JP2007262156A - Fuel composition intended for very-low-temperature district - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a fuel composition intended for very-low-temperature-districts, designed to entirely satisfy its low-temperature fluidity in such districts, its flexibility compatible with multiple applications and its performance as an environmentally compatible fuel. <P>SOLUTION: The fuel composition comprises a hydrocarbon mixture obtained through predetermined steps with a specific hydrocarbon mixture as feedstock oil. This fuel composition has the following properties: saybolt color index is +28 or greater; density at 15°C is 740-840 kg/m<SP>3</SP>; 10% distillation temperature is 170-220°C; 90% distillation temperature is 220-300°C; cetane index is 45 or greater; cetane number is 48 or greater; flash point is 45°C or higher; the result of its reaction test is neutral; copper plate corrosion index is l or less; the peroxide value after subjected to an accelerated oxidation test is 10 mass ppm or less; pour point is -60°C or lower; sulfur content is 10 mass ppm or less; dynamic viscosity at 30°C is 1.6-5.0 mm<SP>2</SP>/s; dynamic viscosity at -30°C is 30 mm<SP>2</SP>/s or less; moisture content is 0.01 vol.% or less; and the residual carbon content of its 10% residual oil is 0.1 mass% or less. <P>COPYRIGHT: (C)2008,JPO&INPIT

Description

  The present invention relates to a fuel composition used in heating, power generation applications, and moving source applications such as automobiles, snow vehicles, ships, and helicopters in cryogenic regions such as the North Pole and Antarctica. In addition, the present invention relates to a fuel composition for cryogenic regions having both fuel flexibility and environmental performance.

  Because the current JIS standard prescribes product performance in Japan, the standard that can cope with the lowest temperature is a special grade 3 diesel oil (pour point -30 ° C or less) for diesel engines. Kerosene corresponds to this for heating. However, these fuels are likely to lose fluidity in extremely cold regions such as the inland region of Heilongjiang, China, the Russian Siberian region, the Alaska region of the United States, the Arctic Circle and Antarctica. Particularly in such areas, it is difficult to prepare multiple fuels for each application due to the problem of securing supply channels, and flexibility as a fuel that can be applied to multiple applications with one type of fuel is required at the same time. Yes. Furthermore, recently, environmental measures have been demanded even in regions that are not restricted by exhaust gas regulations, etc., and the application of environmentally friendly fuels is becoming a common social requirement.

As a fuel for cryogenic regions, for example, Patent Document 1 discloses a diesel light oil composition mainly containing a desulfurization and dewaxing base material. According to this document, it is described that it is possible to achieve both excellent low-temperature performance, fuel efficiency, and acceleration performance as a diesel engine application. However, the diesel light oil composition shown in this document is a factor that inhibits low-temperature fluidity by dewaxing. Exhaust gas performance due to heavy residue and a large amount of aromatics remaining in the feedstock, mainly due to the base material that has been mainly decomposed from chain saturated hydrocarbon compounds and chemically converted to saturated hydrocarbon compounds having side chains Continue to have concerns about Furthermore, a fuel containing a large amount of aromatic components and a small amount of linear saturated hydrocarbon compound has a problem that the ignition performance becomes unstable because the cetane number becomes low. From the above, it can be said that such a fuel is not suitable as an environmentally friendly fuel. Further, the diesel light oil composition lacks flexibility as a fuel that can be applied to a plurality of uses with one kind of fuel, and is not suitable as a fuel for heating. Furthermore, in general, fuel in such a cryogenic region is not in a situation where it can be arbitrarily replenished whenever it is used, so it is often forced to store for a relatively long period of time at a cryogenic temperature. Various performances should never deteriorate.
In other words, low temperature fluidity in a cryogenic region, flexibility that can be used for multiple applications, performance as an environmentally friendly fuel, and fuel performance at extremely low temperatures can be maintained, and these requirements are at a high level. It is very difficult to design a high-quality fuel that can be achieved simultaneously with the above, and the examples and knowledge based on the examination of realistic manufacturing methods that sufficiently satisfy the performance required for other fuel oils Does not exist.
Japanese Patent No. 3729211

  The present invention has been made in view of such a situation, and an object of the present invention is the extreme satisfaction satisfying all of the low temperature fluidity in a cryogenic region, the flexibility capable of responding to a plurality of uses, and the performance as an environment-friendly fuel. It is in providing the fuel composition for low temperature areas.

As a result of intensive studies to solve the above problems, the present inventors have completed the present invention.
That is, the present invention has an initial boiling point of 140 ° C. or higher and 200 ° C. or lower, a distillation property of 90 vol% distillation temperature of 200 ° C. or higher and 300 ° C. or lower, an aromatic content of 20 vol% or lower, and linear saturated hydrocarbon content. Step (1) using a hydrocarbon mixture A having an amount of 25% by mass or more, a linear saturated hydrocarbon content of 10 to 15 carbon atoms of 20% by mass or more, and a sulfur content of 300 ppm by mass or less as a feedstock : Reaction temperature 250 ° C. to 310 ° C., hydrogen pressure 5 MPa to 10 MPa, LHSV 0.5 h ^{−1 to} 3.0 h ⁻¹ , hydrogen / hydrocarbon capacity ratio 0.15 to 0.6 A step of obtaining a hydrocarbon mixture B by hydrodesulfurization treatment with a catalyst containing any of Ni-W, Ni-Mo, Co-Mo, Co-W, or Ni-Co-Mo under the conditions 2): Removing a light portion of the hydrogen fluoride mixture B in the range of 1% by volume or more and 40% by volume or less to obtain a hydrocarbon mixture C, step (3): the hydrocarbon mixture C is reacted at a reaction temperature of 150 ° C. or higher and 250 ° C. or lower; 80% by volume of the hydrocarbon mixture D obtained through the step of obtaining a hydrocarbon mixture D obtained by removing 10% by volume or more of linear saturated hydrocarbons with zeolite under a pressure of 1 MPa to 5 MPa. Contained above, Saybolt color +28 or more, density at 15 ° C. is 740 kg / m ³ or more and 840 kg / m ³ or less, 10% distillation temperature of distillation property is 170 ° C. or more and 220 ° C. or less, 90% distillation temperature is 220 ° C. or more 300 ° C. or lower, cetane index of 45 or higher, cetane number of 48 or higher, flash point of 45 ° C. or higher, reaction test result is neutral, copper plate corrosion is 1 or lower, peroxide value after accelerated oxidation test is 1 Mass ppm or less, a pour point -60 ° C. or less, a sulfur content of 10 ppm by mass or less, a kinematic viscosity at 30 ℃ 1.6mm ² / s or more 5.0 mm ² / s or less, a kinematic viscosity at -30 ℃ 30mm ² / s Hereinafter, the present invention relates to a fuel composition for a cryogenic region, wherein the moisture content is 0.01% by volume or less, and the residual carbon content of 10% residual oil is 0.1% by mass or less.

Further, the present invention has an initial boiling point of 140 ° C. or higher and 200 ° C. or lower, a distillation property of 90 vol% distillation temperature of 200 to 300 ° C., an aromatic content of 20 vol% or lower, and a linear saturated hydrocarbon content. Is a hydrocarbon mixture A having a straight chain saturated hydrocarbon content of 20 mass% or more and a sulfur content of 300 massppm or less having a raw material oil content of 25 mass% or more, 10 to 15 carbon atoms, and step (1): The hydrocarbon mixture A has a reaction temperature of 250 ° C. to 310 ° C., a hydrogen pressure of 5 MPa to 10 MPa, LHSV 0.5 h ^{−1 to} 3.0 h ⁻¹ and a hydrogen / hydrocarbon capacity ratio of 0.15 to 0.6. A step of obtaining a hydrocarbon mixture B by hydrodesulfurization treatment with a catalyst containing any one of Ni-W, Ni-Mo, Co-Mo, Co-W, or Ni-Co-Mo under conditions (2) ): Carbonized water A step of removing a light portion of the mixture B in a range of 1% by volume or more and 40% by volume or less to obtain a hydrocarbon mixture C, step (3): the hydrocarbon mixture C is reacted at a reaction temperature of 150 ° C. or more and 250 ° C. or less and a pressure of 1 MPa. The step of obtaining a hydrocarbon mixture D obtained by removing 10% by volume or more of linear saturated hydrocarbons with zeolite under a condition of 5 MPa or less, and 80 to 100% by volume of the hydrocarbon mixture D obtained through the total fuel composition The sum of the straight chain saturated hydrocarbon compound content of 16 to 20 carbon atoms is 10% by weight or less, and the sum of the straight chain saturated hydrocarbon compound content of 21 to 25 carbon atoms is 2% by weight or less. some FT synthetic base contains 0-20% by volume, Saybolt color +28 or higher, 15 density at ℃ is 740kg / ^{m 3} or more 840 kg / ^{m 3} or less, 10% distillation temperature of the distillation characteristics are 1 0 ° C. or higher and 220 ° C. or lower, 90% distillation temperature is 220 ° C. or higher and 300 ° C. or lower, cetane index 45 or higher, cetane number 48 or higher, flash point 45 ° C. or higher, reaction test result is neutral, copper plate corrosion is 1 or lower, Peroxide value after accelerated oxidation test is 10 mass ppm or less, pour point is −60 ° C. or less, sulfur content is 10 mass ppm or less, kinematic viscosity at 30 ° C. is 1.6 mm ² / s or more and 5.0 mm ² / s or less, − Cryogenic viscosity at 30 ° C. of 30 mm ² / s or less, moisture content of 0.01% by volume or less, residual carbon content of 10% residual oil of 0.1% by mass or less, fuel for cryogenic regions Relates to the composition.

According to the present invention, by using a fuel composition for a cryogenic region produced by the above production method, fraction regulation, etc., low temperature flow in a cryogenic region that was difficult to realize with a conventional fuel composition. Therefore, it is possible to provide a fuel composition for a cryogenic region satisfying all of the properties, flexibility that can be used for a plurality of uses, and performance as an environment-friendly fuel.
For the types and applications of equipment that operates by supplying the fuel composition, such as moving vehicles, snow vehicles, ships, aircraft, helicopters, work vehicles, heating equipment, power generation equipment, etc. The fuel composition does not impose any restrictions, but also imposes restrictions on the types of power sources and heat sources used in them, such as diesel engines, gas turbines, fuel cells, jet engines, burners, stoves, etc. It is not a thing.

  Hereinafter, the present invention will be described in detail.

  The hydrocarbon mixture A, which is a raw material oil for the fuel composition for cryogenic regions of the present invention, has an initial boiling point of 140 ° C. or higher and 200 ° C. or lower, a distillation property of 90 vol% distillation temperature of 200 ° C. or higher and 300 ° C. or lower, aroma Group content is 20% by volume or less, linear saturated hydrocarbon content is 25% by mass or more, linear saturated hydrocarbon content of 10 to 15 carbon atoms is 20% by mass or more, and sulfur content is 300% by mass or less. It is necessary to be. Preferably, the initial boiling point is 145 ° C. or higher and 190 ° C. or lower, the distillation property 90 volume% distillation temperature is 220 ° C. or higher and 290 ° C. or lower, the aromatic content is 17 volume% or lower, and the linear saturated hydrocarbon content is 28. The straight chain saturated hydrocarbon content of 10 mass% or more and 10 to 15 carbon atoms is 23 mass% or more, the sulfur content is 100 mass ppm or less, and more preferably, the initial boiling point is 150 ° C or more and 180 ° C or less, 90 vol% distillation temperature of distillation property is 230 ° C or higher and 285 ° C or lower, aromatic content is 15 vol% or lower, linear saturated hydrocarbon content is 30 mass% or higher, and linear saturation is 10 to 15 carbon atoms The hydrocarbon content is 25 mass% or more and the sulfur content is 50 mass ppm or less. If the properties of the hydrocarbon mixture A deviate from the above range, the reaction efficiency in the subsequent treatment is lowered, and it becomes difficult to obtain the fuel composition for the cryogenic region of the present invention.

Here, the initial boiling point and the 90% by volume distillation temperature are JIS K 2254 "Petroleum products-Distillation test method-Atmospheric pressure distillation test method", and the aromatic content is JIS K 2536 "Petroleum products-Hydrocarbon". The value measured by the fluorescent indicator adsorption method of “type test method”, linear saturated hydrocarbon content (normal paraffin content), linear saturated hydrocarbon content of 10 to 15 carbon atoms (nP content of C10-15) are , And a value (% by mass) measured using GC-FID. That is, a capillary column of methyl silicon (ULTRAALLOY-1) is used for the column, helium is used for the carrier gas, a hydrogen ion detector (FID) is used for the detector, a column length of 30 m, a carrier gas flow rate of 1.0 mL / min, and a splitting. It is a value measured under the conditions of ratio 1:79, sample injection temperature 360 ° C., column temperature rising condition 140 ° C. → (8 ° C./min)→355° C., detector temperature 360 ° C.
The sulfur content is a value measured according to JIS K 2541 “Crude oil and petroleum products—sulfur content test method”.
The hydrocarbon mixture A is not particularly limited other than having the above-mentioned predetermined properties. In addition to petroleum-based substrates, FT synthetic substrates, derived from animal and vegetable oils for reasons of improving exhaust gas performance as environmentally friendly fuels. It is preferable that it is processing oil of these.

  The petroleum base material is a hydrocarbon base material obtained by processing crude oil. Generally, the straight base material obtained from the atmospheric distillation apparatus, the straight-run heavy oil obtained from the atmospheric distillation apparatus or the residue Depressurized base material obtained by treating inspection oil with a vacuum distillation apparatus, catalytic cracking base material or hydrocracking base material obtained by catalytic cracking or hydrocracking of a decompressed heavy base material or desulfurized heavy oil, and these petroleum systems Examples thereof include hydrorefining base materials or hydrodesulfurization base materials obtained by hydrorefining hydrocarbons. In addition to crude oil, non-conventional petroleum resources, such as oil shells, oil sands, orinocotal, etc., are treated appropriately, and the base materials finished to the same performance as the above base materials are also petroleum. It can be used according to the base material.

  The FT synthesis base material is equivalent to naphtha, kerosene, or light oil obtained by applying a Fischer-Tropsch (FT) reaction to a mixed gas (also referred to as synthesis gas) mainly composed of hydrogen and carbon monoxide. It is obtained by purifying liquid fractions, and hydrocarbon mixtures obtained by hydrorefining and hydrocracking them, and FT wax obtained by FT reaction, hydrotreating and hydrocracking them. The base material which consists of a hydrocarbon mixture is shown.

The mixed gas used as the raw material of the FT synthesis base material is obtained by oxidizing a carbon-containing substance using oxygen and / or water and / or carbon dioxide as an oxidizing agent, and further using a shift reaction using water as necessary. It is obtained by adjusting to a predetermined hydrogen and carbon monoxide concentration.
Substances containing carbon include natural gas, petroleum liquefied gas, methane gas, etc., gas components consisting of hydrocarbons that are gaseous at room temperature, petroleum asphalt, biomass, coal, waste such as building materials and garbage, sludge, In addition, mixed gas obtained by exposing heavy crude oil, unconventional petroleum resources, etc. that are difficult to process by ordinary methods to high temperatures is common, but mixed gas mainly composed of hydrogen and carbon monoxide As long as is obtained, the present invention does not limit the raw materials.

  A Fischer-Tropsch reaction requires a metal catalyst. Preferably, the method uses a group 8 metal of the periodic table, for example, cobalt, ruthenium, rhodium, palladium, nickel, iron, etc., more preferably a group 8 group 4 metal as the active catalyst component. Moreover, the metal group which mixed these metals in an appropriate amount can also be used. These active metals are generally used in the form of a catalyst obtained by being supported on a support such as silica, alumina, titania or silica alumina. Further, by using these catalysts in combination with a second metal in addition to the above active metal, the catalyst performance can be improved. Examples of the second metal include zirconium, hafnium, titanium, and the like in addition to alkali metals and alkaline earth metals such as sodium, lithium, and magnesium, and a chain that serves as an index for improving the conversion rate of carbon monoxide and generating wax. It is used appropriately according to the purpose, such as an increase in growth probability (α).

  The Fischer-Tropsch reaction is a synthesis method that generates a liquid fraction and FT wax using a mixed gas as a raw material. In order to efficiently perform this synthesis method, it is generally preferable to control the ratio of hydrogen to carbon monoxide in the mixed gas. The molar mixing ratio of hydrogen to carbon monoxide (hydrogen / carbon monoxide) is preferably 1.2 or more, more preferably 1.5 or more, and even more preferably 1.8 or more. The ratio is preferably 3 or less, more preferably 2.6 or less, and even more preferably 2.2 or less.

  When performing the Fischer-Tropsch reaction using the catalyst, the reaction temperature is preferably 180 ° C. or higher and 320 ° C. or lower, and more preferably 200 ° C. or higher and 300 ° C. or lower. When the reaction temperature is less than 180 ° C., carbon monoxide hardly reacts and the hydrocarbon yield tends to be low. On the other hand, when the reaction temperature exceeds 320 ° C., the amount of gas such as methane increases, and the production efficiency of the liquid fraction and FT wax decreases.

No particular restriction on the gas hourly space velocity relative to the catalyst, but preferably 500h ^-1 or more 4000h ^-1 or less, 1000h ^-1 or more 3000h ^-1 or less is more preferable. If the gas space velocity is less than 500 h ⁻¹ , the productivity of the liquid fuel tends to decrease. If the gas space velocity exceeds 4000 h ⁻¹ , the reaction temperature must be increased, and gas generation increases, resulting in a yield of the target product. It will decline.

  The reaction pressure (partial pressure of synthesis gas composed of carbon monoxide and hydrogen) is not particularly limited, but is preferably 0.5 MPa or more and 7 MPa or less, and more preferably 2 MPa or more and 4 MPa or less. If the reaction pressure is less than 0.5 MPa, the yield of the liquid fuel tends to decrease, and if it exceeds 7 MPa, the amount of capital investment tends to increase, which is uneconomical.

  The FT synthesis substrate can be obtained by hydrorefining or hydrocracking the liquid fraction and FT wax produced by the above FT reaction by any method and adjusting them to the distillation properties, composition, etc. suitable for the purpose. Hydrorefining and hydrocracking may be selected in accordance with the purpose, and selection of only one or a combination of both methods is not limited in any way as long as the fuel composition of the present invention can be produced. .

The catalyst used for hydrorefining is generally a catalyst in which a hydrogenation active metal is supported on a porous carrier, but the present invention does not limit the form of the catalyst as long as the same effect can be obtained.
An inorganic oxide is preferably used as the porous carrier. Specific examples include alumina, titania, zirconia, boria, silica, zeolite, and the like.
Zeolite is a crystalline aluminosilicate, and includes faujasite, pentasil, mordenite, etc., preferably faujasite, beta, mordenite, particularly preferably Y type and beta type. Of these, the Y type is preferably ultra-stabilized.

As the active metal, the following two types (active metal A type and active metal B type) are preferably used.
The active metal A type is at least one metal selected from Group 8 metals of the Periodic Table. Preferably, it is at least one selected from Ru, Rh, Ir, Pd and Pt, more preferably Pd or / and Pt. 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, and the like. When using a noble metal catalyst composed of these metals, it can be used after pre-reduction treatment in a hydrogen stream. In general, when a gas containing hydrogen 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.
Further, as the active metal B type, it contains at least one metal selected from Group 6A and Group 8 metals of the periodic table, and preferably contains two or more metals selected from Groups 6A and 8 What you are doing can also be used. For example, Co-Mo, Ni-Mo, Ni-Co-Mo, and Ni-W can be mentioned. When a metal sulfide catalyst made of these metals is used, it is necessary to include a preliminary sulfidation step.

  As the metal source, a general inorganic salt or a complex salt compound can be used, and as a supporting method, any method of a supporting method used in an ordinary hydrogenation catalyst such as an impregnation method or an ion exchange method can be used. When a plurality of metals are supported, they may be supported simultaneously using a mixed solution, or may be sequentially supported using a single solution. The metal solution may be an aqueous solution or an organic solvent.

The reaction temperature when hydrotreating using a catalyst composed of an active metal A type is preferably 180 ° C. or higher and 400 ° C. or lower, more preferably 200 ° C. or higher and 370 ° C. or lower, and 250 ° C. or higher and 350 ° C. or lower. More preferably, the temperature is 280 ° C. or lower and even more preferably 280 ° C. or higher and 350 ° C. or lower. If the reaction temperature in hydrorefining exceeds 370 ° C., side reactions that decompose into naphtha fractions increase, and the yield of middle fractions is extremely undesirably reduced. On the other hand, when the reaction temperature is lower than 270 ° C., the alcohol component cannot be completely removed and is not preferable.
The reaction temperature when hydrotreating using a catalyst comprising an active metal B type is preferably 170 ° C. or higher and 320 ° C. or lower, more preferably 175 ° C. or higher and 300 ° C. or lower, and 180 ° C. or higher and 280 ° C. More preferably, it is not higher than ° C. If the reaction temperature in the hydrorefining exceeds 320 ° C., side reactions that decompose into naphtha fractions increase, and the yield of middle fractions is extremely undesirably reduced. On the other hand, when the reaction temperature is lower than 170 ° C., the alcohol component cannot be completely removed and is not preferable.

The hydrogen pressure when hydrotreating using a catalyst composed of an active metal A type is preferably 0.5 MPa or more and 12 MPa or less, and more preferably 1.0 MPa or more and 5.0 MPa or less. The higher the hydrogen pressure, the more hydrogenation reaction is promoted, but generally there is an optimal point economically.
The hydrogen pressure when hydrotreating using a catalyst composed of an active metal B type is preferably 2 MPa or more and 10 MPa or less, more preferably 2.5 MPa or more and 8 MPa or less, and 3 MPa or more and 7 MPa or less. More preferably. The higher the hydrogen pressure, the more hydrogenation reaction is promoted, but generally there is an optimal point economically.

The liquid hourly space velocity which hydrorefining is carried out using a catalyst composed of the active metal A type (LHSV) is preferably at 0.1 h ^-1 or more 10.0H ^-1 or less, 0.3h ^-1 or 3 More preferably, it is 5 h ⁻¹ or less. The lower the LHSV, the more advantageous for the reaction. However, if the LHSV is too low, an extremely large reaction tower volume is required, resulting in excessive capital investment, which is not economical.
The liquid hourly space velocity which hydrorefining is carried out using a catalyst composed of the active metal B type (LHSV) is preferably at 0.1 h ^-1 or more ^{2h -1} or less, 0.2 h ^-1 or more 1.5h more preferably ^{1 or} less, and more preferably 0.3h ^-1 or 1.2 h ^-1. The lower the LHSV, the more advantageous for the reaction. However, if the LHSV is too low, an extremely large reaction tower volume is required, resulting in excessive capital investment, which is not economical.

The hydrogen / oil ratio is preferably 50 NL / L or more and 1000 NL / L or less, more preferably 70 NL / L or more and 800 NL / L or less when hydrotreating using a catalyst composed of an active metal A type. preferable. The higher the hydrogen / oil ratio, the more hydrogenation reaction is promoted, but generally there is an optimal point economically.
The hydrogen / oil ratio when hydrotreating using a catalyst composed of an active metal B type is preferably 100 NL / L or more and 800 NL / L or less, more preferably 120 NL / L or more and 600 NL / L or less. Preferably, it is 150 NL / L or more and 500 NL / L or less. The higher the hydrogen / oil ratio, the more hydrogenation reaction is promoted, but generally there is an optimal point economically.

The catalyst used for hydrocracking is generally one in which a hydrogenation active metal is supported on a carrier having a solid acid property, but the present invention does not limit the form of the catalyst as long as the same effect can be obtained. Absent.
Supports having a solid acid property include amorphous and crystalline zeolites. Specific examples include amorphous silica-alumina, silica-magnesia, silica-zirconia, silica-titania and zeolite faujasite type, beta type, MFI type, and mordenite type. Preferred are faujasite type, beta type, MFI type, and mordenite type zeolite, and more preferred are Y type and beta type. The Y type is preferably ultra-stabilized.

As the active metal, the following two types (active metal A type and active metal B type) are preferably used.
The active metal A type is at least one metal selected from Group 6A and Group 8 metals in the periodic table. Preferably, it is at least one metal selected from Ni, Co, Mo, Pt, Pd and W. When using a noble metal catalyst composed of these metals, it can be used after pre-reduction treatment in a hydrogen stream. In general, when a gas containing hydrogen 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 active metal B type may be a combination of these metals, and examples thereof include Pt—Pd, Co—Mo, Ni—Mo, Ni—W, and Ni—Co—Mo. Moreover, when using the catalyst which consists of these metals, it is preferable to use after pre-sulfiding.

  As the metal source, a general inorganic salt or a complex salt compound can be used, and as a supporting method, any method of a supporting method used in an ordinary hydrogenation catalyst such as an impregnation method or an ion exchange method can be used. When a plurality of metals are supported, they may be supported simultaneously using a mixed solution, or may be sequentially supported using a single solution. The metal solution may be an aqueous solution or an organic solvent.

  The reaction temperature when performing hydrocracking using a catalyst comprising an active metal A type and an active metal B type is preferably 200 ° C. or higher and 450 ° C. or lower, more preferably 250 ° C. or higher and 430 ° C. or lower. More preferably, it is 300 ° C. or more and 400 ° C. or less. When the reaction temperature in hydrocracking exceeds 370 ° C., side reactions that decompose into a naphtha fraction increase and the yield of the middle fraction is extremely reduced, which is not preferable. On the other hand, when the temperature is lower than 200 ° C., the activity of the catalyst is remarkably lowered, which is not preferable.

  The hydrogen pressure when hydrocracking using a catalyst comprising an active metal A type and an active metal B type is preferably 1 MPa or more and 20 MPa or less, more preferably 4 MPa or more and 16 MPa or less, and 6 MPa or more and 13 MPa. More preferably, it is as follows. The higher the hydrogen pressure is, the more hydrogenation reaction is promoted. However, the decomposition reaction rather slows down and the progress of the reaction needs to be adjusted by increasing the reaction temperature, leading to a decrease in catalyst life. For this reason, there is generally an economical optimum for the reaction temperature.

The liquid hourly space velocity which hydrocracking is carried out using a catalyst composed of the active metal A type (LHSV) is preferably at 0.1 h ^-1 or more ^{10h -1} or less, 0.3h ^-1 over 3.5h ^-More preferably, it is ¹ or less. The lower the LHSV, the more advantageous for the reaction. However, if the LHSV is too low, an extremely large reaction tower volume is required, resulting in excessive capital investment, which is not economical.
The liquid hourly space velocity which hydrocracking is carried out using a catalyst composed of the active metal B type (LHSV) is preferably at 0.1 h ^-1 or more ^{2h -1} or less, 0.2 h ^-1 or more 1.7h more preferably ^{1 or} less, and more preferably 0.3h ^-1 or 1.5 h ^-1. The lower the LHSV, the more advantageous for the reaction. However, if the LHSV is too low, an extremely large reaction tower volume is required, resulting in excessive capital investment, which is not economical.

The hydrogen / oil ratio is preferably 50 NL / L or more and 1000 NL / L or less, more preferably 70 NL / L or more and 800 NL / L or less when hydrocracking using a catalyst composed of an active metal A type. Preferably, it is 400 NL / L or more and 1500 NL / L or less. The higher the hydrogen / oil ratio, the more hydrogenation reaction is promoted, but generally there is an optimal point economically.
The hydrogen / oil ratio is preferably 150 NL / L or more and 2000 NL / L or less, more preferably 300 NL / L or more and 1700 NL / L or less when hydrocracking using a catalyst composed of an active metal B type. Preferably, it is 400 NL / L or more and 1500 NL / L or less. The higher the hydrogen / oil ratio, the more hydrogenation reaction is promoted, but generally there is an optimal point economically.

The apparatus for hydrotreating may be of any configuration, the reaction towers may be used alone or in combination, hydrogen may be additionally injected between the reaction towers, gas-liquid separation operation, hydrogen sulfide removal equipment, hydrogen It may have a distillation column for fractionating the chemical product and obtaining the desired fraction.
The reaction format of the hydrotreating apparatus can take a fixed bed system. Hydrogen can take either a countercurrent or a cocurrent flow with respect to the feedstock, and may have a plurality of reaction towers and a combination of countercurrent and cocurrent flow. The general format is downflow, and there is a gas-liquid twin parallel flow format. Hydrogen gas may be injected into the middle stage of the reaction tower as a quench for the purpose of removing reaction heat or increasing the hydrogen partial pressure.

  The treatment oil derived from animals and plants is composed of hydrocarbons obtained by applying the chemical reaction treatment applied when obtaining the above-mentioned petroleum-based base material to the oils and fats produced and produced from the animal and plant raw materials. It is a substrate. More specifically, an inorganic material having at least one metal selected from Group 6A and Group 8 of the periodic table and acid properties using a hydrocarbon fraction containing components derived from animal and plant oils and animal fats as raw material oils. A hydrocarbon-containing mixed base material which is brought into contact with a hydrocracking catalyst containing an oxide under hydrogen pressure. The raw material oil for the processed oil derived from animals and plants needs to be a component derived from animal and vegetable oils and fats. The animal and vegetable oils and fats and components derived from animal and vegetable oils and fats in the present invention refer to animal and vegetable oils and fats and components derived from animal and vegetable oils and fats that are produced or manufactured naturally or artificially. Animal fats and oils are made from beef tallow, milk fat (butter), pork tallow, sheep fat, whale oil, fish oil, liver oil, etc. (Rapeseed flowers), rice bran, sunflower, cottonseed, corn, soybean, sesame, linseed and other seeds and other parts can be mentioned, but other fats and oils can be used without problems. These raw oils may be solid or liquid, but it is preferable to use vegetable oils and vegetable oils as raw materials because of ease of handling, high carbon dioxide absorption capacity and high productivity. Moreover, in this invention, the waste oil which used these animal oils and vegetable oils for consumer use, industrial use, food use etc. can also be used as a raw material after adding the removal process of miscellaneous matters.

As a typical composition of the fatty acid portion of the glyceride compound contained in these raw materials, butyric acid (C ₃ H ₇ COOH), which is a fatty acid having no unsaturated bond in the molecular structure called saturated fatty acid, caproic acid ( C ₅ H ₁₁ COOH), caprylic acid (C ₇ H ₁₅ COOH), capric acid (C ₉ H ₁₉ COOH), lauric acid (C ₁₁ H ₂₃ COOH), myristic acid (C ₁₃ H ₂₇ COOH), palmitic acid ( C ₁₅ H ₃₁ COOH), stearic acid (C ₁₇ H ₃₅ COOH), and oleic acid (C ₁₇ H ₃₃ COOH), which is an unsaturated fatty acid having one or more unsaturated bonds, linoleic acid (C ₁₇ H ₃₁ COOH) ), linolenic acid _{(C 17} H 29 COOH), ricinoleic acid _{(C 17 H 32 (OH)} COOH) Hitoshigakyo It is. The hydrocarbon part of these fatty acids in natural substances is generally linear, but it is used in the present invention even if it has a structure having a side chain, that is, an isomer, as long as the properties defined in the present invention are satisfied. be able to. Further, the position of the unsaturated bond in the molecule of the unsaturated fatty acid is not limited to those generally found in nature as long as the properties defined in the present invention are satisfied in the present invention. The set one can also be used.

The above-mentioned raw material oils (animal and vegetable oils and fats and components derived from animal and vegetable oils and fats) have one or more of these fatty acids, and the fatty acids they have differ depending on the raw materials. For example, coconut oil has a relatively large amount of saturated fatty acids such as lauric acid and myristic acid, while soybean oil has a large amount of unsaturated fatty acids such as oleic acid and linoleic acid.
The feedstock oil preferably contains a fraction of 250 ° C or higher, more preferably contains a fraction of 300 ° C or higher, and contains a fraction of 360 ° C or higher. Further preferred. When the fraction having a boiling point of 230 ° C. or higher is not contained, the production of gas is increased during production, so that the yield of the liquid product is decreased, and the life cycle carbon dioxide may be increased.

  Moreover, as raw material oil of the process oil derived from animals and plants, what mixed the petroleum hydrocarbon fraction with the animal and plant oils and fats and animal fats and oils-derived components may be used. In this case, the ratio of the petroleum hydrocarbon fraction is preferably 10 to 99% by volume, more preferably 30 to 99% by volume, and still more preferably 60 to 98% by volume based on the total volume of the feedstock. If the proportion of petroleum hydrocarbon fraction is less than 10% by volume, there may be a need for equipment for treating by-product water, and the proportion of petroleum hydrocarbon fraction is 99% by volume. When exceeding, it is not preferable from a viewpoint of life-cycle carbon dioxide reduction.

The hydrocracking conditions in the hydrotreating of the feedstock oil are performed under conditions such as a hydrogen pressure of 6 to 20 MPa, a liquid space velocity (LHSV) of 0.1 to 1.5 h ⁻¹ , and a hydrogen / oil ratio of 200 to 2000 NL / L. More desirable are conditions such as a hydrogen pressure of 8 to 17 MPa, a liquid space velocity of 0.2 to 1.1 h ⁻¹ , a hydrogen / oil ratio of 300 to 1800 NL / L, a hydrogen pressure of 10 to 16 MPa, and a liquid space velocity of 0.3. Conditions such as ~ 0.9h ^-1 and hydrogen / oil ratio 350-1600NL / L are even more desirable. These conditions are all factors that influence the reaction activity. For example, when the hydrogen pressure and the hydrogen oil ratio are less than the lower limit values, there is a risk of causing a decrease in reactivity or a rapid decrease in activity. If the hydrogen oil ratio exceeds the upper limit, excessive equipment investment such as a compressor may be required. Liquid hourly space velocity tends to be more advantageous for the lower the reaction, if it is less than 0.1 h ^-1 tend to be extremely large reactor volume is required excessive capital investment, while the 1.5 h ^-1 If it exceeds, the reaction will not proceed sufficiently.

  The hydrocarbon mixture A which is a raw material oil is processed in the following steps (1) to (3).

In the step (1), the hydrocarbon composition A is reacted at a reaction temperature of 250 ° C. or higher and 310 ° C. or lower, a hydrogen pressure of 5 MPa or higher and 10 MPa or lower, LHSV 0.5h ⁻¹ or higher and 3.0h ⁻¹ or lower, hydrogen / hydrocarbon capacity ratio. Hydrogen with a catalyst containing any of Ni-W, Ni-Mo, Co-Mo, Co-W, or Ni-Co-Mo under the condition (hydrogen / oil ratio) of 0.15 to 0.6 Hydrodesulfurization treatment is performed to obtain hydrocarbon mixture B.

The reaction temperature of the hydrodesulfurization treatment is 250 ° C. or higher and 310 ° C. or lower, preferably 280 ° C. or higher and 305 ° C. or lower. When the reaction temperature is less than 250 ° C., a sufficient hydrodesulfurization reaction rate cannot be obtained. On the other hand, when the reaction temperature exceeds 310 ° C., the hydrodesulfurization reaction becomes insufficient in terms of reaction equilibrium. The hydrogen pressure in the hydrodesulfurization treatment is 5 MPa or more and 10 MPa or less, preferably 7 MPa or more and 9 MPa or less. LHSV in hydrodesulfurization process is less 0.5h ^-1 or 3.0 h ^-1, preferably not ^{1h -1} or ^{2h -1} or less. A lower LHSV is advantageous for the reaction, but if it is less than 0.5 h ⁻¹ , a very large reaction column volume is required. The hydrogen / hydrocarbon capacity ratio is 0.15 or more and 0.6 or less, preferably 0.2 or more and 0.4 or less. When the hydrogen pressure is less than 5 MPa and when the hydrogen / hydrocarbon capacity ratio is less than 0.15, the effect of promoting the desulfurization reaction or the hydrogenation reaction becomes insufficient. In addition, when the hydrogen pressure exceeds 10 MPa and the hydrogen / hydrocarbon capacity ratio exceeds 0.6, the apparatus cost increases and becomes inefficient.

  The catalyst used in the hydrodesulfurization treatment needs to contain any of Ni—W, Ni—Mo, Co—Mo, Co—W, and Ni—Co—Mo as an active metal of the catalyst. 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 amount of the above-mentioned active metal supported is not particularly limited, but is preferably 20% by mass or more and 35% by mass or less in terms of the total amount of metal oxides with respect to the catalyst mass. The catalyst is preferably used after presulfiding with hydrogen and a sulfur compound. In general, a gas containing hydrogen and a sulfur compound is circulated, and heat of 200 ° C. or higher is given in accordance with a predetermined procedure to presulfurize the active metal on the catalyst and develop hydrogenation and desulfurization activities.

  In step (2), a light mixture (generally boiling point of 200 ° C. or less) is stripped (removed) from hydrocarbon mixture B obtained in step (1) to obtain hydrocarbon mixture C. The strip amount is 1% by volume or more and 40% by volume or less, preferably 10% by volume or more and 37% by volume or less, more preferably 20% by volume or more and 35% by volume or less, based on hydrodesulfurized oil. . When stripping is not performed or when the strip amount is not sufficient, the load of the removal device for the linear saturated hydrocarbon (normal paraffin) in the subsequent stage increases, and the removal efficiency decreases. Also, if the strip amount is excessive (over 40% by volume), the time required for strip processing increases, and the energy consumption during production increases.

In step (3), the hydrocarbon mixture C obtained by stripping (removing) the light components in step (2) is linearized with zeolite under conditions of a temperature of 150 ° C. to 250 ° C. and a pressure of 1 MPa to 5 MPa. The hydrocarbon mixture D is obtained by extracting and removing 10% or more of saturated hydrocarbons.
The reaction temperature for the removal of the linear saturated hydrocarbon is 150 ° C. or higher and 250 ° C. or lower, preferably 180 ° C. or higher and 200 ° C. or lower. When the reaction temperature is less than 150 ° C., a sufficient removal rate of linear saturated hydrocarbon cannot be obtained. On the other hand, when it exceeds 250 degreeC, the removal efficiency of a linear saturated hydrocarbon will fall. Further, the pressure at this time is 1 MPa or more and 5 MPa or less, preferably 1.5 MPa or more and 3 MPa or less. If the pressure is less than 1 MPa, a sufficient removal rate of linear saturated hydrocarbons cannot be obtained. On the other hand, if it exceeds 5 MPa, a sufficient removal rate of linear saturated hydrocarbons cannot be obtained. The zeolite used for the removal of the linear saturated hydrocarbon is not particularly limited, but generally, A-type zeolite is used, and among these, the molecular sieve 5A is preferable. Under the above conditions, it is necessary to extract and remove linear saturated hydrocarbons by 10% by volume or more, preferably 20% by mass or more.

The fuel composition for cryogenic regions of the present invention contains a hydrocarbon mixture D obtained through the above steps (1) to (3) in an amount of 80% by volume or more based on the total fuel composition, and has the following specific properties. It is necessary to have.
Moreover, the fuel composition for cryogenic regions of the present invention comprises a hydrocarbon mixture D obtained through the above steps (1) to (3) in an amount of 80 to 100% by volume, 16 to 20 carbon atoms, based on the total fuel composition. The sum total of the following linear saturated hydrocarbon compound content is 10 mass% or less, and the sum total of the linear saturated hydrocarbon compound content of 21 to 25 carbon atoms is 2 mass% or less. It is preferable that the FT synthetic substrate is contained in an amount of 0 to 20% by volume and has the following specific properties.

  The fuel composition for cryogenic regions of the present invention is carbonized obtained through the above steps (1) to (3) from the viewpoint of ensuring low temperature fluidity and good exhaust gas performance required for environmentally friendly fuels. The hydrogen mixture D may be contained in an amount of 80 to 100% by volume with respect to the total fuel composition, and a FT synthetic base material having specific properties may be blended in an amount exceeding 0% by volume and not more than 20% by volume based on the total fuel composition. it can. The FT synthetic base material that can be blended has a total content of linear saturated hydrocarbon compounds having 16 to 20 carbon atoms in a total content of 10% by mass or less and a linear saturated hydrocarbon compound content having 21 to 25 carbon atoms. FT synthesis base material characterized in that total is 2% by mass or less, more preferably the total content of linear saturated hydrocarbon compounds having 16 to 20 carbon atoms is 8% by mass or less, and carbon The sum total of the linear saturated hydrocarbon compound content of 21 to 25 is 1.8% by mass or less, more preferably the sum of the linear saturated hydrocarbon compound content of 16 to 20 carbons is 6% by mass. And an FT synthetic substrate having a total content of straight chain saturated hydrocarbon compounds having 21 to 25 carbon atoms of 1.5 mass% or less, and even more preferably a straight chain having 16 to 20 carbon atoms. Chain saturated carbonization The sum of the silicon compound content is not less than 5% by weight, and an FT synthetic base sum total 21 to 25 straight-chain saturated hydrocarbon compound content of carbon is less than 1 wt%. When an FT synthetic base material and other base materials other than this range are blended, it becomes difficult to achieve both low-temperature fluidity and environmental performance. Here, the FT synthetic substrate refers to a hydrocarbon substrate obtained by the above-described production method. The linear saturated hydrocarbon compound content (mass%) of 16 to 20 carbon atoms (nP of C16 to C20) and 21 to 25 carbon atoms (nP of C21 to C25) is the above-described GC-FID. Can be measured.

The fuel composition for cryogenic regions of the present invention has a Saybolt color of +28 or more, a density at 15 ° C. of 740 kg / m ³ or more and 840 kg / m ³ or less, a 10% distillation temperature of distillation property of 170 ° C. or more and 220 ° C. or less, 90 % Distillation temperature is 220 ° C. or higher and 300 ° C. or lower, cetane index 45 or higher, cetane number 48 or higher, flash point 45 ° C. or higher, reaction test result is neutral, copper plate corrosion is 1 or lower, peroxide value after accelerated oxidation test Is 10 mass ppm or less, the pour point is −60 ° C. or less, the sulfur content is 10 mass ppm or less, the kinematic viscosity at 30 ° C. is 1.6 mm ² / s or more and 5.0 mm ² / s or less, and the kinematic viscosity at −30 ° C. is 30 mm ^2. / S or less, the water content is 0.01% by volume or less, and the residual carbon content of the 10% residual oil is required to be 0.1% by mass or less.

  As described above, the Saybolt color of the fuel composition for the cryogenic region of the present invention needs to be +28 or more, preferably +29 or more, and more preferably +30 or more from the viewpoint of removing the oxidation stability inhibitor. preferable. The Saebold color here means a value measured according to JIS K 2580 “Petroleum products—color test method—Saebold color test method”.

The density at 15 ° C. of the fuel composition for cryogenic regions of the present invention needs to be 740 kg / m ³ or more from the viewpoint of securing a calorific value, preferably 750 kg / m ³ or more, and 755 kg / m ³ or more. Is more preferable. Further, the density, NOx, from the viewpoint of reducing the emissions of PM, must be at 840 kg / ^{m 3} or less, preferably 830 kg / ^{m 3} or less, 820 kg / ^{m 3} or less is more preferable. In addition, the density here means the density measured by JIS K 2249 “Density test method and density / mass / capacity conversion table of crude oil and petroleum products”.

The distillation properties in the fuel composition for cryogenic regions of the present invention require that the 10% distillation temperature is 170 ° C. or higher and 220 ° C. or lower, and the 90% distillation temperature is 220 ° C. or higher and 300 ° C. or lower. If the 10% distillation temperature is less than 170 ° C., the engine output and the startability at low temperatures tend to deteriorate. Therefore, the temperature is preferably 173 ° C. or higher, more preferably 178 ° C. or higher, and further preferably 180 ° C. or higher. On the other hand, if the 10% distillation temperature exceeds 220 ° C, the exhaust gas performance tends to deteriorate, so it is preferably 215 ° C or less, more preferably 210 ° C or less, and even more preferably 205 ° C or less.
Further, if the 90% distillation temperature is less than 220 ° C, the effect of improving the fuel efficiency becomes insufficient and the engine output tends to decrease. Therefore, it is preferably 225 ° C or higher, more preferably 230 ° C or higher, and further preferably 235 ° C. That's it. On the other hand, when the 90% distillation temperature exceeds 300 ° C., the amount of PM and fine particles discharged tends to increase. Therefore, it is preferably 295 ° C. or less, more preferably 290 ° C. or less, and further preferably 285 ° C. or less. The 10% distillation temperature and 90% distillation temperature here mean values measured according to JIS K 2254 “Petroleum products—Distillation test method—Atmospheric pressure method”.

  The cetane index of the fuel composition for cryogenic regions of the present invention needs to be 45 or more. When the cetane index is less than 45, the concentration of PM, aldehydes, or NOx in the exhaust gas tends to increase. For the same reason, the cetane index is preferably 46 or more, and more preferably 47 or more. The cetane index referred to in the present invention is defined by “Calculation method of cetane index using 8.4 variable equations” in JIS K 2280 “Petroleum products-fuel oil-octane number and cetane number test method and cetane index calculation method”. It means the calculated value. Here, the cetane index in the JIS standard is generally applied to light oil to which no cetane number improver is added, but in the present invention, the above-mentioned " Applying “8.4 Calculation Method of Cetane Index Using Variable Equation”, a value calculated by the calculation method is expressed as a cetane index.

  The cetane number in the fuel composition for cryogenic regions of the present invention needs to be 48 or more. When the cetane number is less than 48, the concentration of NOx, PM, and aldehydes in the exhaust gas tends to be high, and thus it is preferably 48.5 or more, and more preferably 49 or more. Further, from the viewpoint of reducing black smoke in the exhaust gas, the cetane number is preferably 90 or less, more preferably 85 or less, and further preferably 80 or less. Moreover, in the fuel composition of the present invention, an appropriate amount of a cetane number improver can be blended as required to improve the cetane number of the resulting fuel composition. The cetane number referred to here is a cetane number measured in accordance with “7. Cetane number test method” in JIS K 2280 “Petroleum products—Fuel oil—Octane number and cetane number test method and cetane index calculation method”. Means.

  The flash point of the fuel composition for cryogenic regions of the present invention needs to be 45 ° C. or higher. When the flash point is less than 45 ° C., it is not preferable from the viewpoint of safety. Therefore, the flash point is preferably 47 ° C. or higher, and more preferably 49 ° C. or higher. The flash point in the present invention is a value measured by JIS K 2265 “Crude oil and petroleum product flash point test method”.

  The result of the reaction test of the fuel composition for the cryogenic region of the present invention must be neutral. When the result of the reaction test is not neutral, it is not preferable because the possibility that the influence of corrosion on the metal member by the fuel becomes obvious is increased. In addition, the result of the reaction test as used in this invention shows the value measured by JISK2252 "petroleum product-reaction test method".

  The copper plate corrosion of the fuel composition for a cryogenic region of the present invention needs to be 1 or less, and preferably 1a. When the copper plate corrosion is not 1 or less, the possibility that the influence of the corrosion on the metal member by the fuel becomes obvious is increased, which causes a problem in stability and long-term storage. In addition, copper plate corrosion as used in the field of this invention shows the value measured by JISK2513 "Petroleum product-Copper plate corrosion test method".

The peroxide value after the accelerated oxidation test of the fuel composition for cryogenic regions of the present invention needs to be 10 ppm by mass or less. The peroxide value after the accelerated oxidation test is preferably 8 ppm by mass or less, more preferably 6 ppm by mass or less, and even more preferably 4 ppm by mass or less, from the viewpoint of storage stability and compatibility with members.
The peroxide value after the accelerated oxidation test referred to here is the Petroleum Institute Standard JPI- after conducting the accelerated oxidation test under conditions of 95 ° C. and oxygen bubbling for 16 hours in accordance with ASTM D2274-94. It means the value of peroxide value measured according to 5S-46-96. In order to reduce the peroxide value, an additive such as an antioxidant or a metal deactivator can be appropriately added to the fuel composition for cryogenic regions of the present invention.

  The pour point of the cryogenic fuel composition of the present invention is required to be −60 ° C. or lower. Furthermore, from the viewpoint of low-temperature startability or low-temperature operability at extremely low temperatures, and from the viewpoint of maintaining injection performance in the electronically controlled fuel injection pump, it is preferably −62 ° C. or lower. Here, the pour point means a pour point measured according to JIS K 2269 “Pour point of crude oil and petroleum products and cloud point test method of petroleum products”.

  The sulfur content of the fuel composition for the cryogenic region of the present invention must satisfy 10 ppm by mass or less, preferably 8 masses from the viewpoint of reducing harmful exhaust components discharged from the engine and improving the performance of the exhaust gas aftertreatment device. ppm or less, more preferably 5 mass ppm or less, further preferably 3 mass ppm or less, and even more preferably 1 mass ppm or less. In addition, the sulfur content here means the mass content of the sulfur content based on the total amount of the fuel composition measured by JIS K 2541 “Sulfur content test method”.

Kinematic viscosity at 30 ° C. cryogenic locations for fuel compositions of the present invention is required to be 1.6 mm ² / s or more, preferably 1.65 mm ² / s or more, 1.7 mm ² / S or more is more preferable. When the kinematic viscosity is less than 1.6 mm ² / s, the fuel injection timing control on the fuel injection pump side tends to be difficult, and the lubricity of each part of the fuel injection pump mounted on the engine is impaired. There is a fear. On the other hand, the upper limit of the kinematic viscosity at 30 ° C. needs to be 5.0 mm ² / s, preferably 4 mm ² / s or less, and more preferably 3 mm ² / s or less. If the kinematic viscosity exceeds 5.0 mm ² / s, the resistance inside the fuel injection system increases, the injection system becomes unstable, and the concentrations of NOx and PM in the exhaust gas increase, which is not preferable. In addition, kinematic viscosity here means kinematic viscosity measured by JISK2283 "crude oil and petroleum products-kinematic viscosity test method and viscosity index calculation method".

The kinematic viscosity at −30 ° C. of the fuel composition for cryogenic regions of the present invention needs to be 30 mm ² / s or less, preferably 28 mm ² / s or less, and 26 mm ² / s or less. It is more preferable. When the kinematic viscosity exceeds 30 mm ² / s, workability is impaired at extremely low temperatures, which is not preferable. In addition, kinematic viscosity here means kinematic viscosity measured according to JISK2283 "Crude oil and petroleum products-kinematic viscosity test method and viscosity index calculation method".

  The water content of the fuel composition for the cryogenic region of the present invention needs to be 100 ppm by volume or less, preferably 50 ppm by volume or less, more preferably 20 from the viewpoint of prevention of freezing at extremely low temperatures. The capacity is ppm or less. The water content here means a value measured by JIS K 2275 “Crude oil and petroleum products—moisture test method—Karl Fischer coulometric titration method”.

  The residual carbon content of 10% residual oil of the fuel composition for cryogenic regions of the present invention must be 0.1% by mass or less, and 0.08% by mass or less from the viewpoint of preventing filter clogging by sludge. Is preferable, and 0.05 mass% or less is more preferable. The residual carbon content of 10% residual oil here means a value measured by JIS K 2270 “Crude oil and petroleum products—residual carbon content test method”.

  In the fuel composition for a cryogenic region of the present invention, it is preferable to add an appropriate amount of an antifreezing agent, a low temperature fluidity improver, and a lubricity improver as necessary.

  It is preferable to add an antifreezing agent to the fuel composition for the cryogenic region of the present invention from the viewpoint of preventing moisture in the oil and preventing problems of the fuel filter and the fuel injection system. Moreover, it is preferable that the addition amount is 100 mass ppm or more and 500 mass ppm or less, and it is more preferable that it is 200 mass ppm or more and 400 mass ppm or less. Although the kind of antifreezing agent is not particularly limited, various compounds having an antifreezing function can be arbitrarily used, and examples thereof include 2-methoxyethanol, isopropyl alcohol, polyglycol ether, etc. From the viewpoint of ensuring fluidity, the melting point or pour point of these antifreeze agents is preferably −60 ° C. or lower. However, those having a metal and those having a salt structure, such as sodium acetate, calcium acetate, sodium chloride, and calcium chloride, are not suitable for fuel applications. These antifreeze agents may be used alone or in combination of two or more, but those having a purity of 98% or more of each antifreeze-containing main compound are more preferably used. can do.

It is preferable to add a low-temperature fluidity improver to the cryogenic fuel composition of the present invention from the viewpoint of preventing the filter blockage of a diesel vehicle. Moreover, the addition amount is preferably 200 mg / L or more and 1000 mg / L or less, more preferably 300 mg / L or more and 800 mg / L or less in terms of active ingredient concentration.
The type of the low-temperature fluidity improver is not particularly limited. For example, ethylene-unsaturated ester copolymer represented by ethylene-vinyl acetate copolymer, alkenyl succinic acid amide, dibehenate ester of polyethylene glycol Linear compounds such as phthalic acid, ethylenediaminetetraacetic acid, nitriloacetic acid and the like, or polar nitrogen compounds consisting of reaction products of hydrocarbyl-substituted amines, alkyl fumarate or alkyl itaconate-unsaturated esters One kind or two or more kinds of low-temperature fluidity improvers such as a comb polymer made of a copolymer can be used. Further, a copolymer of ethylene and methyl methacrylate, a copolymer of ethylene and α-olefin, a chlorinated methylene-vinyl acetate copolymer, an alkyl ester polymer of unsaturated carboxylic acid, a nitrogen-containing compound having a hydroxyl group And esters synthesized from saturates and saturated fatty acids, esters and amide derivatives synthesized from polyhydric alcohols and saturated fatty acids, esters synthesized from polyoxyalkylene glycols and saturated fatty acids, alkylene oxides of polyhydric alcohols or partial esters thereof Low temperature fluidity improver combining one or more selected from esters synthesized from adducts and saturated fatty acids, chlorinated paraffin / naphthalene condensates, alkenyl succinic acid amides, amine salts of sulfobenzoic acid, etc. can do. Among these, from the viewpoint of versatility, an ethylene-vinyl acetate copolymer additive can be preferably used. In addition, since a commercial product referred to as a low temperature fluidity improver may be diluted with an appropriate solvent for an active ingredient (active ingredient) that contributes to low temperature fluidity, such a commercial product may be used in the present invention. In the case of adding to the fuel composition, the above-mentioned addition amount means the addition amount (active ingredient concentration) as an active ingredient.

  In order to prevent wear of the fuel injection pump, it is preferable to add a lubricity improver to the fuel composition for cryogenic regions of the present invention. Moreover, the addition amount is preferably 20 mg / L or more and 200 mg / L or less, more preferably 50 mg / L or more and 180 mg / L or less in terms of active ingredient concentration. When the addition amount of the lubricity improver is within the above range, the effect of the added lubricity improver can be effectively extracted. For example, in a diesel engine equipped with a distributed injection pump, An increase in driving torque can be suppressed and pump wear can be reduced.

The type of the lubricity improver is not particularly limited. For example, one or more of carboxylic acid-based, ester-based, alcohol-based and phenol-based lubricity improvers can be used arbitrarily. . Among these, carboxylic acid-based and ester-based lubricity improvers are preferable.
Examples of the carboxylic acid-based lubricity improver include linoleic acid, oleic acid, salicylic acid, palmitic acid, myristic acid, hexadecenoic acid and a mixture of two or more of the above carboxylic acids.
Examples of ester-based lubricity improvers include carboxylic acid esters of glycerin. The carboxylic acid constituting the carboxylic acid ester may be one kind or two or more kinds, and specific examples thereof include linoleic acid, oleic acid, salicylic acid, palmitic acid, myristic acid, hexadecenoic acid and the like. There is.
In addition, since this invention presupposes the use in a very low temperature area, what has the unsaturated bond for the fatty-acid structure of these lubricity improvement agents is more preferable from a viewpoint of low-temperature fluidity ensuring.

Further, for the purpose of further enhancing the performance of the fuel composition for cryogenic regions in the present invention, other known fuel oil additives (hereinafter referred to as “other additives” for convenience) are added alone or in combination of several kinds. You can also Other additives include, for example, nitrate esters represented by alkyl nitrates having 6 to 8 carbon atoms, cetane number improvers such as organic peroxides; imide compounds, alkenyl succinimides, succinates, Detergents such as polymerized polymers and ashless detergents; antioxidants such as phenols and amines; metal deactivators such as salicylidene derivatives; corrosion inhibitors such as aliphatic amines and alkenyl succinates; anionics Antistatic agents such as cationic and amphoteric surfactants; colorants such as azo dyes; antifoaming agents such as silicon.
The addition amount of other additives can be arbitrarily determined, but the addition amount of each additive is preferably 0.5% by mass or less, more preferably 0. 0% by mass based on the total amount of the fuel composition for cryogenic regions. 2% by mass or less.

  As described above, according to the present invention, it is difficult to realize the conventional fuel composition by using the fuel composition for cryogenic regions manufactured by the manufacturing method, fraction regulation, etc. shown in the present invention. It is possible to provide a fuel composition for a cryogenic region satisfying all the low-temperature fluidity in a cryogenic region, the flexibility to cope with a plurality of uses, and the performance as an environment-friendly fuel.

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

(Examples 1-4 and Comparative Examples 1-2)
The raw material oil having the properties shown in Table 1 was reacted and processed under the conditions for each step shown in Table 2 to prepare fuel compositions for cryogenic regions shown in Table 3 (Examples 1 to 3). Examples 1, 2, and 3 are obtained by subjecting different raw oils to respective process treatments under different conditions. In Example 1, a high-grade hydrorefining treatment including a ring-opening reaction for aromatics was performed on petroleum-based hydrocarbons, and the resulting hydrocarbons were used as feedstock oil. In Example 2, natural gas is subjected to wax and middle distillation by FT reaction, and a hydrocarbon obtained by subjecting this to hydrogenation is used as a raw material oil. Example 3 is a process of hydrorefining the oil obtained from palm palm (not separated into fractions and used in a hole state) to remove hydrocarbons obtained after removing unnecessary alcohol and the like. It is a raw material oil.
Example 4 blends the synthetic fuel base material shown in Table 1 after producing the fuel oil composition of Example 1. The blended synthetic fuel base material consists of a hydrocarbon mixture obtained by subjecting natural gas to wax and middle distillation by FT reaction and hydrotreating it, and the isomerization reaction has progressed relatively. It contains a saturated hydrocarbon compound having a side chain. Comparative Example 1 is a catalyst in which a zeolite is loaded with a metal group selected from Group 6A and Group 8 metals on the conditions of a reaction pressure of 3 MPa, a reaction temperature of 380 ° C., and a liquid space velocity of 0.8 h ⁻¹ . A composition produced by mixing a treated desulfurized and dewaxed base material with a kerosene fraction. Comparative Example 2 produced a light oil fraction and a kerosene fraction by a general hydrorefining process, and appropriate amounts thereof It is a composition having a low temperature performance equivalent to JIS No. 3 diesel oil when blended.

The additives used in this example are as follows.
Antifreezing agent: 2-methoxyethanol Lubricity improver: Carboxylic acid mixture based on linoleic acid Low temperature fluidity improver: Ethylene-vinyl acetate copolymer Cetane improver: 2-ethylhexyl nitrate

  The blending ratio of the blended fuel composition and the blended fuel composition, density at 15 ° C., kinematic viscosity at 30 ° C., kinematic viscosity at −30 ° C., flash point, sulfur content, distillation properties, aroma Group content, cetane index, cetane number, pour point, hue, residual carbon content of 10% residual oil, results of reaction test, copper plate corrosion, moisture, total insoluble content and peroxide value after oxidation stability test, The results of measuring the conductivity and wear scar diameter are shown in Table 3.

The properties of the raw material oil and fuel oil were measured by the following method.
The density refers to a density measured according to JIS K 2249 “Determination method of density of crude oil and petroleum products and density / mass / capacity conversion table”.
The kinematic viscosity refers to a kinematic viscosity measured according to JIS K 2283 “Crude oil and petroleum products—Kinematic viscosity test method and viscosity index calculation method”.
The flash point indicates a value measured according to JIS K 2265 “Crude oil and petroleum product flash point test method”.
The sulfur content refers to the mass content of the sulfur content based on the total amount of the fuel composition measured by JIS K2541 “Sulfur content test method”.
All the distillation properties are values measured by JIS K 2254 "Petroleum products-Distillation test method".
The aromatic content is measured according to the Japan Petroleum Institute method JPI-5S-49-97 “Hydrocarbon Type Test Method—High Performance Liquid Chromatograph Method” published by the Japan Petroleum Institute. Means the capacity percentage (volume%).
Linear saturated hydrocarbon content, C10-C15 nP (C10-C15 linear saturated hydrocarbon content), C11-C15 nP, C16-C20 nP using the above-mentioned GC-FID It means the value (mass%) to be measured.

The cetane index refers to a value calculated according to “Method for calculating cetane index using 8.4 variable equation” in JIS K 2280 “Petroleum products—fuel oil—octane number and cetane number test method and cetane index calculation method”. The cetane index in the JIS standard is not applied to the cetane number improver added, but the cetane index of the cetane index added with the cetane number improver also uses the above “8.4 variable equation”. It shall represent the value calculated by “Calculating method of cetane index”.
The cetane number means a cetane number measured according to “7. Cetane number test method” of JIS K 2280 “Petroleum products—fuel oil—octane number and cetane number test method and cetane index calculation method”.
The pour point refers to a pour point measured according to JIS K 2269 “Crude point of petroleum and petroleum products and a cloud point test method of petroleum products”.

Hue means the Saybolt color measured according to the Saebold color test method described in JIS K 2580 “Petroleum products—color test method”.
The reaction test refers to a reaction measured by JIS K 2252 “Petroleum products—Reaction test method”.
Copper plate corrosion refers to the classification of corrosion measured by JIS K 2252 “Petroleum products—copper plate corrosion test method”.
Moisture refers to moisture measured by the Karl Fischer coulometric titration method described in JIS K 2275 “Crude oil and petroleum products—moisture test method”.
The residual carbon content of 10% residual oil means the residual carbon content of 10% residual oil as measured by JIS K 2270 “Crude oil and petroleum products—residual carbon content test method”.
The peroxide value (peroxide value) after the oxidation stability test is accelerating oxidation under conditions of 95 ° C. and oxygen bubbling for 16 hours in accordance with ASTM D2274-94, and then the Petroleum Institute Standard JPI-5S- It means a value measured according to 46-96.
The total insoluble content after the oxidation stability test (total insoluble content) means a value measured after accelerated oxidation under conditions of 95 ° C. and oxygen bubbling for 16 hours in accordance with ASTM D2274-94. .
The conductivity means a value measured in accordance with JIS K 2276 “Petroleum product-aviation fuel oil test method”.
Lubrication performance and HFRR wear scar diameter (WS1.4) refer to the lubrication performance measured by the Petroleum Institute Standard JPI-5S-50-98 “Diesel Oil-Lubricity Test Method” issued by the Japan Petroleum Institute. .

As shown in Table 3, the fuel compositions used in Examples and Comparative Examples are prepared by blending a hydrocarbon base material obtained through a specific process and an FT synthetic base material having a specific property at a specific ratio. As is apparent from Table 3, in Examples 1 to 4 blended under the conditions specified in the present invention using the base material manufactured through a predetermined process, the fuel composition satisfying the specified properties Things could be obtained easily and reliably. On the other hand, in Comparative Examples 1 and 2 in which the fuel composition was prepared without using the specific fuel substrate, the fuel composition targeted by the present invention is not necessarily obtained.

  Next, using the fuel compositions of Examples 1 to 4 and Comparative Examples 1 to 2, various tests shown below were performed. All test results are shown in Table 4. As can be seen from the results in Table 4, the fuel compositions of Examples 1 to 4 were compared with the fuel compositions of Comparative Examples 1 and 2, and the combustion property confirmation test in the stove, the white smoke measurement test at low temperature startability, Good results have been obtained in exhaust gas performance tests, low-temperature storage tests, etc., and low temperature fluidity in a very low temperature region, which has been difficult to realize with conventional fuel compositions, flexibility that can support multiple applications, and environmental response It can be confirmed that a fuel composition for cryogenic regions satisfying all the performance as a mold fuel is provided.

(Combustion confirmation test with a core-type stove)
Test the fuel in a core type oil stove (SX-E261Y manufactured by Corona Co., Ltd., manufactured in 2004, heating output: 2.56 to 2.05 kW) that was left in an environment of -30 ° C, and perform a normal ignition operation. When there is no ignition failure, misfire, red fire, black smoke, white smoke at the time of ignition, and the case where the same abnormal combustion does not occur when burned for 10 minutes after that, it is determined as pass (○). When abnormal combustion occurred, the test was rejected (x). In addition, the test method concerning the combustion confirmation test in the heart-type stove was carried out in accordance with JIS S 3031 “General Rules for Test Methods for Petroleum Combustion Equipment”.

(Measurement of white smoke at low temperature start)
On a chassis dynamometer capable of controlling the environmental temperature, at room temperature, (1) flush the fuel system of the Diesel vehicle with the evaluation fuel, (2) extract the flushing fuel, and (3) remove the main filter Replacing with a new one, (4) Applying the specified amount of fuel to the fuel tank (1/2 of the fuel tank capacity of the test vehicle). Thereafter, (5) the ambient temperature is rapidly cooled from room temperature to −20 ° C., (6) held at −20 ° C. for 1 hour, and (7) to a predetermined temperature (−30 ° C.) at a cooling rate of 1 ° C./h. (8) Hold the engine at a predetermined temperature for 1 hour, and then start the engine. If cranking for 10 seconds is repeated twice at 30-second intervals, it cannot be measured. If the engine can be started, leave it idle for 30 seconds, then repeat the operation of depressing the accelerator pedal to fullness in 5 seconds, and measure the white smoke at that time with a transmission type measuring instrument. The average value of 5 times was computed, the result of the comparative example 1 was set to 100, and each result was compared and quantified relatively.

(Vehicle exhaust gas test)
Fuel consumption was measured using a diesel engine-equipped vehicle (vehicle 1) shown below. The test mode was a transient operation mode simulating actual traveling shown in FIG. The smoke measurement uses a transmission type measuring instrument. For each exhaust gas performance value, the test result in Comparative Example 1 was set to 100, and each result was relatively compared and quantified. In addition, the test method relating to the vehicle test is in accordance with Annex 27 “Technical Standards for Diesel Vehicle 10/15 Mode Emission Measurement”, supervised by the former Ministry of Transport.
(Vehicle specifications): Vehicle 1
Engine type: Supercharged inline 4 cylinder diesel engine with intercooler Displacement: 3L
Compression ratio: 18.5
Maximum output: 125kW / 3400rpm
Maximum torque: 350Nm / 2400rpm
Regulatory compliance: 1997 exhaust gas regulatory compliance Vehicle weight: 1900 kg
Mission: 4AT
Exhaust gas aftertreatment device: oxidation catalyst

(Low temperature storage test)
The target fuel composition is stored in a freezer that can be controlled at a constant temperature of -30 ° C for one month. After the storage, the appearance of the fuel composition is checked. In addition, the supernatant of the fuel composition after storage (portion within 1 cm from the liquid surface) is sampled and pour point measurement is performed, and the case where the same performance as before storage is obtained is indicated as “good”.

It is a figure which shows the transient operation mode which simulated real driving | running | working.

Claims (6)

Initial boiling point is 140 ° C. or higher and 200 ° C. or lower, distillation property 90% by volume distillation temperature is 200 ° C. or higher and 300 ° C. or lower, aromatic content is 20% by volume or lower, and linear saturated hydrocarbon content is 25% by mass or higher. The following steps (1) to (3) are carried out using a hydrocarbon mixture A having a straight-chain saturated hydrocarbon content of 10 to 15 carbon atoms and a sulfur content of 300 mass ppm or less as a feedstock. The hydrocarbon mixture D obtained through the process contains 80% by volume or more of the total fuel composition, the Saybolt color is +28 or more, the density at 15 ° C. is 740 kg / m ³ or more and 840 kg / m ³ or less, and the distillation property is 10% distillate. Temperature is 170 ° C. or higher and 220 ° C. or lower, 90% distillation temperature is 220 ° C. or higher and 300 ° C. or lower, cetane index 45 or higher, cetane number 48 or higher, flash point 45 ° C. or higher, reaction test result is neutral, copper plate corrosion is 1 Less than Peroxide after the accelerated oxidation test is 10 ppm by mass or less, a pour point -60 ° C. or less, a sulfur content of 10 ppm by mass, kinematic viscosity at 30 ° C. is 1.6 mm ² / s or more 5.0 mm ² / s or less, - Cryogenic viscosity at 30 ° C. of 30 mm ² / s or less, moisture content of 0.01% by volume or less, residual carbon content of 10% residual oil of 0.1% by mass or less, fuel for cryogenic regions Composition.
Step (1): The hydrocarbon mixture A is reacted at a reaction temperature of 250 ° C. or higher and 310 ° C. or lower, a hydrogen pressure of 5 MPa or higher and 10 MPa or lower, LHSV 0.5h ⁻¹ or higher and 3.0h ⁻¹ or lower, and a hydrogen / hydrocarbon capacity ratio of 0.15 or higher. Hydrodesulfurization treatment is performed with a catalyst containing any of Ni-W, Ni-Mo, Co-Mo, Co-W, or Ni-Co-Mo under conditions of 0.6 or less to obtain a hydrocarbon mixture B. Step Step (2): A step of removing a light portion of the hydrocarbon mixture B in the range of 1% by volume or more and 40% by volume or less to obtain a hydrocarbon mixture C. Step (3): The hydrocarbon mixture C is reacted at a reaction temperature of 150 ° C. The process of obtaining the hydrocarbon mixture D which removed the linear saturated hydrocarbon 10 volume% or more with the zeolite on the conditions above 250 degreeC or less and pressure 1MPa or more and 5MPa or less Initial boiling point is 140 ° C. or higher and 200 ° C. or lower, distillation property 90% by volume distillation temperature is 200 ° C. or higher and 300 ° C. or lower, aromatic content is 20% by volume or lower, and linear saturated hydrocarbon content is 25% by mass or higher. The following steps (1) to (3) are carried out using a hydrocarbon mixture A having a straight-chain saturated hydrocarbon content of 10 to 15 carbon atoms and a sulfur content of 300 mass ppm or less as a feedstock. The hydrocarbon mixture D obtained through 80 to 100% by volume with respect to the total fuel composition, the total content of linear saturated hydrocarbon compounds having 16 to 20 carbon atoms is 10% by mass or less, and 21 carbon atoms It contains 0 to 20% by volume of an FT synthetic base material having a total content of straight chain saturated hydrocarbon compounds of 2 or less and 25 or less, and a Savort color +28 or more and a density at 15 ° C. of 740 kg / m ³ or more and 840 kg. / M ³ or less, distillation property 10% distillation temperature is 170 ° C to 220 ° C, 90% distillation temperature is 220 ° C to 300 ° C, cetane index 45 or more, cetane number 48 or more, flash point 45 ° C or more, reaction test Results in neutral, copper plate corrosion is 1 or less, peroxide value after accelerated oxidation test is 10 mass ppm or less, pour point is −60 ° C. or less, sulfur content is 10 mass ppm or less, and kinematic viscosity at 30 ° C. is 1.6 mm ^2. / S or more and 5.0 mm ² / s or less, kinematic viscosity at −30 ° C. is 30 mm ² / s or less, moisture content is 0.01% by volume or less, and 10% residual oil has a residual carbon content of 0.1% by mass or less. A fuel composition for cryogenic regions, characterized by
Step (1): The hydrocarbon mixture A is reacted at a reaction temperature of 250 ° C. or higher and 310 ° C. or lower, a hydrogen pressure of 5 MPa or higher and 10 MPa or lower, LHSV 0.5h ⁻¹ or higher and 3.0h ⁻¹ or lower, and a hydrogen / hydrocarbon capacity ratio of 0.15 or higher. Hydrodesulfurization treatment is performed with a catalyst containing any of Ni-W, Ni-Mo, Co-Mo, Co-W, or Ni-Co-Mo under conditions of 0.6 or less to obtain a hydrocarbon mixture B. Step Step (2): A step of removing a light portion of the hydrocarbon mixture B in the range of 1% by volume or more and 40% by volume or less to obtain a hydrocarbon mixture C. Step (3): The hydrocarbon mixture C is reacted at a reaction temperature of 150 ° C. The process of obtaining the hydrocarbon mixture D which removed the linear saturated hydrocarbon 10 volume% or more with the zeolite on the conditions above 250 degreeC or less and pressure 1MPa or more and 5MPa or less   The fuel composition for cryogenic regions according to claim 1 or 2, wherein the hydrocarbon mixture A is an FT synthesis base material.   The fuel composition for a cryogenic region according to claim 1 or 2, wherein the hydrocarbon mixture A is a processing oil derived from a vegetable oil.   The fuel composition for cryogenic regions according to any one of claims 1 to 4, wherein an antifreezing agent is added in an amount of 100 mass ppm to 500 mass ppm. The low temperature fluidity improver is added in an active ingredient concentration of 200 mg / L or more and 1000 mg / L or less, and the lubricity improver is added in an active ingredient concentration of 20 mg / L or more and 200 mg / L or less. The fuel composition for cryogenic regions as described.

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