JP4948003B2 - kerosene - Google Patents

Description

  The present invention relates to kerosene, and more particularly to kerosene that is suitably used in heating equipment such as an oil stove and an oil fan heater, a fuel reforming fuel cell, and the like.

While interest in environmental issues is socially increasing, in the field of indoor heating equipment, techniques for reducing odorous substances (such as hydrocarbons) discharged from the heating equipment are being studied. As a method for reducing odorous substances, improvement of a combustion part of a heating device, installation of an exhaust gas purification device, and the like have been proposed (see, for example, Patent Document 1).
On the other hand, it has been reported that if kerosene with poor stability is used over a long period of time, normal combustion is less likely to occur, which may cause a reduction in fuel consumption rate and further cause a malfunction of the apparatus (for example, see Non-Patent Document 1). ). If normal combustion is not performed due to clogging of the carburetor, the exhaust gas deteriorates or the odor becomes stronger. From the viewpoint of reducing exhaust gas and odorous substances, heat and oxygen in the vaporizer etc. It is desirable to use stable kerosene that does not deteriorate.
Furthermore, in a fuel reforming type fuel cell or the like, when troubles such as clogging of the carburetor occur, hydrogen cannot be stably produced, and the system cannot operate normally.
Japanese Patent Publication No.59-16814 Shinichiro Uchida, “PETROTECH”, Petroleum Institute, 1994, Vol. 17, No. 11, p. 37-42

General methods for evaluating the stability of kerosene include methods based on indices such as hue, olefin content, peroxide value, and the like. However, such an evaluation method is not always sufficient in terms of accuracy. Even with kerosene that is evaluated as having good stability based on the above index, the operation of the hydrogen production system in a heating device or a fuel reforming fuel cell may become unstable. This is because kerosene deteriorates due to heat and oxygen at the vaporizer parts such as the vaporization nozzle and vaporization cylinder surface, and tar is generated and deposited by condensation polymerization, etc., and normal operating conditions cannot be obtained. Conceivable.
The present invention has been made in view of such circumstances, suppresses the generation of tar and the like in the vaporizer portion, etc., and stably operates a hydrogen production system in a heating device or a fuel reforming fuel cell over a long period of time. It aims at providing kerosene which can be done.

  In order to achieve the above object, the present inventors first examined a kerosene evaluation method for stably operating a hydrogen production system in a heating device or a fuel reforming fuel cell. As a result, it was found that an exothermic peak at 390 ° C. or higher measured under a specific condition using a high-pressure differential scanning calorimeter is suitable as an indicator for evaluating the characteristics of kerosene. And when the kerosene whose exothermic peak at 390 ° C. or higher is less than a specific ratio with respect to the total exothermic peak is used for a hydrogen production system in a heating device or a fuel reforming fuel cell, the above problem is solved. The headline and the present invention were completed.

That is, according to the present invention, the area of the exothermic peak at 390 ° C. or higher when the temperature is increased from 50 ° C. to 500 ° C. at 20 ° C./min in a 4 MPa air atmosphere is measured using a high-pressure differential scanning calorimeter. , 5% or less of the area of all the exothermic peak, the sulfur content is 5 ppm by mass or less, an aromatic content of 20% by volume, density at 15 ℃ is 740kg / ^{m 3} or more 750.9kg / ^{m 3} or less, distillation properties The initial boiling point is 140 ° C. or higher, the 50% by volume distillation temperature is 180 ° C. or higher and 230 ° C. or lower, the end point is 300 ° C. or lower, the flash point is 40 ° C. or higher, and the kinematic viscosity at 30 ° C. is 1.0 mm ² / s or higher. .7mm ² / s or less, the smoke point above 21 mm, and peroxide value relates kerosene, characterized in that not more than 1 mass ppm.
According to the kerosene having the above-mentioned properties of the present invention, the tar generation suppression and fuel consumption are balanced at a high level by setting the area of the exothermic peak at 390 ° C. or higher to 5 % or less of the total exothermic peak area . Since both are well balanced, it becomes possible to stably operate a hydrogen production system in a heating device or a fuel reforming fuel cell over a long period of time.

Particularly in the present invention, as described above, aromatic content, initial boiling point, final point and 50 vol% distillation temperature in distillation characteristics, pull the fire point, sulfur content, density at 1 5 ° C., dynamic at 30 ° C. When the viscosity, smoke point, and peroxide value satisfy the above specific conditions, the fuel consumption rate of kerosene can be improved, and the stability, flammability, safety, heating equipment and fuel reforming fuel can be improved. Compatibility with the hydrogen production system in the battery can be improved. Therefore, by using such kerosene in a hydrogen production system for heating equipment and fuel reforming fuel cells, it is possible to suppress the production of tar and the like in the carburetor part, improve combustibility, reduce odorous substance emissions, Reduction of the load on the hydrogen production system in the fuel reforming fuel cell can be realized, and as a result, the hydrogen production system in the heating device and the fuel reforming fuel cell can be more stably operated.

In addition, the present invention uses a high-pressure differential scanning calorimeter to measure an exothermic peak when the temperature of kerosene is raised from 50 ° C. to 500 ° C. at 20 ° C./min in an atmosphere of 4 MPa, and at 390 ° C. or higher. 5% area of the exothermic peak relative to the area of all exothermic peak below, a sulfur content of 5 ppm by mass or less, an aromatic content of 20% by volume, density at 15 ℃ is 740kg / ^{m 3} or more 750.9kg / ^{m 3} Hereinafter , the initial boiling point in distillation properties is 140 ° C. or higher, the 50% by volume distillation temperature is 180 ° C. or higher and 230 ° C. or lower, the end point is 300 ° C. or lower, the flash point is 40 ° C. or higher, and the kinematic viscosity at 30 ° C. is 1.0 mm ^2. / s or 1.7 mm ² / s or less, the smoke point above 21 mm, and peroxide value regarding selection method kerosene, characterized in that selecting the kerosene is below 1 mass ppm.
Thus, the ratio of the area of the exothermic peak above 390 ° C. is measured, and the ratio is 5 % or less with respect to the area of the total exothermic peak, and the kerosene having the above properties is selected, thereby heating It is possible to easily and reliably obtain kerosene capable of stable operation of the hydrogen production system in equipment and fuel reforming fuel cells.

  Since the kerosene of the present invention has sufficiently high stability and can suppress the generation of tar and the like in the vaporizer portion, etc., the kerosene is used for a hydrogen production system in a heating device or a fuel reforming fuel cell. This makes it possible to perform stable operation over a long period of time.

Hereinafter, preferred embodiments of the present invention will be described in detail.
The ratio of the exothermic peak at 390 ° C. or higher of the kerosene of the present invention needs to be 10% or less, preferably 8% or less, more preferably 5% or less. When the ratio of the exothermic peak at 390 ° C. or higher is larger than 10%, tar or the like is likely to be generated in the vaporizer portion and the like, and as a result, the fuel consumption rate is lowered after the long-term operation is performed, and combustion failure is likely to occur. System troubles such as an increase in outlet pressure of the fuel delivery pump are likely to occur.

  The ratio of the exothermic peak at 390 ° C. or higher referred to in the present invention is measured using a high-pressure differential scanning calorimeter (hereinafter also referred to as “high-pressure DSC”). More specifically, the sample is introduced into a DSC pressure cell (for example, manufactured by Metradred), and the temperature is raised from 50 ° C. to 500 ° C. at 20 ° C./min in a 4 MPa air atmosphere. A correlation curve with temperature is obtained. The ratio of the exothermic peak at 390 ° C. or higher is determined based on the area of the exothermic peak that appears at 390 ° C. or higher in the correlation curve and the ratio of the area of the total exothermic peak.

  FIG. 1 is a graph showing an example of a correlation curve between the calorific value and temperature measured using a high-pressure DSC, and shows the measurement results for kerosene in Example 1 described later. In FIG. 1, the vertical axis represents the amount of heat generated, and the horizontal axis represents the temperature. By calculating the ratio of the area of the exothermic peak at 390 ° C or higher to the area of the total exothermic peak at the vertical stripes, and selecting kerosene based on the ratio of the exothermic peak at 390 ° C or higher, heating equipment and fuel reforming A kerosene capable of stably operating a hydrogen production system in a fuel cell can be obtained easily and reliably.

When preparing the kerosene of this invention, 1 type, or 2 or more types of kerosene base materials can be used. In this case, the base material is selected and the blending amount is adjusted so that the ratio of the exothermic peak at 390 ° C. or higher of the prepared composition is 10% or lower.
In addition, even if the ratio of the exothermic peak at 390 ° C. or higher of the kerosene after adjustment is 10% or less, a base material having a ratio of the exothermic peak at 390 ° C. or higher of greater than 10% is included in the kerosene composition. Good. On the other hand, when the ratio of the exothermic peak at 390 ° C. or higher is measured in advance for the base material, and the base material with the ratio of the exothermic peak at 390 ° C. or higher is selected to be 10% or less, the desired characteristics are obtained. Kerosene having the above can be obtained efficiently and reliably.

  Specific examples of the kerosene base material include hydrodesulfurized kerosene obtained by hydrorefining straight-run kerosene obtained from a crude oil atmospheric distillation apparatus, straight-run heavy oil obtained from an atmospheric distillation apparatus, Hydrorefining kerosene obtained by hydrorefining a vacuum gas oil fraction obtained by treating the residual oil with a vacuum distillation unit, hydrocracked kerosene obtained by hydrocracking the vacuum gas oil fraction, vacuum gas oil fraction or desulfurization Catalytic cracked kerosene obtained by catalytic cracking of heavy oil, pyrolysis kerosene obtained by pyrolyzing straight-run heavy oil, hydrodesulfurized kerosene obtained by hydrotreating pyrolysis kerosene, and residual oil are hydrogenated Ultra-low sulfur kerosene, straight-run kerosene, or hydrogenation obtained by deep hydrotreating using hydrodesulfurized kerosene, straight-run kerosene and / or hydrorefined kerosene obtained by refining in the presence of a hydrogenation catalyst Normal paraffin by extraction of desulfurized kerosene or hydrorefined kerosene Demineralized paraffin kerosene, which is a residue from which the hydrogen content has been removed, a gas oil fraction of GTL (Gas to Liquids) obtained by FT (Fischer-Tropsch) synthesis after decomposing natural gas into carbon monoxide and hydrogen, and And / or a substrate such as a hydrocracked product thereof.

  Among these kerosene base materials, hydrodesulfurized kerosene, straight-run kerosene and / or hydrorefined kerosene obtained by hydrorefining straight-run kerosene obtained from crude oil atmospheric distillation equipment is used as a raw material. GTL (Gas to Liquids) obtained by FT (Fischer-Tropsch) synthesis after decomposing ultra-low sulfur kerosene, natural gas, etc. obtained by deep hydrotreating in the presence of a catalyst into carbon monoxide and hydrogen A kerosene fraction and / or a hydrocracked product thereof is preferred, and a gas oil fraction of GTL (Gas to Liquids) obtained by FT (Fischer-Tropsch) synthesis after cracking natural gas or the like into carbon monoxide and hydrogen, and The hydrocracked product thereof is most preferred.

The hydrorefining conditions for the kerosene base material are not particularly limited as long as kerosene having predetermined properties is obtained, but the reaction temperature is 100 to 370 ° C., the hydrogen pressure is 0.5 to 10 MPa in the presence of the hydrogenation catalyst. , LHSV 0.1 to 10 h ⁻¹ , hydrogen / oil ratio 10 to 800 NL / L are preferable.

  The hydrogenation catalyst is not particularly limited, and examples thereof include a hydrogenation active metal supported on a porous carrier. An inorganic oxide is preferably used as the porous carrier. Specific examples of the inorganic oxide include alumina, titania, zirconia, boria, silica, and zeolite. Among these, at least one of titania, zirconia, boria, and silica is composed of alumina, particularly silica. -A support containing alumina or zeolite is preferably used in the present invention.

  The active metal of the catalyst used for the hydrotreatment is preferably at least one metal selected from Group 6 and / or Group 8 metals of the Periodic Table. More preferably, it is at least one selected from Ru, Rd, Ir, Pd, Pt, Ni, Co, Mo and W. The active metal may be a combination of these metals. For example, Pt—Pd, Pt—Rh, Pt—Ru, Ir—Pd, Ir—Rh, Ir—Ru, Pt—Pd—Rh, Pt—Rh— A combination of Ru, Ir—Pd—Rh, Ir—Rh—Ru, Co—Mo, Ni—Mo, Ni—W, or the like can be employed. Specifically, Pd, Pt, Pt—Pd, Co—Mo, Ni—Mo, and Ni—W are preferably used.

  The kerosene of the present invention may contain various additives in addition to the kerosene base as necessary. Additives include antioxidants such as phenolic and amine compounds, metal deactivators such as Schiff and thioamide compounds, surface ignition agents such as organophosphorus compounds, succinic acid amides, polyalkylamines, and polyethers. Detergents such as amines, antifreezing agents such as polyhydric alcohols and ethers thereof, alkali metal salts and alkaline earth metal salts of organic acids, sulfates of higher alcohols, auxiliary combustors such as 1-methoxy-2-acetoxypropane , An anionic surfactant, a cationic surfactant, an antistatic agent such as an amphoteric surfactant, a coloring agent such as an azo dye, and a discriminating agent such as coumarin. These fuel oil additives can be used alone or in combination of two or more. The addition amount of these fuel oil additives is arbitrary, but the total addition amount is preferably 0.5% by mass or less, more preferably 0.05% by mass or less, with respect to the total amount of kerosene.

  As said additive, what was synthesize | combined according to the conventional method may be used, and a commercially available additive may be used. In addition, the additive currently marketed may have diluted the active ingredient which contributes to the effect which the additive aimed at with the appropriate solvent. When using a commercially available additive in which the active ingredient is diluted, it is preferable to add the commercially available additive so that the content of the active ingredient in kerosene falls within the above-mentioned range.

The other properties of the kerosene of the present invention are not particularly limited as long as the exothermic peak at 390 ° C. or higher is 10% or less of the total exothermic peak, but preferably has the following properties.
The initial boiling point is preferably 140 ° C. or higher, more preferably 143 ° C. or higher, and further preferably 145 ° C. or higher. When the initial boiling point is less than 140 ° C., it is not preferable because there is an influence on safety due to a decrease in flash point.
The end point is preferably 300 ° C. or lower, and more preferably 290 ° C. or lower. If the end point exceeds 300 ° C., soot is likely to occur during ignition.
The 30 vol% distillation temperature (T30) is preferably 170 ° C or higher, more preferably 175 ° C or higher, and further preferably 180 ° C or higher. When T30 is less than 170 ° C., it is not preferable from the viewpoint of heat generation. On the other hand, from the viewpoint of ignitability at low temperatures, the temperature is preferably 210 ° C or lower, more preferably 205 ° C or lower, and further preferably 200 ° C or lower.

The 50 vol% distillation temperature (T50) is preferably 180 ° C or higher, more preferably 185 ° C or higher, and further preferably 190 ° C or higher. When T50 is less than 180 ° C., the fuel consumption rate tends to be insufficient. On the other hand, from the viewpoint of combustibility, it is preferably 230 ° C. or lower, and more preferably 225 ° C. or lower.
The 70 vol% distillation temperature (T70) is preferably 190 ° C or higher, more preferably 195 ° C or higher, from the viewpoint of the amount of heat generated. On the other hand, from the viewpoint of combustibility, it is preferably 250 ° C. or lower, and more preferably 245 ° C. or lower.
The 95% by volume distillation temperature (T95) is preferably 270 ° C. or lower, more preferably 268 ° C. or lower, from the viewpoint of combustibility.

  Here, the initial boiling point, T30, T50, T70, T95, and end point mean values measured by JIS K2254 “Petroleum products—distillation test method—atmospheric pressure distillation test method”, respectively. The initial boiling point by gas chromatographic distillation means the initial boiling point measured by JIS K2254 “Petroleum products—Distillation test method—Gas chromatographic distillation test method”.

  The flash point of the kerosene of the present invention is preferably 40 ° C. or higher, and more preferably 41 ° C. or higher. When the flash point is less than 40 ° C., it is not preferable from the viewpoint of handling safety. Note that the flash point here means a value measured by a closed tag type of JIS K2265 “Crude oil and petroleum products—flash point test method”.

  The sulfur content of the kerosene of the present invention is preferably 10 ppm by mass or less, more preferably 5 ppm by mass or less, and further preferably 1 ppm by mass or less. As the sulfur content increases, the odor tends to become stronger. In addition, the sulfur oxides in the combustion exhaust gas are suppressed, and the life of the exhaust gas aftertreatment catalyst installed in the heating equipment is prolonged. It is preferable not to exceed 10 ppm by mass. The sulfur content in the present invention means a value measured by JIS K2541 “Sulfur content test method”.

The aromatic content of the kerosene of the present invention is preferably 25% by volume or less, and more preferably 20% by volume or less from the viewpoint of combustibility. In addition, aromatic content here means content of the total aromatic content measured by Petroleum Institute method JPI-5S-49-97 "petroleum product-hydrocarbon type test method-high performance liquid chromatograph". .
Of the aromatic components, the aromatic components having two or more rings are preferably 1.5% by volume or less, more preferably 1.0% by volume or less, and 0.5% by volume or less. More preferably it is. When the aromatic content of two or more rings exceeds 1.5% by volume, the combustibility is lowered or the storage stability is lowered.
In addition, the aromatic component more than two rings here means the bicyclic aromatic component measured by Petroleum Institute method JPI-5S-49-97 "petroleum product-hydrocarbon type test method-high performance liquid chromatograph" and Means the sum of the aromatic content of three or more rings.

Density at 15 ℃ kerosene invention, 740Kg / ^{m 3} or more, preferably 820 kg / ^{m 3} or less, 745Kg / ^{m 3} or more, more preferably 810Kg / ^{m 3} or less. When the density at 15 ° C. is less than 740 Kg / m ³ , it is not preferable from the viewpoint of the fuel consumption rate, and when it exceeds 820 Kg / m ³ , it is not preferable from the viewpoint of combustibility. Here, the density at 15 ° C. means a value measured according to JIS K2249 “Crude oil and petroleum products—density test method and density / mass / capacity conversion table”.

The kinematic viscosity of the kerosene of the present invention at 30 ° C. is preferably 1.0 mm ² / s or more and 1.7 mm ² / s or less, and is 1.1 mm ² / s or more and 1.6 mm ² / s or less. It is more preferable. When the kinematic viscosity at 30 ° C. is less than 1.0 mm ² / s, it is not preferable from the viewpoint of penetration into the core in the core type stove, while when it exceeds 1.7 mm ² / s, the core type is used. It is not preferable from the standpoint of preventing exudation from the core due to residual heat after the stove is extinguished. Here, the kinematic viscosity at 30 ° C. means a value measured by JIS K2283 “Crude oil and petroleum products—Kinematic viscosity test method”.

  The smoke point of the kerosene of the present invention is preferably 21 mm or more, more preferably 23 mm or more. When the smoke point is less than 21 mm, it is not preferable from the viewpoint of preventing soot generation and incomplete combustion in the core type stove. The smoke point here means a value measured by JIS K2537 “Petroleum products—aviation turbine fuel oil and kerosene—smoke point test method”.

  The peroxide value of the kerosene of the present invention is preferably 1 mass ppm or less. When the peroxide value exceeds 1 mass ppm, there is a concern about poor combustion due to the generation of peroxide. The peroxide value referred to here means a value measured by the Petroleum Institute method JPI-5S-46-96 “Test method for peroxide value of kerosene”.

  The saturated content of the kerosene of the present invention is preferably 68% by volume or more, more preferably 72% by volume or more, and further preferably 75% by volume or more from the viewpoint of combustibility. In addition, saturated content here means content of the saturated hydrocarbon measured by Petroleum Institute method JPI-5S-49-97 "petroleum product-hydrocarbon type test method-high performance liquid chromatograph".

  From the viewpoint of storage stability, the olefin content of the kerosene of the present invention is preferably 5% by volume or less, more preferably 3% by volume or less, and still more preferably 1% by volume or less. The olefin content here means the content of olefinic hydrocarbons measured by the Petroleum Institute method JPI-5S-49-97 “Petroleum products—Hydrocarbon type test method—High performance liquid chromatograph”.

  The Saybolt color of the kerosene of the present invention is preferably +25 or more in consideration of safety effects such as impurity identification. The Saybolt color here means a value measured by the Saybolt color test method in JIS K2580 “Petroleum products-color test method”.

  The copper plate corrosion (50 ° C., 3 h) of the kerosene of the present invention is preferably 1 or less, and more preferably 1a. When the copper plate corrosion exceeds 1, the metal member may be corroded, which is not preferable. In addition, copper plate corrosion here means the value measured based on JISK2513 "Petroleum product-copper plate corrosion test method" (test temperature 50 degreeC, test time 3 hours).

  The kerosene of the present invention having the above properties has improved stability, odor reduction, flammability, combustibility, safety, and suitability for heating equipment and hydrogen production systems in fuel reforming fuel cells in a well-balanced manner. Therefore, it is possible to stably operate a hydrogen production system in a heating device or a fuel reforming fuel cell over a long period of time. Therefore, the kerosene of the present invention is very useful as a kerosene used in heating equipment such as an oil stove (for example, a core-type stove) and an oil fan heater and a hydrogen production system in a fuel reforming fuel cell.

  EXAMPLES Hereinafter, although this invention is demonstrated more concretely based on an Example and a comparative example, this invention is not limited to a following example at all.

<Kerose (1)>
An unrefined oil having a sulfur content of 1700 mass ppm, an initial boiling point of 163 ° C., and T95 = 242 ° C. using a cobalt-molybdenum supported alumina catalyst, a reaction temperature of 310 ° C., a hydrogen partial pressure of 3.6 MPa, LHSV 2.9 h ⁻¹ , hydrogen / Hydrogenation purification was performed under the condition of an oil ratio of 85 NL / L to obtain kerosene (1). The general properties of this kerosene (1) are shown in Table 1.

<Kerose (2)>
Hydrogenated refined oil having a sulfur content of 10 ppm by mass, an initial boiling point of 152 ° C., and T95 = 263 ° C. using a platinum-palladium-supported silica-alumina catalyst, reaction temperature of 200 ° C., hydrogen partial pressure of 5.0 MPa, LHSV 1.0 h ⁻¹ Then, hydrorefining was performed under the condition of a hydrogen / oil ratio of 200 NL / L to obtain kerosene (2). The general properties of this kerosene (2) are shown in Table 1.

<Kerose (3)>
Silica with FT wax (21 to 70 carbon atoms) as a raw material and 0.5% by mass of platinum supported
Hydrocracking was performed using a catalyst containing 60% by mass and 3% by mass of USY zeolite having an average particle size of 0.4 μm. First, the catalyst was prereduced at 345 ° C. and activated. Then, hydrocracking was performed under the conditions of a hydrogen partial pressure of 3 MPa, LHSV 2.0 h ⁻¹ , a hydrogen oil ratio of 520 NL / L, and a reaction temperature of 304 ° C., and the resulting oil was TBP distilled to obtain kerosene (3). . Table 1 shows the general properties of this kerosene (3).

<Comparison kerosene (1)>
A comparative kerosene (1) was obtained by hydrocracking a vacuum distilled light oil fraction of 340-580 ° C. using a zeolite catalyst at a reaction pressure of 10.5 MPa and a reaction temperature of 410 ° C. The general properties of this comparative kerosene (1) are shown in Table 1.

[Examples 1 to 3 and Comparative Example 1]
A vaporizer in which kerosene (1) to (3) and comparative kerosene (1) were fed at 1 g / min using a Shimadzu high-speed liquid chromatograph feeding unit LC-10AT and heated to 330 ° C. Was dropped from a nozzle having an inner diameter of 1 mm (entered 5 mm in the vaporizer).
The dropping for 10 hours per day was performed for 30 days, and the outlet pressure of the liquid feeding unit was compared with that at the start of dropping. In addition, it was set as the failure when the exit pressure became 10 MPa or more. The results are shown in Table 2.

From the results in Table 2, it can be seen that the clogging of the vaporizing nozzle can be suppressed by using the kerosene of Examples 1 to 3 according to the present invention.
On the other hand, in the case of Comparative Example 1, as shown in Table 2, the test was ended because the outlet pressure exceeded 10 MPa on the 12th day. When the nozzle was disassembled after the test, the inner tube was clogged with black material, suggesting that the fuel deteriorates in the vaporizer and that system failure is likely to occur.

It is a graph which shows an example of the correlation curve of the emitted-heat amount measured using high voltage | pressure DSC, and temperature.

Claims (2)

Is measured using a high pressure differential scanning calorimeter, under an air atmosphere at 4 MPa, the area of the area of the exothermic peak total exothermic peak at 390 ° C. or more when heated at 20 ° C. / min from 50 ° C. to 500 ° C. 5% for less, a sulfur content of 5 ppm by mass or less, an aromatic content of 20% by volume, density at 15 ℃ is 740kg / ^{m 3} or more 750.9kg / ^{m 3} or less, an initial boiling point in distillation characteristics are 140 ° C. The 50 vol% distillation temperature is 180 ° C. or higher and 230 ° C. or lower, the end point is 300 ° C. or lower, the flash point is 40 ° C. or higher, and the kinematic viscosity at 30 ° C. is 1.0 mm ² / s or higher and 1.7 mm ² / s or lower. A kerosene having a smoke point of 21 mm or more and a peroxide value of 1 mass ppm or less . Using a high-pressure differential scanning calorimeter, the exothermic peak was measured when the kerosene was heated from 50 ° C. to 500 ° C. at 20 ° C./min in an air atmosphere of 4 MPa, and the area of the exothermic peak at 390 ° C. or higher was all 5% of the area of the exothermic peak below, a sulfur content of 5 ppm by mass or less, an aromatic content of 20% by volume, density at 15 ℃ is 740kg / ^{m 3} or more 750.9kg / ^{m 3} or less, the first in the distillation properties The boiling point is 140 ° C or higher, the 50% by volume distillation temperature is 180 ° C or higher and 230 ° C or lower, the end point is 300 ° C or lower, the flash point is 40 ° C or higher, and the kinematic viscosity at 30 ° C is 1.0 mm ² / s or higher and 1.7 mm. ^2. A kerosene sorting method, wherein kerosene having a smoke point of 21 mm or more, a peroxide value of 1 mass ppm or less is selected.

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