for example. For example, the kinematic viscosity is 4.0 to 6.0 mm ² / s, the pour point is + 2.5 ° C. or less, and the clogging point is + 5 ° C. or less.

  The feedstock oil used in the present invention can be prepared by mixing a cracked gas oil fraction and another gas oil base material (hereinafter referred to as a feedstock base material).

  As the cracking gas oil fraction, direct degassing oil obtained from a direct desulfurization unit (hereinafter referred to as RGO), degassing oil obtained from an indirect desulfurization unit, light cycle oil obtained from a fluid catalytic cracking unit (hereinafter referred to as LCO), And a diesel oil fraction distilled from a heavy oil upgrading process such as a pyrolysis diesel oil obtained from a pyrolysis apparatus. As the cracked light oil fraction, RGO is preferable from the viewpoint of oxidation stability of the light oil after desulfurization.

  RGO has a total aromatic content of preferably 25.0% by volume or more, more preferably 25.0 to 40.0% by volume, and further preferably 30.0 to 40.0% by volume. If the total aromatic content is small, an exothermic reaction is difficult to occur and the oxidation stability of the light oil after desulfurization may be deteriorated. If it is large, the cetane index of the light oil after desulfurization will be low, causing problems such as poor ignition. There is. For example, the aromatic content is 20.0 to 35.0% by volume, the bicyclic aromatic content is 2.5 to 4.5% by volume, and the tricyclic or higher aromatic content is 1.0 to 2.0% by volume. be able to. The total naphthene content is preferably 15.0 mass% or more, the bicyclic naphthene content is 4.0 mass% or more, and the tricyclic naphthene content is preferably 1.0 mass% or more. One part naphthene content can be made into 14.0-20.0 mass%, for example. If the naphthene content is small, the oxidation stability may be deteriorated. If the naphthene content is large, the cetane index will be low, and problems such as poor ignition may occur. The sulfur content is preferably 0.01% by mass or more.

For example, RGO can have a 10% distillation temperature of 210.0-240.0 ° C and a 50% distillation temperature of 280.0-320.0 ° C. The 90% distillation temperature is preferably 380 ° C. or lower, and more preferably 370 ° C. or lower. If the 90% distillation temperature is too high, the amount of wax increases, and filter clogging may occur at low temperatures. The density (15 ° C.) is preferably 0.8700 g / cm ³ or less. If the density is too high, particulate matter in the exhaust gas may be increased. For example, the kinematic viscosity is 3.0 to 7.0 mm ² / s, the pour point is 2.5 ° C. or less, and the clogging point is + 5 ° C. or less.

  LCO has a total aromatic content of preferably 60.0% by volume or more, more preferably 65 to 80% by volume, and still more preferably 70 to 80% by volume. When the total aromatic content is small, the exothermic reaction is small, and the oxidation stability after desulfurization may be deteriorated. When the total aromatic content is large, the cetane index after desulfurization is low, and ignition failure may occur. For example, the aromatic content is 15.0 to 30.0% by volume, the bicyclic aromatic content is 20.0 to 40.0% by volume, and the tricyclic or higher aromatic content is 5.0 to 20.0% by volume. be able to. The total naphthene content is preferably 15.0 mass% or more, the bicyclic naphthene content is 3.0 mass% or more, and the tricyclic naphthene content is preferably 1.0 mass% or more. One part naphthene content can be made into 12.0-17.0 mass%, for example. If the naphthene content is small, the oxidative stability after desulfurization may be insufficient, and if it is large, the cetane index may be low, causing problems such as poor ignition. The sulfur content is preferably 0.07% by mass or more.

For example, LCO can have a 10% distillation temperature of 210.0 to 230.0 ° C and a 50% distillation temperature of 250.0 to 280.0 ° C. The 90% distillation temperature is preferably 370.0 ° C or lower. If the 90% distillation temperature is too high, the amount of wax increases, and problems such as filter clogging may occur in winter. The density (15 ° C.) is preferably 0.9800 g / cm ³ or less, and more preferably 0.9200 to 0.9500 g / cm ³ . If the density is too low, the oxidation stability after desulfurization may be low, and if it is too high, the cetane index may be low, resulting in poor ignition. For example, the kinematic viscosity may be 2.0 to 4.0 mm ² / s, the pour point may be −15 to −35 ° C., and the clogging point may be −5 to −20 ° C.

  In the raw material oil, the cracked light oil fraction is preferably 1 to 35% by volume, more preferably 5 to 30% by volume. If the cracked gas oil fraction is too much, the cetane index of the product may be lowered, and if it is too little, the reaction tower outlet temperature is lowered, and a light oil composition having the desired oxidation stability may not be obtained. When the cracked gas oil fraction is RGO, it is preferably 5 to 30% by volume in the feedstock, more preferably 15 to 30% by volume, and further preferably 25 to 30% by volume. If there is too much RGO, the cetane index of the product may be low, and if it is too little, a light oil composition having the desired oxidation stability may not be obtained. When the cracked light oil fraction is LCO, it is preferably 1 to 10% by volume in the raw material oil, and more preferably 5 to 10% by volume. If the LCO is too much, the cetane index of the product may be lowered, and if it is too little, the reaction tower outlet temperature may be lowered, and a light oil composition having the desired oxidation stability may not be obtained.

  Examples of the raw material oil base include a light oil fraction obtained from an atmospheric distillation apparatus (hereinafter referred to as straight-run light oil).

In the present invention, the gas oil composition is obtained by hydrodesulfurizing the above-mentioned raw material oil. The light oil composition obtained has a total aromatic content of 20.0 to 25.0 vol %, preferably 21.0 to 25.0 vol%. For example, the aromatic content is 18.0 to 22.0% by volume. The bicyclic aromatic content is 1.0 to 3.0 % by volume , preferably 2.0 to 3.0% by volume. The tricyclic or higher aromatic content is 0.2 to 1.2 % by volume , preferably 0.5 to 1.2% by volume. If the aromatic content is small, the sealing material of the fuel injection system may be contracted to cause fuel bleeding. If the aromatic content is large, black smoke in the exhaust gas may increase.

The obtained light oil composition contains 13.0 to 18.0 mass % of naphthenobenzenes , preferably 13.0 to 16.5 mass%, more preferably 13.0 to 15.0 mass%. If the amount of naphthenobenzenes is small, the fuel supply system sealant may contract and cause fuel bleeding. If the amount of naphthenobenzenes is large, the oxidation stability may deteriorate. The naphthenobenzenes are preferably 15.0% by mass or less, more preferably 9.0 to 13.0% by mass, still more preferably 9.0 to 12.0% by mass, and particularly preferably 9.0 to 11%. 0.0% by mass. If the amount of naphthenobenzenes is too small, the fuel supply system sealant may shrink and cause fuel bleeding, and if it is too high, oxidation stability may deteriorate. The bicyclic naphthenobenzenes are preferably 5.0% by mass or less, more preferably 1.0 to 4.0% by mass, and still more preferably 1.0 to 3.0% by mass. An excessive amount of bicyclic naphthenobenzenes is not preferred because the oxidation stability tends to deteriorate. The sulfur content is 10 mass ppm or less.

  In the present invention, the one-part naphthenobenzenes include naphthenobenzene and those having an alkyl group, and examples thereof include indane and tetralin. Bicyclic naphthenobenzenes include bicyclic naphthenobenzene and those having an alkyl group, and examples thereof include octahydroanthracene and alkyloctahydroanthracene. Naphthenobenzenes include naphthenobenzenes, bicyclic naphthenobenzenes, and polycyclic naphthenobenzenes.

The ASTM color is 0.2 to 2.0 , preferably 0.5 to 2.0 , and more preferably 1.0 to 2.0 . If the ASTM color is too small, the oxidation stability is deteriorated, and if it is too large, black smoke in the exhaust gas increases, which is not preferable. The density (15 ° C.) is 0 . 8200 to 0.8600 g / cm ³ . For example, the 10% distillation temperature may be 220.0 to 250.0 ° C, the 50% distillation temperature may be 270.0 to 300.0 ° C, and the 90% distillation temperature may be 330.0 to 360.0 ° C. . The kinematic viscosity is 2.5 to 5.5 mm ² / s, the pour point is 2.5 ° C. or less, the clogging point is + 1 ° C. or less, and the cetane index is preferably 45 to 60, more preferably 50 to 60, and even more preferably. Is 55-58. If the cetane index is too large, unburned hydrocarbons in the exhaust gas may increase, and if it is too small, start-up failure may occur.

  The light oil composition according to the present invention is excellent in oxidation stability. The oxidation stability can be expressed by, for example, the induction period by the PetroOXY method. In the light oil composition according to the present invention, it is preferably 70 minutes or more, more preferably 90 minutes or more, still more preferably 125 minutes or more, particularly preferably Is over 140 minutes.

  By performing hydrodesulfurization using the above-mentioned raw material oil, the above light oil composition having excellent oxidation stability can be obtained. By appropriately controlling the reaction temperature of the desulfurizer reactor and the sulfur content and aromatic content of the raw material oil, a light oil composition particularly excellent in oxidation stability can be obtained. The hydrodesulfurization is performed under conditions such that the light oil composition as described above is obtained. For example, hydrodesulfurization can be performed as follows.

  For hydrodesulfurization, a desulfurization apparatus using a known catalyst such as a cobalt molybdenum system or a nickel molybdenum system can be used. The desulfurization treatment conditions may be adjusted as appropriate so that the sulfur content of the obtained desulfurized light oil is 10 massppm or less, but the apparatus outlet temperature is set to a region where the dehydrogenation reaction of polycyclic naphthene is dominant.

  In the reactor of the desulfurization apparatus, a dearomatic reaction occurs simultaneously with the desulfurization reaction, and polycyclic aromatics having two or more rings also decrease as the desulfurization reaction proceeds. However, since the desulfurization reaction and the dearomatic reaction are exothermic reactions, the outlet temperature of the desulfurization reaction tower is higher than the inlet temperature. Therefore, when the dehydrogenation reaction of naphthene becomes dominant at a certain temperature, the polycyclic aromatic content tends to increase as the temperature rises.

  That is, when the apparatus outlet temperature is equal to or lower than a predetermined value (temperature T0 in FIG. 1) (region on the left side of temperature T0 in FIG. 1), the polycyclic aromatic dehydrogenation reaction dominates in the apparatus. It becomes the target. Therefore, the reaction proceeds with increasing temperature, and the polycyclic aromatic content decreases. On the other hand, when the outlet temperature of the apparatus is higher than the predetermined value T0, the dehydration reaction of two or more polycyclic naphthenes is dominant in the apparatus, and the reaction proceeds as the temperature rises, and the desulfurized gas oil contains polycyclic aromatics. The amount increases.

  In addition, the graph which shows content of the polycyclic aromatic of FIG. 1 and sulfur content makes an understanding easy, and is not exact.

  By adjusting the device outlet temperature so that the dehydrogenation reaction of polycyclic naphthene is dominant in the device, and by adjusting the amount of naphthenes in the feedstock, the polycyclic aroma of desulfurized gas oil It is possible to improve the oxidation stability by increasing the group content and decreasing the amount of naphthenobenzene. When the raw material oil to be hydrodesulfurized has the predetermined property, oxidation stability can be particularly improved.

Depending on the type of catalyst used in the apparatus, the apparatus outlet temperature is adjusted appropriately for the liquid space velocity, the reaction tower outlet hydrogen partial pressure, and the hydrogen oil ratio to obtain an appropriate reaction tower outlet temperature. Can be in range. For example, a commercially available CoMo-based or NiMo-based desulfurization catalyst is used as the catalyst, the liquid space velocity is 0.4 to 1.5 h ⁻¹ , the reaction tower outlet hydrogen partial pressure is 3.5 to 6.2 MPa, and the hydrogen oil ratio is 100 to 300 NL / L.

  The region (temperature) where the dehydrogenation reaction of polycyclic naphthene is dominant can be determined, for example, as follows. When the reaction temperature is raised to lower the sulfur content, the polycyclic aromatic content of two or more rings also decreases, but there is a temperature at which the polycyclic aromatic content increases at a certain point. The temperature at which the polycyclic aromatic content becomes the lower limit (T0) varies depending on the general desulfurization equipment and operating conditions such as hydrogen partial pressure, catalyst activity, and hydrogen oil ratio, and the properties of the feedstock oil. It can be determined by measuring the aromaticity of the composition (for example, JPI method) and measuring the polycyclic aromatic content and the reaction tower outlet temperature. The region (temperature) in which the dehydrogenation reaction of polycyclic naphthene is dominant is preferably selected from the range of T0 ° C. to T0 + 40 ° C., and more preferably selected from the range of T0 ° C. to T0 + 20 ° C. Within this range, an arbitrary range, that is, an upper limit and a lower limit can be determined to set a region (temperature) in which the dehydrogenation reaction of polycyclic naphthene becomes dominant. If the dominant region (temperature) is too low, it is difficult to obtain the desired oxidation stability, and if it is too high, the polycyclic aromatics increase and the exhaust gas properties may deteriorate.

  In the present invention, the light oil composition may be a product light oil or a base material constituting the product light oil. Therefore, the light oil composition according to the present invention can be used as a product as it is or as a base material.

  When the light oil composition according to the present invention is used as it is as a product, when it is used as a base material, an additive may be mixed in any case. When using as a base material, it can mix with 1 type, 2 or more types of kerosene base materials, or 1 type, or 2 or more types of light oil base materials, for example.

  As the kerosene base material, for example, a kerosene fraction obtained by atmospheric distillation of crude oil and a desulfurized kerosene obtained by desulfurization thereof can be used. A kerosene base material having a sulfur content of 10 mass ppm or less obtained by mixing and desulfurizing a kerosene fraction obtained from an atmospheric distillation apparatus and cracked kerosene at an appropriate ratio can also be used. Note that cracked kerosene refers to kerosene fractions distilled from heavy oil upgrading processes such as kerosene fractions obtained from fluid catalytic cracking equipment and kerosene fractions obtained from thermal cracking equipment. Therefore, it is preferable to make the mixing ratio as high as possible.

  Moreover, as a light oil base material, the GTL light oil etc. with which the paraffin compound was manufactured using the Fischer-Tropsch reaction from carbon monoxide and water are mentioned, for example.

  Examples of the additive include an antioxidant, a lubricity improver, and a low temperature fluidity improver. A commercial item is mentioned as antioxidant. Examples of the lubricity improver include commercially available products such as acid-based acids based on fatty acids and esters based on glycerin monofatty acid esters. These compounds can be used alone or in combination of two or more. The fatty acid used in the lubricity improver is mainly composed of an unsaturated fatty acid having about 12 to 22 carbon atoms, preferably about 18 carbon atoms, that is, a mixture of oleic acid, linoleic acid, linolenic acid and the like. preferable. Examples of the low temperature fluidity improver include commercially available products such as ethylene-vinyl acetate copolymer, ethylene-alkyl acrylate copolymer, alkenyl succinic acid amide, chlorinated polyethylene, and polyalkyl acrylate.

≪Preparation of raw oil≫
RGO and LCO were used as cracking gas oil fractions, and light oil fraction 1 (LGO1) and light oil fraction 2 (LGO2) having different properties such as crude oil type and sulfur content were used as the raw material oil base to be mixed therewith. These properties are shown in Table 1. RGO, LCO, LGO1 and LGO2 were mixed at a volume ratio shown in Table 2 to obtain feedstocks 1-4. Table 2 shows the properties of the feedstocks 1-4. All the properties and the like were determined as follows.

composition:
(Aromatic content)
1 ring aromatic content, 2 ring aromatic content and 3 or more ring aromatic hydrocarbon content measured by JPI-5S-49-97 "Petroleum products-Hydrocarbon type test method-High performance liquid chromatograph method". The sum of these was taken as the total aromatic content.

(Naphthene, naphthenobenzenes)
The ionic strength (%) was obtained by performing FI-MS measurement using a JMS-T100GC time-of-flight mass spectrometer manufactured by JEOL to which an HP-6890N gas chromatogram manufactured by Agilent Technologies was connected, and using the normal paraffin standard sample. ) And the concentration (mass%) correction graph, and then the respective strength ratios (%) were determined with the overall strength as 100 mass%. The analysis conditions are as follows.
GC column: FS, Deactivated (0.250mm × 5m, Agilent technologies)
Column temperature condition: 300 ° C (7 minutes)
Sample vaporization chamber conditions: 300 ° C constant MS detector: 300 ° C

Sulfur content:
Measured according to JIS K 2541-4 “Crude oil and petroleum products—Sulfur content test method Part 4: Radiation excitation method”.
Density (@ 15 ° C):
Measured according to JIS K 2249 “Crude oil and petroleum products—density test method and density / mass / volume conversion table”.
Distillation properties:
Measured according to JIS K 2254 "Petroleum products-Distillation test method".

Kinematic viscosity (@ 30 ° C):
Measured according to JIS K 2283 “Crude oil and petroleum products—Kinematic viscosity test method and viscosity index calculation method”.
Pour point:
Measured according to JIS K 2269 “Pour point of crude oil and petroleum products and cloud point test method of petroleum products”.
Clogging point:
Measured according to JIS K 2288 “Petroleum products—light oil—clogging point test method”.
ASTM color:
It was measured by the stimulus value conversion method of JIS K 2580 “Petroleum products—color test method”. Using a color / turbidity simultaneous measuring device COH400 (manufactured by Nippon Denshoku Co., Ltd.), measurement was performed up to one decimal place.

Cetane index:
Measured according to JIS K 2280-5 “Petroleum products—Octane number and cetane number and determination of cetane index—Part 5: Cetane index”.
Induction period by the PetroOXY method (induction period):
As an oxidation stability index, using an oxidation stability test apparatus PetroOXY (manufactured by Petrotest), the initial oxygen pressure was set to 700 kPa, and the elapsed time until the pressure decreased by 10% from the maximum pressure was measured. In this test, the test temperature was 140 ° C. in order to evaluate oxidation stability at high temperatures.

Example 1
The raw material oil 1 was prepared using a commercially available desulfurization catalyst, the liquid space velocity was 1.0 h ⁻¹ , the hydrogen partial pressure was 5.6 MPa, and the hydrogen oil ratio was 150 NL / L. In a dominant region (temperature), desulfurization treatment was performed until the sulfur content became 10 massppm or less, and the light oil composition according to Example 1 was obtained. Table 3 shows properties and the like of the obtained light oil composition.

(Examples 2-3)
The light oil composition which concerns on Examples 2-3 was obtained like Example 1 except having used raw material oil 2 or 3 instead of the raw material oil 1. FIG. Table 3 shows properties and the like of the obtained light oil composition.

(Comparative Example 1)
A light oil composition according to Comparative Example 1 was obtained in the same manner as in Example 1 except that the raw material oil 4 was used instead of the raw material oil 1. Table 3 shows properties and the like of the obtained light oil composition.

Claims (3)

The total aromatic content from 20.0 to 25.0% by volume, bicyclic aromatic content from 1.0 to 3.0 volume%, the aromatic content or tricyclic 0.2 to 1.2 volume%, naphtheno 13.0 to 18.0 % by mass of benzenes and 10 mass ppm or less of sulfur content, density (15 ° C.) is 0.8200 to 0.8600 g / cm ³ , and ASTM color is 0.2 to 2 A process for producing a light oil composition that is 0.0 ,
A process for producing a gas oil composition, comprising hydrodesulfurizing the following feedstock containing a cracked gas oil fraction.
Feedstock: total aromatic content of 25.0 to 35.0 volume%, the total naphthene content from 15.0 to 25.0 wt%, a bicyclic naphthenes 4.0 to 7.0 wt%, tricyclic naphthenes min 1.0 to 2.5 wt%, and a sulfur content viewed contains 0.50 to 1.60 wt%, a 90% distillation temperature of 340.0 ~380.0 ℃. Wherein a degradation system gas oil fraction is below direct desulfurization gas oil, a manufacturing method of claim 1 gas oil composition according the containing 5-30% by volume direct desulfurization gas oil to the feedstock.
Direct degassing oil: 25.0 vol% or more of total aromatic content, 15.0 mass% or more of total naphthene content, 4.0 mass% or more of bicyclic naphthene content, 1.0 mass% or more of tricyclic naphthene content And a sulfur content of 0.01% by mass or more, a 90% distillation temperature of 380.0 ° C. or lower, and a density (15 ° C.) of 0.8700 g / cm ³ or lower. Method for producing a degradation system is a gas oil fraction is below light cycle oil, gas oil composition of claim 1 wherein said containing light cycle oil 1-10% by volume in said feedstock.
Light cycle oil: total aromatic content is 60.0% by volume or more, total naphthene content is 15.0% by mass or more, bicyclic naphthene content is 3.0% by mass or more, tricyclic naphthene content is 1.0% by mass or more, And a sulfur content of 0.07% by mass or more, a 90% distillation temperature of 370.0 ° C. or lower, and a density (15 ° C.) of 0.9800 g / cm ³ or lower.