JP4268495B2 - Kerosene composition and method for producing the same - Google Patents

Description

  The present invention relates to a kerosene composition. Specifically, the present invention relates to a kerosene composition used in heating equipment such as an oil stove and an oil fan heater.

  While interest in environmental issues is socially increasing, in the field of indoor heating equipment, technologies for reducing odorous substances (such as hydrocarbons) and pollutants (such as SOx) discharged from heating equipment are being studied. For example, 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, the use of kerosene made of, for example, n-paraffins and i-paraffins has been proposed as a fuel for heating equipment (see, for example, Patent Document 2).
Japanese Patent Publication No.59-16814 JP-A-63-150380

  However, the above-mentioned conventional kerosene is not sufficient as a fuel for existing heating equipment that has not been improved in the combustion section or fitted with an exhaust gas purification device. In addition, even when conventional kerosene is used in a heating device having an improved combustion section or an exhaust gas purification device, it is not always easy to maintain clean combustion over a long period of time.

  This invention is made | formed in view of such a situation, and it aims at providing the kerosene composition which can drive | operate a heating apparatus stably over a long period of time, and its manufacturing method.

  As a result of intensive studies to achieve the above object, the inventors of the present invention are kerosene base materials that have been subjected to a specific deep hydrogenation treatment, and include distillation properties, naphthene content, total aromatic content, two or more rings. It was found that the above-mentioned problems can be solved when a kerosene composition satisfying specific conditions of the aromatic content, naphthene content / total aromatic content volume ratio, sulfur content, and density is used as a fuel for heating equipment. The invention has been completed.

That is, the kerosene composition of the present invention comprises a raw material oil containing at least one selected from unrefined oil and hydrorefined oil in the presence of a hydrogenation catalyst, reaction temperature of 100 to 350 ° C., hydrogen pressure of 1 to 6 MPa, liquid A kerosene base material obtained by deep hydrogenation treatment at a space velocity of 0.1 to 4 h ⁻¹ and a hydrogen / oil ratio of 70 to 500 NL / L, having an initial boiling point of 140 ° C. or higher and an end point of 300 ° C. in distillation properties. Hereinafter, the 50 volume% distillation temperature is 200 to 230 ° C. , the 70 ° C. volume% distillation temperature is 220 to 250 ° C. , the naphthene content is 20 volume% or more, the total aromatic content is 15 volume% or less, and two or more rings. Kerosene base material having an aromatic content of 1% by volume or less, a volume ratio of naphthene / total aromatic content of 2.0 or more, a sulfur content of 10 mass ppm or less, and a density at 15 ° C. of 770 to 820 kg / m ^3. It is characterized by containing.

  In the present invention, raw oil is subjected to deep hydrotreating under specific conditions, distillation properties, naphthene content, total aromatic content, aromatic content of two or more rings, naphthene content / total aromatic content ratio, sulfur content, and A kerosene base material whose density satisfies a specific condition is obtained. The kerosene composition of the present invention contains the kerosene base material, which can drastically improve the combustibility of the kerosene composition and can maintain a high level of combustibility for a long period of time. it can. Moreover, the kerosene composition of the present invention is excellent in stability, flammability, safety, and adaptability to a combustion part of a heating device and an exhaust gas purification device. Therefore, by using the kerosene composition of the present invention for heating equipment, it becomes possible to improve fuel efficiency, reduce the emission of odorous substances and pollutants, reduce the load on the heating equipment, etc. It becomes possible to operate stably over a long period of time.

  The total aromatic content of the kerosene composition of the present invention is preferably 10% by volume or less.

  In addition, the raw oil used for the deep hydrogenation treatment preferably has an initial boiling point of 140 ° C. or higher and an end point of 310 ° C. or lower in the distillation properties.

In the method for producing a kerosene composition of the present invention, a raw material oil containing at least one selected from unrefined oil and hydrorefined oil is prepared in the presence of a hydrogenation catalyst at a reaction temperature of 100 to 350 ° C., a hydrogen pressure of 1 Deep hydrogenation treatment is performed at 6 MPa, LHSV 0.1 to 4 h ⁻¹ , hydrogen / oil ratio 70 to 500 NL / L. 200 to 230 ° C., a 70 ° C. vol% distillation temperature of 220 to 250 ° C., naphthene content of 20 vol% or more, a total aromatic content of 15% by volume or less, bicyclic or more aromatics content of 1% by volume or less And a step of obtaining a kerosene base material having a volume ratio of naphthene / total aromatic content of 2.0 or more, a sulfur content of 10 mass ppm or less, and a density at 15 ° C. of 770 to 820 kg / m ^3. To do.

  According to the said manufacturing method, the kerosene composition of this invention which can drive | operate a heating apparatus stably over a long period of time can be obtained easily and reliably.

  ADVANTAGE OF THE INVENTION According to this invention, it becomes possible to provide the kerosene composition which can drive a heating apparatus stably over a long period of time, and its manufacturing method.

  Hereinafter, preferred embodiments of the present invention will be described in detail.

(Kerosene base material)
The kerosene base material according to the present invention is obtained by subjecting a raw oil containing at least one selected from unrefined oil and hydrorefined oil to a specific deep hydrogenation treatment.

  Specific examples of unrefined oil and hydrorefined oil include straight-run kerosene obtained from a crude oil atmospheric distillation device, hydrodesulfurized kerosene obtained by hydrorefining straight-run kerosene, and atmospheric distillation device. Hydrocracked kerosene obtained by hydrorefining a vacuum gas oil fraction obtained by treating straight-run heavy oil and residual oil obtained from the above with a vacuum distillation unit, and hydrogenation obtained by hydrocracking a vacuum gas oil fraction Hydrogenation obtained by hydrocracking pyrolysis kerosene, pyrolysis kerosene obtained by thermal cracking of cracked kerosene, vacuum gas oil fraction or desulfurized heavy oil, catalytic cracked kerosene obtained by pyrolyzing heavy oil Examples include desulfurized kerosene and hydrodesulfurized kerosene obtained by hydrorefining residual oil. These feedstocks can be used alone or in combination of two or more.

  The raw material oil may be composed of only unrefined oil and / or hydrorefined oil as long as the obtained kerosene base material satisfies the conditions specified in the present invention, and further contains other components. May be. Other components include demineralized kerosene, which is a residue obtained by removing normal paraffin by extraction of straight-run kerosene, hydrodesulfurized kerosene, or hydrorefined kerosene, after decomposing natural gas into carbon monoxide and hydrogen. Examples include kerosene fractions of GTL (Gas to Liquids) obtained by FT (Fischer-Tropsch) synthesis and / or hydrocracked products thereof. When the raw material oil contains these components, the total amount of unrefined oil and hydrorefined oil is preferably 50% by volume or more, more preferably 60% by volume or more, and 70% by volume or more. More preferably it is.

  The distillation property of the raw material oil is not particularly limited, but the initial boiling point is preferably 140 ° C. or higher. The end point of the raw material oil is preferably 310 ° C. or lower, more preferably 305 ° C. or lower, and further preferably 300 ° C. or lower. By using the raw material oil having such distillation properties, the kerosene base material according to the present invention can be reliably obtained. Moreover, the higher desulfurization effect can be acquired because the distillation property of raw material oil satisfy | fills the said conditions.

The raw material oil is deeply hydrogenated under the conditions of a reaction temperature of 100 to 350 ° C., a hydrogen pressure of 1 to 6 MPa, a liquid space velocity of 0.1 to 4 h ⁻¹ , and a hydrogen / oil ratio of 70 to 500 NL / L.

  The reaction temperature in the deep hydrogenation treatment is 100 to 350 ° C, preferably 130 to 320 ° C. When the reaction temperature is less than 100 ° C., a sufficient hydrogenation reaction rate cannot be obtained. On the other hand, when the reaction temperature exceeds 350 ° C., the hydrogenation reaction becomes insufficient in terms of reaction equilibrium.

  The hydrogen pressure in the deep hydrogenation treatment is 1 to 6 MPa, preferably 2 to 6 MPa. The hydrogen / oil ratio is 70 to 500 NL / L, preferably 90 to 400 NL / L. When the hydrogen pressure is less than 1 MPa and the hydrogen / oil ratio is less than 70 NL / L, the effect of promoting the desulfurization reaction or hydrogenation reaction is insufficient. In addition, when the hydrogen pressure exceeds 6 MPa and when the hydrogen / oil ratio exceeds 500 NL / L, the manufacturing cost increases.

The liquid space velocity (Liquid Hourly Space Velocity, hereinafter referred to as “LHSV”) in the deep hydrogenation treatment is 0.1 to 4 h ⁻¹ , preferably 0.2 to 3 h ⁻¹ . A lower LHSV is advantageous for the reaction, but if it is less than 0.1 h ⁻¹ , a very large reaction column volume is required.

  The catalyst used for the deep hydrogenation treatment is not particularly limited, and examples thereof include a catalyst in which a hydrogenation active metal is 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, silica, and zeolite and an alumina is used. It is suitably used in the present invention.

  The active metal of the catalyst used for the deep hydrogenation treatment is preferably at least one metal selected from Group 6 and / or Group 8 metals in 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-Ru. , Ir-Pd-Rh, Ir-Rh-Ru, Co-Mo, Ni-Mo, Ni-W, and the like can be employed. Although the amount of active metal supported is not particularly limited, it is desirable that the total amount of metal is 0.1 to 30% by mass with respect to the catalyst mass.

  The catalyst is preferably used after pre-reduction treatment in a hydrogen or hydrogen sulfide stream. In general, when a gas containing hydrogen or hydrogen sulfide is circulated and heat of 200 ° C. or higher is applied according to a predetermined procedure, the active metal on the catalyst is reduced, and hydrogenation activity is exhibited.

  The kerosene base material according to the present invention obtained by the above-described deep hydrogenation treatment has a distillation property, naphthene content, total aromatic content, aromatic content of two or more rings, naphthene content / total aromatic content volume ratio, sulfur content. As well as the density, a specific condition is satisfied. Hereinafter, various properties of the kerosene base material will be described in detail.

(Distillation properties)
The initial distillation point in the distillation properties of the kerosene base material is 140 ° C. or higher, the end point is 300 ° C. or lower, and the 50 vol% distillation temperature is 190 to 230 ° C.

  The initial boiling point of the kerosene base material needs to be 140 ° C. or higher, preferably 143 ° C. or higher, and more preferably 145 ° C. or higher because of the influence on safety caused by the reduction of the flash point. On the other hand, the temperature is preferably 170 ° C. or lower, more preferably 165 ° C. or lower, from the viewpoint of maintaining ignition characteristics at low temperatures.

  The end point of the kerosene base material needs to be 300 ° C. or less, preferably 290 ° C. or less, and more preferably 280 ° C. or less. When the end point exceeds 300 ° C., soot is likely to be generated at the time of ignition, and when used in a core-type stove, tar tends to adhere to the core.

  The 50 vol% distillation temperature (hereinafter referred to as “T50”) of the kerosene base material is required to be 190 ° C. or higher, preferably 195 ° C. or higher, and more preferably 200 ° C. or higher. When T50 is less than 190 ° C., the fuel consumption rate deteriorates. On the other hand, from the viewpoint of combustibility, T50 needs to be 230 ° C. or lower, and is preferably 225 ° C. or lower.

  Other distillation properties of the kerosene base material are not particularly limited, but desirably satisfy the following properties.

  The 30% by volume distillation temperature (hereinafter referred to as “T30”) is preferably 170 ° C. or higher, more preferably 175 ° C. or higher, more preferably 180 ° C. or higher, from the viewpoints of odor reduction and heat generation during refueling. More preferably. On the other hand, from the viewpoint of ignitability at low temperatures, T30 is preferably 210 ° C. or lower, more preferably 205 ° C. or lower, and further preferably 200 ° C. or lower.

  The 70 vol% distillation temperature (hereinafter referred to as “T70”) is preferably 220 ° C. or higher, and more preferably 225 ° C. or higher, from the viewpoint of heat generation. On the other hand, from the viewpoint of combustibility, T70 is preferably 250 ° C. or lower, and more preferably 245 ° C. or lower.

  The 95% by volume distillation temperature (hereinafter referred to as “T95”) is preferably 270 ° C. or less, and more preferably 268 ° C. or less from the viewpoint of combustibility.

  The initial boiling point, T30, T50, T70, T95, and end point in the present invention mean values measured by JIS K 2254 “Petroleum products-distillation test method”, respectively.

(For naphthenic)
The naphthene content of the kerosene base material needs to be 20% by volume or more, preferably 25% by volume or more, and more preferably 28% by volume or more. When the naphthene content is less than 20% by volume, the amount of heat generated per unit capacity is insufficient.

  The naphthene content in the present invention refers to ASTM D 2425 (Standard Test Method for Hydrocarbon Types in Middle Distillates by Mass Spectrometry). .

(Aromatic content)
The total aromatic content of the kerosene base material is required to be 15% by volume or less, preferably 10% by volume or less, more preferably 8% by volume or less from the viewpoint of combustibility.

  The total aromatic content as used in the field of this invention means the value of the total aromatic content measured by Petroleum Institute method JPI-5S-49-97 "petroleum product-hydrocarbon type test method-high performance liquid chromatograph".

  In addition, the aromatic content of two or more rings in the total aromatic content needs to be 1% by volume or less, preferably 0.8% by volume or less, more preferably 0.5% by volume or less. . When the aromatic content of two or more rings exceeds 1% by volume, the flammability is significantly reduced.

  The term “bicyclic or higher aromatics” as used in the present invention refers to bicyclic aromatics and tricyclics measured by the Petroleum Institute method JPI-5S-49-97 “Petroleum products—hydrocarbon type test method—high performance liquid chromatograph”. This means the sum of aromatic content.

(Naphthene / total aromatic content ratio)
The volume ratio of the naphthene content / total aromatic content of the kerosene base material needs to be 2.0 or more, preferably 3.0 or more, from the viewpoint of the balance between the fuel consumption rate and the combustibility.

  The naphthene content and the total aromatic content here are the same contents as the above-mentioned naphthene content and the total aromatic content, respectively, and ASTM D2425 (Standard Test Method for Hydrocarbon Types in Middle Distillates by Mass Spectral Method). It means a value determined in accordance with 5S-49-97 “Petroleum Products—Hydrocarbon Type Test Method—High Performance Liquid Chromatograph”.

(Sulfur content)
The sulfur content of the kerosene base material must be 10 mass ppm or less from the viewpoint of sulfur oxide suppression in the combustion exhaust gas and the life of the exhaust gas aftertreatment catalyst attached to the heating equipment, Preferably it is 5 mass ppm or less, More preferably, it is 1 mass ppm or less.

  The sulfur content in the present invention means a value measured by JIS K 2541 “Sulfur content test method”.

(density)
Density at 15 ℃ kerosene base material, it is necessary in terms of the fuel consumption rate is 770 kg / ^{m 3} or more, preferably 780 kg / ^{m 3} or more. On the other hand, from the viewpoint of flammability, it must be at 820 kg / ^{m 3} or less, preferably 810Kg / ^{m 3} or less.
The density at 15 ° C. in the present invention is a value measured by JIS K2249 “Crude oil and petroleum products—density test method and density / mass / capacity conversion table”.

(Kinematic viscosity)
The kinematic viscosity of the kerosene base material is not particularly limited, but is preferably less than 1.7 mm ² / s at 30 ° C. from the viewpoint of penetration into the core of the core stove. On the other hand, it is desirable that it is 1.0 mm < ² > / s or more at 30 degreeC from the point of prevention of the seepage from the core by the residual heat after fire extinguishing in a core type stove.

  The kinematic viscosity at 30 ° C. in the present invention means a value measured by JIS K2283 “Crude oil and petroleum products—Kinematic viscosity test method”.

(Flash point)
The flash point of the kerosene base material is not particularly limited, but is preferably 40 ° C. or higher from the viewpoint of safety in handling.

  The flash point as used in the field of this invention means the value measured by the tag sealing type | formula of JISK2265 "Crude oil and petroleum products-Flash point test method."

(Smoke point)
The smoke point of the kerosene base material is not particularly limited, but is preferably 21 mm or more from the viewpoint of soot generation and incomplete combustion prevention in the core type stove.

  The smoke point as used in the field of this invention means the value measured by JISK2537 "Petroleum products-Aviation turbine fuel oil and kerosene-Smoke point test method".

(Saebold color)
The color of the kerosene base material is not particularly limited, but it is desirable that the Saybolt color be +25 or more in consideration of the influence on safety such as identification of impurities.

  The Saebold color here is a value measured by the Saebold color test method in JIS K2580 “Petroleum products-color test method”.

  The kerosene composition of the present invention may be composed only of the above-mentioned kerosene base material, and may contain various additives described later as necessary. In addition, when the kerosene composition of this invention contains an additive, it is preferable that the conditions prescribed | regulated about the kerosene base material are the whole composition.

  That is, the initial boiling point in the distillation properties of the kerosene composition is preferably 140 ° C. or higher, more preferably 143 ° C. or higher, and further preferably 145 ° C. or higher. The initial boiling point is preferably 170 ° C. or lower, more preferably 165 ° C. or lower. The end point of the kerosene composition is preferably 300 ° C. or lower, more preferably 290 ° C. or lower, and further preferably 280 ° C. or lower. Moreover, T50 of a kerosene composition becomes like this. Preferably it is 190 degreeC or more, More preferably, it is 195 degreeC or more, More preferably, it is 200 degreeC or more. The T50 is preferably 230 ° C. or lower, more preferably 225 ° C. or lower. Moreover, T30 of a kerosene composition becomes like this. Preferably it is 170 degreeC or more, More preferably, it is 175 degreeC or more, More preferably, it is 180 degreeC or more. The T30 is preferably 210 ° C. or lower, more preferably 205 ° C. or lower, and further preferably 200 ° C. or lower. Moreover, T70 of a kerosene composition becomes like this. Preferably it is 220 degreeC or more, More preferably, it is 225 degreeC or more. Moreover, the T70 is preferably 250 ° C. or lower, more preferably 245 ° C. or lower. Moreover, T95 of a kerosene composition becomes like this. Preferably it is 270 degrees C or less, More preferably, it is 268 degrees C or less.

  The naphthene content of the kerosene composition is preferably 20% by volume or more, more preferably 25% by volume or more, and still more preferably 28% by volume or more. The total aromatic content is preferably 15% by volume or less, more preferably 10% by volume or less, and still more preferably 8% by volume or less. The aromatic content of two or more rings in the total aromatic content is preferably 1% by volume or less, more preferably 0.8% by volume or less, and still more preferably 0.5% by volume or less. Further, the volume ratio of the naphthene content / total aromatic content of the kerosene base material is preferably 2.0 or more, and preferably 3.0 or more. The sulfur content of the kerosene composition 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.

The density of the kerosene composition at 15 ° C. is preferably 770 Kg / m ³ or more, more preferably 780 Kg / m ³ or more. The density is preferably 820 Kg / m ³ or less, more preferably 810 Kg / m ³ or less. Moreover, the kinematic viscosity at 30 ° C. of the kerosene composition is preferably 1.0 mm ² / s or more and less than 1.7 mm ² / s.

The flash point of the kerosene composition is preferably 40 ° C. or higher, and the smoke point is preferably 21 mm or higher. Furthermore, the kerosene composition preferably has a Saybolt color of +25 or more.
(Additive)
The kerosene composition of the present invention may be prepared by using a phenolic compound such as 2,6-di-tert-butyl-p-cresol and an amine such as N, N′-di-sec-butyl-p-phenylenediamine, if necessary. Antioxidants such as Schiff compounds, metal deactivators such as Schiff and thioamide compounds, surface igniters such as organophosphorus compounds, detergents and dispersants such as succinic amides, polyalkylamines and polyetheramines, polyvalent Anti-icing agent such as alcohol and its ether, alkali metal or alkaline earth metal salt of organic acid, sulfuric acid ester of higher alcohol, auxiliary combustor such as 1-methoxy-2-acetoxypropane, anionic surfactant, cationic interface One or a combination of known fuel oil additives such as activators, amphoteric surfactants and other antistatic agents, and azo dyes and other colorants May be added. The addition amount of these fuel oil additives is arbitrary, but the total addition amount is usually preferably 0.5% by mass or less, and more preferably 0.05% by mass or less.

  As the above-mentioned additive, one synthesized according to a conventional method may be used, or 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 the kerosene composition falls within the above range.

  The kerosene composition of the present invention having the above-described configuration has a well-balanced increase in flammability, flammability, safety, and suitability for heating equipment, and can stably operate the heating equipment for a long period of time. It is possible. Therefore, the kerosene composition of the present invention is very useful as a heating fuel composition used in heating equipment such as a petroleum stove (for example, a core-type stove) and a petroleum fan heater.

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

[Examples 1 to 3, Comparative Examples 1 to 4]
In Examples 1 to 3 and Comparative Examples 1 to 3, a crude oil or hydrorefined oil was hydrotreated under the conditions shown in Tables 1 and 2 to obtain a kerosene base material. Various properties of each kerosene base are shown in Tables 1 and 2.

  In Examples 1 and 2 and Comparative Examples 1 and 2, the obtained kerosene base material was directly used as a sample oil for the following tests. In Example 3 and Comparative Example 3, 20 mass ppm of phenolic antioxidant (2,6-di-tert-butyl-p-cresol) was added to the obtained kerosene base material, and the resulting kerosene composition was obtained. The product was used as sample oil. In Comparative Example 4, a hydrocracked GTL kerosene fraction obtained by FT synthesis was used as sample oil.

[Combustion test]
Next, a combustion test was performed using the sample oils of Examples 1 to 3 and Comparative Examples 1 to 4. Specifically, as heating equipment for testing, a core up-and-down stove (open type oil stove core type natural ventilation type, exhaust gas purification device, SX-E261Y made by Corona), and oil fan heater (open type oil stove vaporization type forced Ventilation type, no exhaust gas purification device, KD-F32C manufactured by Mitsubishi Electric) was filled with sample oil, ignition—5 hours of steady operation—extinguishing was taken as one cycle, and these steps were repeated 100 cycles.

  In this test, the THC (Total HydroCarbon) concentration after the first cycle (hereinafter referred to as “THC concentration 1”), the THC concentration after the 100th cycle (hereinafter referred to as “THC concentration 2”), and the SOx concentration. Was measured. Specifically, the exhaust gas from the heating equipment is collected using an X-tube conforming to the JIS S 3031 method from the extinction of each cycle until 30 seconds elapse, and the THC concentration in the exhaust gas or further The SOx concentration was measured. When measuring the THC concentrations 1 and 2 and the SOx concentration, FIA-510H manufactured by HORIBA, Ltd. and PG-200 series manufactured by HORIBA, respectively were used as analyzers. The obtained results are shown in Tables 3 and 4. The THC concentrations 1 and 2 in Tables 3 and 4 are relative values when the THC concentration 1 of Comparative Example 1 is 100. Similarly, the SOx concentrations in Tables 3 and 4 are relative values when the SOx concentration in Comparative Example 1 is 100. The THC concentrations 1 and 2 are indicators of odorous substance emissions, and the SOx concentration is an indicator of pollutant emissions.

  In this test, the fuel consumption rate in the first cycle (hereinafter referred to as “fuel consumption rate 1”) and the fuel consumption rate in the final cycle (hereinafter referred to as “fuel consumption rate 2”) were measured. Difference Δ (fuel consumption rate 1−fuel consumption rate 2). The obtained results are shown in Tables 3 and 4. The fuel consumption rates 1 and 2 are shown as relative values when the fuel consumption rate 1 of Comparative Example 1 is 100. The larger the value of the fuel consumption rate 1, the worse the fuel consumption. In addition, when the number of cycles increases, the heating efficiency deteriorates due to adhesion of fixed substances (for example, oxidized deterioration substances) to the combustion part, and therefore the fuel consumption rate 2 is usually smaller than the fuel consumption rate 1. The difference Δ (fuel consumption rate 1−fuel consumption rate 2) is an index of the amount of sticking matter adhering to the combustion part and the THC concentration (that is, the amount of odorous substance discharged).

  As shown in Table 3, it was confirmed that all of Examples 1 to 3 showed good flammability, and the generation of odorous substances and pollutants in the exhaust gas was sufficiently suppressed. . Furthermore, the decrease in the fuel consumption rate and the increase in the THC concentration during 100 cycles were small, suggesting that sticking of oxidative degradation products to the combustion portion was sufficiently suppressed.

  On the other hand, in Comparative Examples 1 to 3, the THC concentration 1 and the SOx concentration were high. Further, Δ (fuel consumption rate 1−fuel consumption rate 2) was large, and a large amount of adhering matter due to oxidative degradation adhered to the combustion portion of the heating equipment after 100 cycles. On the other hand, in the case of Comparative Example 4, the fuel consumption rate showed a large value, and the amount of THC emission was large.

Claims (1)

In the presence of a hydrogenation catalyst, a raw material oil containing at least one selected from unrefined oil and hydrorefined oil is reacted at a reaction temperature of 100 to 350 ° C., a hydrogen pressure of 1 to 6 MPa, and a liquid space velocity of 0.1 to 4 h. ^-1 Deep hydrogenation treatment at a hydrogen / oil ratio of 70 to 500 NL / L, the initial boiling point in distillation properties is 140 ° C. or higher, the end point is 300 ° C. or lower, the 50 vol% distillation temperature is 200 to 230 ° C., 70 ° C. volume% Distillation temperature is 220 to 250 ° C., naphthene content is 20% by volume or more, total aromatic content is 15% by volume or less, bicyclic or higher aromatic content is 1% by volume or less, naphthene content / total aromatic content The capacity ratio is 2.0 or more, the sulfur content is 10 mass ppm or less, and the density at 15 ° C. is 770 to 820 kg / m. ³ To obtain a kerosene base material
A method for producing a kerosene composition, comprising: