JP6607492B2 - Method for producing kerosene composition - Google Patents

Description

  The present invention relates to a kerosene composition and a method for producing the kerosene composition, and particularly to a kerosene composition suitably used for heating equipment such as a petroleum stove and a petroleum fan heater, and an internal combustion engine such as a diesel engine, and a method for producing the same.

  Various improvements have been made to the kerosene composition in order to obtain a kerosene composition suitable for use in heating equipment such as an oil stove and an oil fan heater. As such a kerosene composition that has been improved, for example, a fuel composition for oil combustion equipment that has good ignitability and combustibility and low fuel consumption (see, for example, Patent Document 1), improved oxidation stability Kerosene composition (see, for example, Patent Document 2), kerosene composition with excellent storage stability (see, for example, Patent Document 3), low-sulfur kerosene that can stably operate heating equipment over a long period of time (for example, Patent Document 4) is known as the prior art.

JP 2011-84675 A JP 2007-77355 A JP-A-2005-290186 JP 2006-348186 A

  Since the kerosene compositions described in Patent Documents 1 to 4 are not evaluated for long-term use (for example, 1000 hours of use), the improved kerosene composition is used for long-term heating equipment. In fact, it is not always possible to operate stably. Kerosene compositions are often used as fuel oil for diesel engines such as generators in addition to heating equipment. In an internal combustion engine such as a diesel engine, low temperature startability is important. For this reason, it is desirable that the kerosene composition can further improve the low-temperature startability of the internal combustion engine. Therefore, the present invention provides a kerosene composition that is excellent in storage stability, can stably operate a heating device over a long period of time, and can improve the low-temperature startability of an internal combustion engine, and a method for producing the kerosene composition. The purpose is to provide.

The present invention relates to a saturated component composed of paraffin and naphthene in the kerosene composition and a ratio (% by mass) of the aromatic component to the total mass of the aromatic component, a saturated component composed of paraffin and naphthene in the kerosene composition, and The ratio of the bicyclic aromatic content (mass%) to the total mass of the aromatic content (mass%), the value of 0.5 times the mass of the bicyclic naphthene (mass%) and the proportion of the tricyclic naphthene (mass%). By making the total value within a predetermined range, a kerosene composition is obtained that has excellent storage stability, can stably operate the heating equipment over a long period of time, and can improve the low-temperature startability of the internal combustion engine. The present invention has been completed. That is, the present invention is as follows.
[1] The ratio (mass%) of the aromatic content to the sum of the saturated and aromatic components consisting of paraffin and naphthene is a, and the bicyclic aromatic content to the total of the saturated and aromatic content consisting of paraffin and naphthene When the total value of the ratio (mass%) of 0.5, the value (mass%) of 0.5 times the ratio of 2-ring naphthene and the ratio (mass%) of 3-ring naphthene is b,
The kerosene composition which is 15.000 <= a <= 29.000 and is 1.600 <= b <= 4.500.
[2] The ratio (mass%) of the aromatic content to the sum of the saturated and aromatic components consisting of paraffin and naphthene is a, and the bicyclic aromatic content to the total of the saturated and aromatic content consisting of paraffin and naphthene When the total value of the ratio (mass%) of 0.5, the value (mass%) of 0.5 times the ratio of 2-ring naphthene and the ratio (mass%) of 3-ring naphthene is b,
The kerosene composition according to the above [1], wherein 18.000 ≦ a ≦ 29.000 and 1.600 ≦ b ≦ 3.640.
[3] The ratio (mass%) of the aromatic content to the sum of the saturated and aromatic components consisting of paraffin and naphthene is a, and the bicyclic aromatic content to the total of the saturated and aromatic content consisting of paraffin and naphthene. When the total value of the ratio (mass%) of 0.5, the value (mass%) of 0.5 times the ratio of 2-ring naphthene and the ratio (mass%) of 3-ring naphthene is b,
Kerosene composition which is 23.730 <= a <= 29.000 and is 1.600 <= b <= 3.640.
[4] The ratio of the monocyclic aromatic in the aromatic component is 11% by mass or more and 29% by mass or less with respect to the total of the saturated component and the aromatic component composed of paraffin and naphthene. ] The kerosene composition as described in any one of.
[5] A kerosene base produced by hydrocracking heavy gas oil mixed with catalytic cracking gas oil with a hydrocracking unit, a kerosene fraction obtained by fractionating and desulfurizing catalytic cracking gas oil, and desulfurized kerosene derived from oil sands The kerosene composition according to any one of the above [1] to [4], which contains 1% by volume or more of at least one selected from the group consisting of fractions.
[6] The above-mentioned [1] to [5], wherein the ratio of the bicyclic naphthene in the saturated component is 1% by mass or more and less than 12% by mass with respect to the total of the saturated component and the aromatic component composed of paraffin and naphthene. ] The kerosene composition as described in any one of.
[7] Any one of the above [1] to [6], wherein a ratio of a tricyclic naphthene component in a saturated component is 1% by mass or less with respect to a saturated component and an aromatic component composed of paraffin and naphthene. The kerosene composition according to one.
[8] The above [1] to [1], wherein the ratio of indans and tetralins in the aromatic component is 1% by mass or more and less than 10% by mass with respect to the total of the saturated component and the aromatic component composed of paraffin and naphthene. 7] The kerosene composition as described in any one of [7].
[9] The kerosene composition according to any one of [1] to [8], wherein the smoke point is 21 mm or more and less than 50 mm.
[10] The density is 0.75 g / cm ³ or more and 0.85 g / cm ³ or less,
The boiling range is 140 ° C. or more and 300 ° C. or less,
95% distillation temperature is 220 ° C. or higher and 270 ° C. or lower,
Sulfur content is 80 mass ppm or less,
The peroxide value is 1 ppm or less,
The nitrogen content is 1 mass ppm or less,
The kinematic viscosity at 30 ° C. is 0.9 mm ² / s to 1.7 mm ² / s,
Saybolt color is +25 or more,
Copper plate corrosion is 1 or less,
The flash point is 40 ° C or higher,
The kerosene composition according to any one of the above [1] to [9], wherein the cetane index is 45 or more.
[11] A raw material oil obtained by mixing a kerosene fraction obtained by mixing catalytic cracked light diesel oil (HVN) or oil sand-derived kerosene fraction with a catalyst bed formed by using a hydrorefining catalyst to produce hydrogen. It is a manufacturing method of the kerosene composition including the process of chemical refining process, Comprising: A straight-run kerosene has the property of following (a)-(c), and catalytic cracking light gas oil has the property of following (d)-(f), respectively. Meet,
At the feedstock inlet for hydrorefining treatment,
The hydrogen pressure is 2 MPa or more and 10 MPa or less,
LHSV is 2h- ¹ or more and 15h- ¹ or less,
The reaction temperature is 200 ° C. or higher and 360 ° C. or lower,
The hydrogen / raw oil ratio was set to 50 nL / L or more and 500 nL / L or less.
A method for producing a kerosene composition.
(A) 95% distillation temperature distilled from an atmospheric distillation apparatus in straight-run kerosene is 200 ° C. or higher and 280 ° C. or lower,
(B) the density of the straight run kerosene 0.750 g / cm ³ or more 0.850 g / cm ³ or less,
(C) The sulfur content of straight-run kerosene is 0.001% by mass to 0.8% by mass,
(D) The cetane index of straight-run kerosene is 47.5 or more,
(E) The 95% distillation temperature distilled from the catalytic cracking device in the catalytic cracking light diesel oil is 180 ° C. or higher and 270 ° C. or lower,
(F) the density of catalytically cracked light gas oil is 0.750 g / cm ³ or more 0.900 g / cm ³ or less,
(G) The sulfur content of the catalytically cracked light gas oil is 0.001% by mass or more and 0.08% by mass or less.
[12] A catalyst bed formed by using a hydrocracking catalyst with a raw oil obtained by mixing a heavy gas oil (HGO), a vacuum heavy gas oil (VGO) or a mixture thereof with a catalytic cracking gas oil (LCO). A method for producing a kerosene composition comprising a step of hydrocracking by contacting with
Heavy gas oil and reduced pressure heavy gas oil satisfy the following properties (a) to (c), and catalytic cracked light gas oil satisfies the following properties (d) to (f):
At the feedstock inlet for hydrocracking,
A hydrogen pressure of 3 MPa to 20 MPa,
A LHSV 0.1h ^-1 more than ^{10h -1} or less,
The reaction temperature is 300 ° C. or more and 450 ° C. or less,
The hydrogen / raw oil ratio was set to 300 nL / L or more and 2000 nL / L or less,
A method for producing a kerosene composition.
(A) 95% distillation temperature distilled from an atmospheric distillation apparatus or a reduced pressure distillation apparatus for heavy gas oil and vacuum heavy gas oil is 400 ° C or higher and 600 ° C or lower,
(B) The density of heavy gas oil and vacuum heavy gas oil is 0.800 g / cm ³ or more and 1.000 g / cm ³ or less,
(C) The sulfur content of heavy gas oil and reduced-pressure heavy gas oil is 1.0% by mass or more and 3.0% by mass or less,
(D) 90% distillation temperature of distilling from the catalytic cracking unit in catalytic cracking light diesel oil is 280 ° C or higher and 390 ° C or lower
(E) The density of the catalytically cracked light diesel oil is 0.800 g / cm ³ or more and 1.000 g / cm ³ or less,
(F) The sulfur content of the catalytically cracked light gas oil is 0.1% by mass or more and 0.8% by mass or less. (G) The cetane index of the catalytically cracked light gas oil is 24 or more.
[13] Oil sand synthetic crude oil containing one or more selected from the group consisting of premium Arabian synthetic, Sancor oil sand blend A and cinque sweet blend is passed through an atmospheric distillation unit. The method for producing a kerosene composition according to the above [11], which is a kerosene fraction obtained by oiling.

  According to the present invention, a kerosene composition that is excellent in storage stability, can stably operate a heating device over a long period of time, and can improve the low-temperature startability of an internal combustion engine, and a method for producing the kerosene composition are provided. Can be provided.

FIG. 1 is a graph in which the values of a and b of Examples 1 to 9 and Comparative Examples 1 to 6 are plotted.

[The kerosene composition of the present invention]
In the kerosene composition of the present invention, the ratio (mass%) of the aromatic component to the sum of the saturated and aromatic components consisting of paraffin and naphthene is a, and the sum of the saturated and aromatic components consisting of paraffin and naphthene is When the total value of the ratio (mass%) of the bicyclic aromatic fraction (0.5%), the ratio of bicyclic naphthene (0.5%) and the ratio of tricyclic naphthene (mass%) is b ,
15.000 ≦ a ≦ 29.000 and 1.600 ≦ b ≦ 4.500.
Hereinafter, the kerosene composition of the present invention will be described in detail.

(Saturated and aromatic content)
The kerosene composition of the present invention contains a saturated component and an aromatic component. Saturates consist of paraffin and naphthene. Paraffin is a saturated chain compound, and paraffin is linear or branched. Naphthene is a compound having a naphthene ring (saturated ring). The naphthene contained in the kerosene composition of the present invention includes at least one naphthene selected from the group consisting of a bicyclic naphthene having two naphthene rings and a tricyclic naphthene having three naphthene rings. The naphthene contained in the kerosene composition of the present invention may further contain a monocyclic naphthene having one naphthene ring.

  On the other hand, the aromatic component is a compound having an aromatic ring. The aromatic component contained in the kerosene composition of the present invention includes a two-ring aromatic having two aromatic rings. The aromatic component contained in the kerosene composition of the present invention may further contain a single-ring aromatic having one aromatic ring. The monocyclic aromatic may include alkylbenzenes, indanes and tetralins. The bicyclic aromatic may also contain at least one compound selected from the group consisting of indenes, naphthalenes and biphenyls.

In the kerosene composition of the present invention, when the ratio (mass%) of the aromatic component to the total of the saturated component and the aromatic component consisting of paraffin and naphthene is a,
15.000 ≦ a ≦ 29.000,
Preferably, 18.000 ≦ a ≦ 29.000,
More preferably, it is 23.730 <= a <= 29.000.
When the value of a is less than 15.000, the storage stability of the kerosene composition may deteriorate and the low temperature startability of the internal combustion engine may deteriorate. On the other hand, if the value of a is larger than 29.00, it may be difficult to operate the heating device stably over a long period of time. In addition, the ratio of a saturated part and the ratio of an aromatic part are the values measured by two-dimensional gas chromatography.

  The above-mentioned heating equipment is stably operated over a long period of time, for example, after burning a kerosene composition in a heating equipment for 1000 hours, an exhaust gas test, a fuel consumption test, an odor test, an ignition time and a fire extinguishing time test, and a core type It is a success in observing the deterioration of the core of the stove and the nozzle of the fan heater. Each test and deterioration state observation will be described in detail in Examples described later.

The ratio (mass%) of the bicyclic aromatic content and the ratio of the bicyclic naphthene content (mass%) and the tricyclic naphthene content to the sum of the saturated and aromatic content consisting of paraffin and naphthene. When the total value with the ratio (mass%) is b,
1.600 ≦ b ≦ 4.500,
Preferably 1.600 ≦ b ≦ 3.640.
When the value of b is less than 1.600, the storage stability of the kerosene composition deteriorates,
The low temperature startability of the internal combustion engine may deteriorate. On the other hand, if the value of b is larger than 4.500, it may be difficult to operate the heating device stably over a long period of time. In addition, the ratio for a saturated part, the ratio for an aromatic part, the ratio for a two-ring aromatic part, the ratio for a two-ring naphthene, and the ratio for a three-ring naphthene are values measured by two-dimensional gas chromatography.

Furthermore, 15.000 ≦ a ≦ 29.000 and 1.600 ≦ b ≦ 4.500,
Preferably, 15.000 ≦ a ≦ 29.000 and 1.600 ≦ b ≦ 3.640,
Preferably, 18.000 ≦ a ≦ 29.000 and 1.600 ≦ b ≦ 4.500,
More preferably, 18.000 ≦ a ≦ 29.000 and 1.600 ≦ b ≦ 3.640,
More preferably, 23.730 ≦ a ≦ 29.000 and 1.600 ≦ b ≦ 4.500,
More preferably, 23.730 ≦ a ≦ 29.000 and 1.600 ≦ b ≦ 3.640.

Moreover, from the viewpoint that the storage stability of the kerosene composition becomes better, the heating equipment can be operated more stably over a long period of time, and the low-temperature startability of the internal combustion engine can be made better.
More preferably, 23.000 ≦ a ≦ 29.000 and 1.600 ≦ b ≦ 3.000,
More preferably, 23.000 ≦ a ≦ 29.000 and 1.600 ≦ b ≦ 2.300 may be satisfied.

The present inventors have found that, among naphthene components, 2-ring naphthene and 3-ring naphthene affect the long-term operation of heating equipment. The ratio of the bicyclic naphthene in the saturated component is preferably 1% by mass or more and less than 12% by mass, and more preferably 1% by mass or more and 8% by mass with respect to the total of the saturated component and the aromatic component composed of paraffin and naphthene. % Or less, and more preferably 1% by mass or more and 6% by mass or less. When the proportion of the bicyclic naphthene in the saturated group is 1% by mass or more and less than 12% by mass, the kerosene composition can operate the heating equipment more stably over a long period of time.
Further, the ratio of the tricyclic naphthene in the saturated portion is preferably 1% by mass or less based on the total of the saturated portion and the aromatic portion composed of paraffin and naphthene. When the proportion of tricyclic naphthene in the aromatic component is 1% by mass or less, the kerosene composition can operate the heating device more stably over a long period of time.
The ratios of 2-ring naphthene and 3-ring naphthene are values measured by two-dimensional gas chromatography.

  The present inventors have found that, among aromatic components, the monocyclic aromatic component affects the long-term operation of the heating equipment. The ratio of monocyclic aromatics in the aromatic component is preferably 11% by mass or more and 29% by mass or less, and more preferably 23.3% by mass with respect to the total of the saturated component and the aromatic component composed of paraffin and naphthene. % Or more and 28.3 mass% or less. When the ratio of the monocyclic aromatic in the aromatic component is 11% by mass or more and 29% by mass or less, the kerosene composition can operate the heating device more stably over a long period of time. In addition, the ratio of the monocyclic aromatic component and the bicyclic aromatic component is a value measured by two-dimensional gas chromatography.

  The present inventors have found that, among monocyclic aromatic components, indans and tetralins in particular affect the long-term operation of heating equipment. The ratio of indanes and tetralins in the aromatic component is preferably 1% by mass or more and less than 10% by mass with respect to the total of the saturated component and the aromatic component composed of paraffin and naphthene. When the ratio of indans and tetralins is 1% by mass or more and less than 10% by mass, the kerosene composition can operate the heating equipment more stably over a long period of time. In addition, the ratio of indanes and tetralins is a value measured by two-dimensional gas chromatography.

  The smoke point of the kerosene composition of the present invention is preferably 21 mm or more and less than 50 mm, more preferably 23 mm or more and less than 50 mm. In addition, the smoke point of a kerosene composition is the value measured based on JISK2537. When the smoke point is 21 mm or more and less than 50 mm, it is possible to suppress the generation of smoke during the operation of the heating device over a long period of time.

(Properties of kerosene composition)
The kerosene composition of the present invention preferably further has the following properties.
Density: 0.75 g / cm ³ or more and 0.85 g / cm ³ or less Boiling range: 140 ° C. or more and 300 ° C. or less 95% distillation temperature: 220 ° C. or more and 270 ° C. or less Sulfur content: 80 mass ppm or less Peroxide value: 1 ppm or less Nitrogen content: 1 mass ppm or less Kinematic viscosity at 30 ° C .: 0.9 mm ² / s to 1.7 mm ² / s or less Saybolt color: +25 or more Copper plate corrosion: 1 or less Flash point: 40 ° C. or more Cetane index: 45 or more

The density is a value measured according to JIS K 2249. When the density is less than 0.75 g / cm ³ , the fuel consumption rate is lowered, and when it exceeds 0.85 g / cm ³ , the combustibility is deteriorated, so the density is 0.75 g / cm ³ or more and 0.85 g / cm ^3. When it is below, the calorific value of the kerosene composition is increased, and the fuel consumption rate is improved. The density is more preferably 0.77 g / cm ³ or more and 0.82 g / cm ³ or less.

  The boiling range is the boiling range of a fraction obtained by distilling crude oil. When the boiling range is 140 ° C. or more and 300 ° C. or less, the combustibility of the kerosene composition is improved. The boiling range is more preferably 145 ° C. or higher and 285 ° C. or lower.

  The 95% distillation temperature is a value measured according to JIS K 2254. When the 95% distillation temperature is 220 ° C. or more and 270 ° C. or less, it is possible to suppress the occurrence of defects due to unburned residue remaining in the core when used in the core type stove. The 95% distillation temperature is more preferably 225 ° C. or higher and 268 ° C. or lower.

  The sulfur content is a value measured according to JIS K2541. Generation | occurrence | production of SOx during combustion can be suppressed as a sulfur content is 80 mass ppm or less. The sulfur content is more preferably 50 ppm by mass or less.

  The peroxide value is a value measured according to JIS K 2276. When the peroxide value is 1 ppm or less, the storage stability of the kerosene composition is improved. The peroxide value is more preferably 0.5 ppm or less.

  The nitrogen content is a value measured by a chemiluminescence method, and is a value measured by a gas chromatography-atomic emission method or a gas chromatography-chemiluminescence method. Generation | occurrence | production of NOx during combustion can be suppressed as nitrogen content is 1 mass ppm or less. The nitrogen content is more preferably 0.5 ppm by mass or less.

The kinematic viscosity at 30 ° C. is a value measured according to JIS K 2283. When the kinematic viscosity at 30 ° C. is 0.9 mm ² / s or more and 1.7 mm ² / s or less, combustible vapor is generated at room temperature, and it is possible to suppress ignition by static electricity and the like, and fuel is generated by capillary action. Even when used as a fuel for a core type stove to be supplied, the fuel can be supplied stably. The kinematic viscosity at 30 ° C. is more preferably 1.0 mm ² / s to 1.6 mm ² / s.

  The Saebold color is a value measured in accordance with JIS K 2580. When the Saybolt color is +25 or more, the kerosene composition can be prevented from being colored and regarded as deteriorated kerosene. The Saybolt color is more preferably +30 or more.

  Copper plate corrosion is a value measured according to JIS K2513. When the copper plate corrosion is 1 or less, the heating equipment can be prevented from being corroded by the kerosene composition.

  The flash point is a value measured in accordance with JIS K 2265 (tag sealed flash point test method). When the flash point is 40 ° C. or higher, combustible vapor is generated at room temperature, and ignition of the kerosene composition due to static electricity or the like can be suppressed. The flash point is more preferably 41 ° C. or higher.

  The cetane index is a value measured according to JIS K 2280 (petroleum product-fuel oil-octane number and cetane number test method and cetane index calculation method). When the cetane index is 45 or more, the low-temperature startability of the internal combustion engine can be improved.

(Raw material of kerosene composition)
The kerosene composition of the present invention is preferably a kerosene base prepared by hydrocracking heavy gas oil mixed with catalytic cracking gas oil using a hydrocracking apparatus, a kerosene fraction obtained by fractionating and desulfurizing catalytic cracking gas oil, and 1 vol% or more of at least one selected from the group consisting of desulfurized kerosene fraction derived from oil sand is included. More preferably, in the kerosene composition of the present invention, the kerosene base ratio of kerosene base prepared by hydrocracking heavy gas oil mixed with catalytic cracking light oil with a hydrocracking apparatus is 1% by volume or more and 40% by volume. More preferably, it is 1% by volume or more and 20% by volume or less, and the maximum oil passage ratio of catalytically cracked light gas oil (HVN) which is a kerosene fraction obtained by fractionating and desulfurizing catalytically cracked light oil is 1% by volume or more and 15% The volume ratio is less than volume%, more preferably 1 volume% or more and 11 volume% or less, and the kerosene fraction maximum ratio of the desulfurized kerosene fraction derived from the oil sand is 1 volume% or more and 10 volume% or less. By using such a kerosene base material or kerosene fraction, a kerosene composition satisfying the above-described value range of a and value range of b can be obtained.

[Method for producing kerosene composition of the present invention]
The kerosene composition of the present invention is formed, for example, by using a hydrorefining catalyst, a raw material oil obtained by mixing a kerosene fraction obtained from catalytic cracking light diesel oil (HVN) or oil sand with straight-run kerosene (KERO). It is obtained by a method for producing a kerosene composition comprising a step of hydrotreating by contacting with a catalyst bed (manufacturing method 1 of a kerosene composition). In particular, the hydrorefining treatment can reduce mercaptans that cause odors in the feedstock and aromatics that cause smoke, and improve the corrosivity and color of the feedstock. In this case, preferably, the 95% distillation temperature of distillation from the atmospheric distillation apparatus in straight-run kerosene is 200 ° C. or higher and 280 ° C. or lower, more preferably 220 ° C. or higher and 270 ° C. or lower. is a 0.750 g / cm ³ or more 0.850 g / cm ³ or less, more preferably 0.770 g / cm ³ or more 0.820 g / cm ³ or less, sulfur content of straight run kerosene 0.001% It is 0.8 mass% or less, more preferably 0.005 mass% or more and 0.7 mass% or less, and the cetane index of straight-run kerosene is 47.5 or more, more preferably 48.0 or more. is there. In addition, the 95% distillation temperature of distillation from the catalytic cracking device in the catalytic cracking light diesel oil is 180 ° C. or higher and 270 ° C. or lower, more preferably 180 ° C. or higher and 250 ° C. or lower. 750 g / cm ³ or more 0.900 g / cm ³ or less, and more preferably not more than 0.770 g / cm ³ or more 0.880 g / cm ^3, the sulfur content of the catalytically cracked light gas oil than 0.001 wt% 0 0.08% by mass or less, and more preferably 0.001% by mass or more and 0.07% by mass or less. Furthermore, the inlet of the feedstock in the hydrotreating process, hydrogen pressure is less 10MPa or more 2 MPa, more preferably not more than 8MPa than 2.5 MPa, LHSV is at ^{2h -1} or ^{15h -1} or less, more preferably not more than ^{3h -1} or ^{12h -1,} reaction temperature is 200 ° C. or higher 360 ° C. or less, and more preferably not more than 340 ° C. 250 ° C. or higher, a hydrogen / feed oil ratio, 50 nL / L or more 500nL / L or less, more preferably 70 nL / L or more and 300 nL / L or less.

  As the hydrorefining catalyst, for example, an alumina catalyst in which molybdenum is supported on an alumina carrier can be used. Further, cobalt, nickel, molybdenum and the like may be used as a promoter metal. The oil sand-derived kerosene fraction is an oil sand synthetic crude oil containing one or more selected from the group consisting of premium Arabian synthetics, sangkor oil sand blend A and cinque sweet blend. It is preferable that it is a kerosene fraction obtained by passing through the oil.

  An oil composition obtained by hydrorefining raw material oil obtained by mixing kerosene with kerosene and keratin fraction derived from catalytic cracking light diesel oil (HVN) or oil sand may be used as it is as a kerosene composition. However, it is more preferable to use as the kerosene composition a composition obtained by adding at least one compound selected from the group consisting of gas oil peripheral oil type identification agent (coumarin) and fuel oil antistatic agent to the above composition.

In addition, a raw oil obtained by mixing the kerosene composition of the present invention with heavy light oil (HGO), reduced pressure heavy light oil (VGO) or a mixture thereof with catalytic cracking light oil (LCO) is used with a hydrocracking catalyst. It can also be obtained by a method for producing a kerosene composition comprising a hydrocracking treatment by contacting with a catalyst bed formed in this manner (kerosene composition production method 2). In this case, the 95% distillation temperature of distillation from the atmospheric distillation apparatus or the vacuum distillation apparatus in heavy gas oil and vacuum heavy gas oil is preferably 400 ° C. or more and 600 ° C. or less, more preferably 420 ° C. or more and 580 ° C. or less, the density of the heavy gas oil and vacuum heavy gas oil is at 0.800 g / cm ³ or more 1.000 g / cm ³ or less, more preferably 0.820 g / cm ³ or more 0.950 g / cm ³ or less In addition, the sulfur content of heavy gas oil and vacuum heavy gas oil is 1.0% by mass or more and 3.0% by mass or less, and more preferably 1.5% by mass or more and 2.8% by mass or less. The 90% distillation temperature of the catalytic cracking light gas oil distilled from the catalytic cracking apparatus is 280 ° C. or higher and 390 ° C. or lower, more preferably 300 ° C. or higher and 370 ° C. or lower. 800 g / cm ³ or more 1.000 g / cm ³ or less, and more preferably not more than 0.820 g / cm ³ or more 0.980 g / cm ^3, the sulfur content of the catalytically cracked light gas oil 0.1 wt% 0 0.8 mass% or less, more preferably 0.2 mass% or more and 0.7 mass% or less, and the cetane index of the catalytically cracked light gas oil is 24 or more, more preferably 24.5 or more. Furthermore, the inlet of the feedstock in the hydrocracking process, the hydrogen pressure is less than 20MPa over 3 MPa, more preferably not more than 18MPa over 10 MPa, LHSV is at 0.1 h ^-1 or more ^{10h -1} or less, more preferably not more than 0.3h ^-1 or ^{5h -1,} reaction temperature must 300 ° C. or higher 450 ° C. or less, more preferably 360 ° C. or higher 420 ° C. or less, the hydrogen / feedstock ratio of 300 nL / L or more 2000nL / L or less, more preferably 500 nL / L or more and 1000 nL / L or less. In the production of catalytic cracking light oil, the reaction tower outlet temperature of the fluid catalytic cracking apparatus is, for example, 500 ° C. or more and 540 ° C. or less, and the reaction tower pressure is, for example, 0.07 MPaG or more and 0.30 MPaG or less, The ratio is, for example, 4 or more and 30 or less.

  The kerosene composition of the present invention can also be produced by mixing the kerosene composition produced by the above-described kerosene composition production method 1 and the kerosene composition produced by the above-described kerosene composition production method 2. it can.

  EXAMPLES Next, although an Example demonstrates this invention further in detail, this invention is not limited at all by these examples.

[Composition analysis and evaluation method of kerosene composition]
Composition analysis and evaluation in each example and comparative example were performed as follows.
(Composition analysis by two-dimensional gas chromatography)
Using two-dimensional gas chromatography (manufactured by ZOEX, model number: ZOEX KT2006), paraffin, monocyclic naphthene, bicyclic ring with respect to the sum of saturated and aromatic components in the kerosene compositions of Examples and Comparative Examples The proportions of naphthene, tricyclic naphthene, alkylbenzenes, indanes and tetralins, indenes, naphthalenes and biphenyls were measured. In addition, the sum total of the ratio of 1-ring naphthene, 2-ring naphthene, and 3-ring naphthene becomes the ratio of naphthene. In addition, the sum of the ratios of paraffin and naphthene is the ratio of saturation. Furthermore, the sum of the proportions of alkylbenzenes, indanes and tetralins is the proportion of monocyclic aromatics. Further, the sum of the proportions of indenes, naphthalenes and biphenyls is the proportion of the bicyclic aromatic component. Furthermore, the sum of the proportions of the monocyclic aromatic component and the bicyclic aromatic component becomes the aromatic component.

(Stove burning test)
Core type stove burned with kerosene composition for a total of 1000 hours (Corona Co., Ltd., model number: SX-246, type: core type, radiation type, ignition method: battery ignition, heating output: 2.42 kW, fuel consumption Quantity: 0.235 L / h, type of core: normal cylindrical core (R-28), nominal size of core: φ65 × 2.8 mm) and fan heater (manufactured by Dainichi Kogyo Co., Ltd., model number: FW-253NES, type : Vaporization type, forced ventilation type, forced convection type, ignition system: continuous discharge ignition, heating output: 2.50 kW, fuel consumption: maximum 0.243 L / h, minimum 0.066 L / h) (hereinafter these are summarized) In some cases, the following items were tested. The heating device was operated for 10 hours a day.

(1) Exhaust gas test Using an exhaust gas analyzer (manufactured by Horiba, Ltd., model number: MEXA-7000DEGR), exhaust gas generated from the heating device 5 minutes after ignition, 30 minutes after steady combustion The concentrations of CO, CO ₂ , NOx and THC (total hydrocarbons) of the exhaust gas generated from the heating device and the exhaust gas generated from the heating device were measured for 5 minutes after extinguishing the fire. The average concentration of the measured concentrations was taken as the concentration during ignition of each gas, the concentration during steady combustion, and the concentration during fire extinguishing. When the CO / CO ₂ and NOx of the exhaust gas during steady combustion were 0.002 or less and 90 ppm or less, respectively, and the THC concentration during ignition was 100 ppm or less, the exhaust gas test was passed. Note that NOx was converted to the minimum combustion time (CO ₂ concentration 15.2%) in accordance with JIS S 3032.

(2) Fuel consumption test The amount of fuel used for one hour in the steady combustion of the heating device was examined. The heating device was set to maximum combustion. When the difference between the fuel consumption for one hour and the rated fuel consumption in the steady combustion of the heating device is within 10% of the rated fuel consumption, the fuel consumption test was passed.

(3) Exhaust gas odor test The exhaust gas odor at the time of ignition, combustion and extinguishing of the heating device was evaluated in five levels by a sensory test with five monitors.
Evaluation stage 1: No feeling Evaluation stage 2: Feeling slightly Evaluation stage 3: Feeling Evaluation stage 4: Feeling slightly strong Evaluation stage 5: Feeling strongly If there are two or more monitors evaluated in evaluation stage 5, the smell of exhaust gas The test passed.

(4) Ignition time, fire extinguishing time In the case of a core-type stove, measure the time from when the type of fire in the heating wire contacts the core until the fire turns around the core, and in the case of a fan heater, the ignition switch The time from when was pressed to when the fire started was measured, and the measured time was taken as the ignition time. In the case of a core-type stove, measure the time until the flame on the core completely disappears after the stove core is set to the normal fire extinguishing position, and in the case of a fan heater, until the fire goes out after the fire switch is pressed Was measured, and the measured time was taken as the fire extinguishing time. In the case of a core-type stove, when the ignition time and the fire extinguishing time are within 10 seconds and within 300 seconds, respectively, in the case of a fan heater, when the ignition time and the fire extinguishing time are within 40 seconds and within 20 seconds, respectively, Time and fire extinguishing time passed.

(5) Observation of deterioration of the core heater and the nozzle of the fan heater The deterioration of the core heater and the nozzle of the fan heater was observed using a magnifying glass. Then, the degree of adhesion of the corktal was examined. If remarkably many coctals were not attached to the core of the core-type stove and the nozzle of the fan heater, the deterioration condition of the core of the core-type stove and the nozzle of the fan heater was passed.

  In addition, when all the above evaluations are passed, it is assumed that the stove combustion test is passed.

(Low temperature startability test)
The cold startability was evaluated by the following test.
(1) Cell start time When operating the DGW190M, which is a small air-cooled single cylinder diesel engine manufactured by Shin-Daiwa Industry Co., Ltd., in a no-load state with the test chamber maintained at a temperature of -10 ° C and a humidity of 60%. The cell start-up time was evaluated. The time for rotating the cell motor was 10 seconds (the switch was turned off for 7 seconds after the decompression switch was turned on for 3 seconds), and it was confirmed whether the cell motor would rotate at this time. If it did not rotate, the cell motor was rotated for 15 seconds, 20 seconds, and 5 seconds, and restarted.

(2) 3000 rpm arrival time When the engine was started under the conditions described in (1), the time until the engine rotation speed reached 3000 rpm for the first time was confirmed.

  In addition, when all the above evaluations are passed, it is assumed that the low temperature startability test is passed.

[Properties of the used oil]
Table 1 summarizes the properties of the feedstock oil used in each Example and Comparative Example.

(Examples 1 and 2)
0% and 20% by volume of a kerosene base material prepared by hydrocracking a raw oil obtained by mixing 20% by volume of catalytic cracking gas oil (LCO) with heavy gas oil (HGO) is added to commercially available kerosene. Thus, kerosene compositions of Examples 1 and 2 were prepared.

The conditions for hydrocracking treatment are as follows: the end point of distillation from the atmospheric distillation apparatus or the vacuum distillation apparatus for heavy light oil is 540 ° C., the density of heavy light oil is 0.910 g / cm ³ , The sulfur content was 2.20% by mass. In addition, the 90% distillation temperature of distilling from the catalytic cracking light diesel oil in the catalytic cracking light oil is 352 ° C., the density of the catalytic cracking light diesel oil is 0.940 g / cm ³ , and the sulfur content of the catalytic cracking light diesel oil is 0. It was 50 mass%. Furthermore, at the inlet of the raw material oil in the hydrocracking treatment, the hydrogen pressure was 15 MPa, the LHSV was 3 h ⁻¹ , the reaction temperature was 380 ° C., and the hydrogen / raw material oil ratio was 700 nL / L. The 90% distillation temperature of the hydrocracked kerosene base material was 245 ° C.

(Example 3)
The kerosene composition of Example 3 was produced by hydrotreating a raw oil in which kerosene fraction derived from 10 vol% oil sand was mixed with straight kerosene (KERO).

Example 4
A desulfurized kerosene (DK) produced by hydrotreating a raw oil obtained by mixing 11 vol% catalytic cracked light diesel oil (HVN) with straight-run kerosene (KERO) was used as a kerosene base material. The kerosene composition of Example 4 has a ratio of the kerosene base material of 100% by volume. The operating conditions of the hydrorefining treatment were a pressure of 5 MPa, a temperature of 290 ° C., an LHSV of 7 h ⁻¹ , a hydrogen / feed oil ratio of 70 nL / L, and a chemical hydrogen consumption of 23 Nm ³ / kL.

(Example 5)
A desulfurized kerosene (DK) produced by hydrotreating raw oil obtained by mixing 25 vol% catalytically cracked light diesel oil (HVN) with straight-run kerosene (KERO) was used as a kerosene base material. The kerosene composition of Example 5 was obtained by mixing the kerosene base material and commercial kerosene at a ratio of 50% by volume and 50% by volume, respectively. The operating conditions of the hydrorefining treatment are: the pressure is 5 MPa, the temperature is 300 ° C., the LHSV is 7 h ⁻¹ , the hydrogen / feed oil ratio is 90 nL / L, and the chemical hydrogen consumption is 33 Nm ³ / kL.

(Example 6)
Hydrogenation produced by hydrorefining a feedstock mixed with 48% by volume heavy gas oil (HGO), 32% by volume vacuum heavy gas oil (VGO) and 20% by volume catalytic cracking gas oil (LCO). Decomposed kerosene (HCK) was used as a kerosene substrate. The kerosene base material and the commercial kerosene were mixed so that the ratio of the kerosene base was 20% by volume and the ratio of the commercial kerosene was 80% by volume to prepare the kerosene composition of Example 6. The operating conditions of the hydrorefining treatment are: the pressure is 16 MPa, the temperature is 380 ° C., the LHSV is 3 h ⁻¹ , the hydrogen / feed oil ratio is 800 nL / L, and the chemical hydrogen consumption is 320 Nm ³ / kL.

(Example 7)
Hydrogenation produced by hydrorefining a feedstock mixed with 54% by volume heavy gas oil (HGO), 36% by volume vacuum heavy gas oil (VGO) and 10% by volume catalytic cracking gas oil (LCO). Decomposed kerosene (HCK) was used as a kerosene substrate. The kerosene base material and the commercial kerosene were mixed so that the ratio of the kerosene base was 4% by volume and the ratio of the commercial kerosene was 60% by volume to prepare the kerosene composition of Example 7. The operating conditions of the hydrorefining treatment were a pressure of 15 MPa, a temperature of 380 ° C., an LHSV of 3 h ⁻¹ , a hydrogen / feed oil ratio of 700 nL / L, and a chemical hydrogen consumption of 300 Nm ³ / kL.

(Example 8)
A desulfurized kerosene (DK) produced by hydrorefining a raw oil obtained by mixing 1 vol% catalytic cracking light diesel oil (HVN) with straight-run kerosene (KERO) was used as a kerosene base material. The kerosene composition of Example 8 has a ratio of the kerosene base material of 100% by volume. The operating conditions of the hydrorefining treatment are: the pressure is 5 MPa, the temperature is 290 ° C., the LHSV is 7 h ⁻¹ , the hydrogen / feed oil ratio is 70 nL / L, and the chemical hydrogen consumption is 20 Nm ³ / kL.

Example 9
A desulfurized kerosene (DK) produced by hydrotreating a raw oil obtained by mixing 30 vol% catalytically cracked light diesel oil (HVN) with straight-run kerosene (KERO) was used as a kerosene base material. The kerosene composition of Example 9 was obtained by mixing the kerosene base material and commercially available kerosene at a ratio of 40% by volume and 60% by volume, respectively. The operating conditions of the hydrorefining treatment are: the pressure is 5 MPa, the temperature is 300 ° C., the LHSV is 7 h ⁻¹ , the hydrogen / feed oil ratio is 90 nL / L, and the chemical hydrogen consumption is 40 Nm ³ / kL.

(Comparative Example 1)
A kerosene composition of Comparative Example 1 was prepared by hydrotreating a raw oil obtained by mixing 15 vol% catalytic cracking light diesel oil (HVN) with straight-run kerosene (KERO).

The conditions of hydrorefining treatment are as follows: 95% distillation temperature distilled from an atmospheric distillation apparatus in straight-run kerosene is 263 ° C., and the density of straight-run kerosene is 0.796 g / cm ³ . The sulfur content was 0.4% by mass. Moreover, the 95% distillation temperature distilled from the catalytic cracking device for catalytic cracking light diesel oil is 223 ° C., the density of the catalytic cracking light diesel oil is 0.861 g / cm ³ , and the sulfur content of the catalytic cracking diesel fuel is 0. 0.05% by mass. Furthermore, at the inlet of the raw material oil in the hydrorefining treatment, the hydrogen pressure is 5 MPa, the LHSV is 7 h ⁻¹ , the reaction temperature is 290 ° C., and the hydrogen / raw oil ratio is 70 nL / L or more and 80 nL / L. It was the following.

The conditions of hydrorefining treatment are as follows: 95% distillation temperature distilled from an atmospheric distillation apparatus in straight-run kerosene is 263 ° C., and the density of straight-run kerosene is 0.796 g / cm ³ . The sulfur content was 0.4% by mass. In addition, the 95% distillation temperature of the kerosene fraction derived from the oil sand distilled from the catalytic cracking apparatus is 263 ° C., the density of the kerosene fraction derived from the oil sand is 0.840 g / cm ³ , and is derived from the oil sand. The sulfur content of the kerosene fraction was 0.006% by mass. Furthermore, at the inlet of the feedstock oil in the hydrorefining treatment, the hydrogen pressure is 6 MPa, the LHSV is 7 h ⁻¹ , the reaction temperature is 300 ° C., and the hydrogen / feedstock ratio is 70 nL / L or more and 80 nL / L. It was the following.

(Comparative Example 2)
Hydrogenation produced by hydrorefining a feedstock mixed with 57% by volume heavy gas oil (HGO), 38% by volume vacuum heavy gas oil (VGO) and 5% by volume catalytic cracking gas oil (LCO). Decomposed kerosene (HCK) was used as a kerosene substrate. The kerosene composition of Comparative Example 2 was obtained by setting the kerosene base to 100% by volume. The operating conditions of the hydrorefining treatment were a pressure of 15 MPa, a temperature of 380 ° C., an LHSV of 3 h ⁻¹ , a hydrogen / feed oil ratio of 700 nL / L, and a chemical hydrogen consumption of 290 Nm ³ / kL.

(Comparative Example 3)
Hydrocracked kerosene (HCK) produced by hydrotreating 57 volume% heavy gas oil (HGO) and 38 volume% vacuum heavy gas oil (VGO) was used as a kerosene base material. The kerosene composition of Comparative Example 3 was obtained by setting this kerosene base material to 100% by volume. The operating conditions of the hydrorefining treatment were a pressure of 15 MPa, a temperature of 380 ° C., an LHSV of 3 h ⁻¹ , a hydrogen / feed oil ratio of 700 nL / L, and a chemical hydrogen consumption of 290 Nm ³ / kL.

(Comparative Example 4)
Hydrogenation produced by hydrorefining a feedstock mixed with 48% by volume heavy gas oil (HGO), 32% by volume vacuum heavy gas oil (VGO) and 20% by volume catalytic cracking gas oil (LCO). Decomposed kerosene (HCK) was used as a kerosene substrate. A kerosene composition of Comparative Example 3 was prepared by mixing a kerosene base material and a straight kerosene (KERO) so that the ratio of the kerosene base was 40% by volume and the ratio of the kerosene kerosene (KERO) was 60% by volume. did. The operating conditions of the hydrorefining treatment are: the pressure is 16 MPa, the temperature is 380 ° C., the LHSV is 3 h ⁻¹ , the hydrogen / feed oil ratio is 800 nL / L, and the chemical hydrogen consumption is 320 Nm ³ / kL.

(Comparative Example 5)
Comparative example by adding 20% by volume of kerosene base material prepared by hydrocracking raw oil mixed with 20% by volume catalytic cracking light oil (LCO) to heavy gas oil (HGO) to commercial kerosene 5 kerosene compositions were prepared. The conditions for hydrocracking treatment are as follows: the end point of distillation from the atmospheric distillation apparatus or the vacuum distillation apparatus for heavy light oil is 540 ° C., the density of heavy light oil is 0.910 g / cm ³ , The sulfur content was 2.20% by mass. In addition, the 90% distillation temperature of distilling from the catalytic cracking light diesel oil in the catalytic cracking light oil is 352 ° C., the density of the catalytic cracking light diesel oil is 0.940 g / cm ³ , and the sulfur content of the catalytic cracking light diesel oil is 0. It was 50 mass%. Furthermore, at the inlet of the raw material oil in the hydrocracking treatment, the hydrogen pressure was 15 MPa, the LHSV was 3 h ⁻¹ , the reaction temperature was 380 ° C., and the hydrogen / raw material oil ratio was 700 nL / L. The 90% distillation temperature of the hydrocracked kerosene base material is 272 ° C.

(Comparative Example 6)
A desulfurized kerosene (DK) produced by hydrotreating a raw oil obtained by mixing 30 vol% catalytically cracked light diesel oil (HVN) with straight-run kerosene (KERO) was used as a kerosene base material. The kerosene composition of Comparative Example 6 was prepared by mixing the kerosene base material and commercial kerosene at a ratio of 50% by volume and 50% by volume, respectively. The operating conditions of the hydrorefining treatment are: the pressure is 5 MPa, the temperature is 300 ° C., the LHSV is 7 h ⁻¹ , the hydrogen / feed oil ratio is 90 nL / L, and the chemical hydrogen consumption is 40 Nm ³ / kL.

  Tables 2 to 4 show the analysis results of the kerosene compositions obtained in the respective Examples and Comparative Examples by two-dimensional gas chromatography, and Tables 5 to 7 show the properties of the kerosene compositions. Regarding the peroxide value, the peroxide value of the kerosene composition after standing for 30 days at a temperature of 43 ° C., the peroxide value of the kerosene composition after standing for 2 hours at a temperature of 120 ° C., and before the standing The peroxide value of the kerosene composition was measured.

  The evaluation result by the stove combustion test of the kerosene composition obtained by each Example and the comparative example is shown to Tables 8-11. In Tables 8 to 11, “core” indicates a core-type stove, and “fan” indicates a fan heater. “OK” indicates that the stove combustion test was passed, and “NG” indicates that the stove combustion test was not passed.

  Tables 12 and 13 show the evaluation results of the kerosene compositions obtained in each Example and Comparative Example by the low temperature startability test. In Tables 12 and 13, when the cell start time is 10 seconds or less and the arrival time at 3000 rpm is 10 seconds or less, the low temperature startability test is passed, and the arrival time at 3000 rpm is 8 seconds or less. Was passed (excellent). On the other hand, when the cell start time was longer than 10 seconds, or when the 3000 rpm arrival time was longer than 10 seconds, or the engine speed could not reach 3000 rpm, the low temperature startability test was rejected.

  The properties of the kerosene compositions shown in Tables 5 to 7, and the peroxide value of the kerosene composition after standing for 30 days at a temperature of 43 ° C. is 1 ppm or less and the excess of the kerosene composition after standing for 2 hours at a temperature of 120 ° C. The storage stability of Examples and Comparative Examples having an oxide value of 30 ppm or less was regarded as “good”. Among these, Examples and Comparative Examples in which the peroxide value of the kerosene composition after standing for 2 hours at a temperature of 120 ° C. was 30 ppm or less The storage stability of the example was defined as “excellent”. On the other hand, the peroxide value of the kerosene composition after standing at a temperature of 43 ° C. for 30 days is greater than 1 ppm, or the peroxide value of the kerosene composition after standing at a temperature of 120 ° C. for 2 hours is greater than 30 ppm. The storage stability of the product was defined as “bad”. In addition, in the evaluation results by the stove combustion test in Tables 8 to 11, the long-term flammability of the examples in which the overall evaluation is “OK” and the comparative example is “good”, and the long-term flammability of the comparative example of “NG” is “poor” " Furthermore, in Table 12 and Table 13, the low temperature startability of the Examples and Comparative Examples that passed the low temperature startability test was set as “good”, and those that passed (excellent) among them were set as “excellent” and did not pass. The thing was made "bad". For the examples in which both storage stability and low-temperature startability are “excellent” and long-term flammability is also “good”, the overall evaluation is passed (excellent), and either storage stability or low-temperature startability is selected. For an example in which one is “excellent”, the other is “good” and the long-term flammability is also “good”, the overall evaluation is passed, and at least storage stability, long-term flammability and low-temperature startability are at least. About the comparative example whose one item is "bad", comprehensive evaluation was set as the failure. Tables 14 and 15 summarize the overall evaluation.

The graph which plotted the value of a of Example 1-9 and Comparative Examples 1-6 and the value of b is shown in FIG. In FIG. 1, “◯” indicates that the overall evaluation is acceptable (excellent) or passed, and “□” indicates that the overall evaluation is unacceptable. In FIG. 1, the hatched range is a range described in claim 1 of the present application, that is, a range that satisfies the following conditions.
15.000 ≦ a ≦ 29.000 and 1.600 ≦ b ≦ 4.500.

  From FIG. 1, the kerosene composition satisfying 15.000 ≦ a ≦ 29.000 and 1.600 ≦ b ≦ 4.500 has excellent storage stability and allows the heating equipment to be stably operated over a long period of time. It can be seen that the low temperature startability of the internal combustion engine can be improved.

Claims (11)

A method for producing a kerosene composition having the following steps,
In the kerosene composition obtained, the ratio (mass%) of the aromatic content to the sum of the saturated and aromatic components consisting of paraffin and naphthene is a, and 2 to the total of the saturated and aromatic content consisting of paraffin and naphthene. When the total value of the ratio (mass%) of the ratio of ring aromatics (0.5%), the ratio (mass%) of the ratio of bicyclic naphthenes, and the ratio (mass%) of tricyclic naphthenes is defined as b,
Satisfying 15.000 ≦ a ≦ 29.000 and 1.600 ≦ b ≦ 4.500 ,
As a process, a raw material oil obtained by mixing a kerosene fraction obtained by catalytic cracking light diesel oil (HVN) or an oil sand-derived kerosene fraction with a straight-run kerosene (KERO) is brought into contact with a catalyst bed formed using a hydrorefining catalyst to produce hydrogen A process of obtaining a kerosene base material by chemical purification treatment;
Using the kerosene base material obtained, preparing a kerosene composition,
The straight-run kerosene used when obtaining the kerosene base material satisfies the following properties (a) to (d), and the catalytically decomposed light gas oil satisfies the following properties (e) to (g):
In the feedstock inlet for the hydrorefining process,
The hydrogen pressure is 2 MPa or more and 10 MPa or less,
LHSV is 2h- ¹ or more and 15h- ¹ or less,
The reaction temperature is 200 ° C. or higher and 360 ° C. or lower,
A method for producing a kerosene composition, wherein a hydrorefining treatment is performed at a hydrogen / raw oil ratio of 50 nL / L to 500 nL / L.
(A) 95% distillation temperature distilled from the atmospheric distillation apparatus in the straight-run kerosene is 200 ° C. or higher and 280 ° C. or lower,
(B) the density of the straight run kerosene 0.750 g / cm ³ or more 0.850 g / cm ³ or less,
(C) The sulfur content of the straight-run kerosene is 0.001% by mass or more and 0.8% by mass or less,
(D) the straight-run kerosene has a cetane index of 47.5 or more,
(E) 95% distillation temperature distilled from the catalytic cracking device in the catalytic cracking light diesel oil is 180 ° C. or higher and 270 ° C. or lower,
(F) the density of the catalytic cracking light gas oil is 0.750 g / cm ³ or more 0.900 g / cm ³ or less,
(G) The sulfur content of the catalytically cracked light gas oil is 0.001% by mass or more and 0.08% by mass or less. Oil sand synthetic crude oil containing one or more selected from the group consisting of premium Arabian synthetic, Sancor oil sand blend A, and cinque sweet blend is passed through an atmospheric distillation apparatus. The method for producing a kerosene composition according to claim 1, which is a kerosene fraction obtained in the above manner. A method for producing a kerosene composition having the following steps,
In the kerosene composition obtained, the ratio (mass%) of the aromatic content to the sum of the saturated and aromatic components consisting of paraffin and naphthene is a, and 2 to the total of the saturated and aromatic content consisting of paraffin and naphthene. When the total value of the ratio (mass%) of the ratio of ring aromatics (0.5%), the ratio (mass%) of the ratio of bicyclic naphthenes, and the ratio (mass%) of tricyclic naphthenes is defined as b,
Satisfying 15.000 ≦ a ≦ 29.000 and 1.600 ≦ b ≦ 4.500,
A catalyst bed formed by using a hydrocracking catalyst as a process, a heavy oil oil (HGO), a vacuum heavy gas oil (VGO) or a mixture thereof mixed with a catalytic cracking light oil (LCO). Hydrocracking by contacting with to obtain a kerosene base material,
Using the kerosene base material obtained, preparing a kerosene composition,
When the kerosene base material is obtained, the heavy gas oil and the vacuum heavy gas oil have the following properties (a) to (c), and the catalytically decomposed light gas oil has the following properties (d) to (g). Meet,
In the feedstock inlet for the hydrocracking treatment,
A hydrogen pressure of 3 MPa to 20 MPa,
LHSV 0.1h ^-1 More than 10h ^-1 Less than,
The reaction temperature is 300 ° C. or more and 450 ° C. or less,
A method for producing a kerosene composition, wherein a hydrocracking treatment is performed at a hydrogen / raw oil ratio of 300 nL / L to 2000 nL / L.
(A) 95% distillation temperature distilled from the atmospheric distillation apparatus or the vacuum distillation apparatus in the heavy gas oil and the vacuum heavy gas oil is 400 ° C. or more and 600 ° C. or less,
(B) The density of the heavy gas oil and the vacuum heavy gas oil is 0.800 g / cm. ³ 1.000 g / cm ³ Less than,
(C) The sulfur content of the heavy gas oil and the vacuum heavy gas oil is 1.0 mass% or more and 3.0 mass% or less,
(D) 90% distillation temperature of distilling from the catalytic cracking device in the catalytic cracking light diesel oil is 280 ° C or higher and 390 ° C or lower,
(E) Density of the catalytic cracked light diesel oil is 0.800 g / cm ³ 1.000 g / cm ³ Less than,
(F) The catalytically cracked light gas oil has a sulfur content of 0.1% by mass or more and 0.8% by mass or less,
(G) The catalytically decomposed light gas oil has a cetane index of 24 or more. In the kerosene composition obtained, the ratio (mass%) of the aromatic content to the sum of the saturated and aromatic components consisting of paraffin and naphthene is a, and 2 to the total of the saturated and aromatic content consisting of paraffin and naphthene. When the total value of the ratio (mass%) of the ratio of ring aromatics (0.5%), the ratio (mass%) of the ratio of bicyclic naphthenes, and the ratio (mass%) of tricyclic naphthenes is defined as b,
The manufacturing method of the kerosene composition of any one of Claims 1-3 which satisfy | fills 18.000 <= a <= 29.000 and 1.600 <= b <= 3.640. In the kerosene composition obtained, the ratio (mass%) of the aromatic content to the sum of the saturated and aromatic components consisting of paraffin and naphthene is a, and 2 to the total of the saturated and aromatic content consisting of paraffin and naphthene. When the total value of the ratio (mass%) of the ratio of ring aromatics (0.5%), the ratio (mass%) of the ratio of bicyclic naphthenes, and the ratio (mass%) of tricyclic naphthenes is defined as b,
The manufacturing method of the kerosene composition of any one of Claims 1-3 which satisfy | fills 23.730 <= a <= 29.000 and 1.600 <= b <= 3.640. 1 aromatic ratio of in the aromatic content of the resulting kerosene composition, the total of the saturated component and aromatic component consists of paraffin and naphthenic is 29 wt% or less 11% by mass or more, according to claim 1 The manufacturing method of the kerosene composition of any one of -5 . Kerosene composition obtained, the proportion of the naphthene content of 2 rings in the saturated components, based on the sum of saturates and aromatics content consisting paraffins and naphthenes, less than 12 mass% 1 mass% or more, claim The manufacturing method of the kerosene composition of any one of 1-6 . The obtained kerosene composition has a ratio of tricyclic naphthene in the saturated content of 1% by mass or less with respect to the total of saturated and aromatic components composed of paraffin and naphthene . The manufacturing method of the kerosene composition of any one . Resulting kerosene composition, the proportion of the indane and tetralin compounds in the aromatic content, the total of the saturated component and aromatic component consists of paraffin and naphthenes, less than 10 mass% 1 mass% or more, wherein Item 9. A method for producing a kerosene composition according to any one of Items 1 to 8 . The manufacturing method of the kerosene composition of any one of Claims 1-9 whose smoke point of the kerosene composition obtained is 21 mm or more and less than 50 mm. The resulting kerosene composition is
The density is 0.75 g / cm ³ or more and 0.85 g / cm ³ or less,
The boiling range is 140 ° C. or more and 300 ° C. or less,
95% distillation temperature is 220 ° C. or higher and 270 ° C. or lower,
Sulfur content is 80 mass ppm or less,
The peroxide value is 1 ppm or less,
The nitrogen content is 1 mass ppm or less,
The kinematic viscosity at 30 ° C. is 0.9 mm ² / s to 1.7 mm ² / s,
Saybolt color is +25 or more,
Copper plate corrosion is 1 or less,
The flash point is 40 ° C or higher,
The method for producing a kerosene composition according to any one of claims 1 to 10 , wherein the cetane index is 45 or more.