JP2013001842A - Gasoline composition and method for producing gasoline composition - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a gasoline composition compounded with a gasoline base material high in the content of a high octane number component by FT reaction, and to provide a method for producing the gasoline composition.SOLUTION: There is provided the gasoline composition compounded with 1-60 vol.% of the gasoline fraction of a product obtained by Fischer-Tropsch (FT) reaction from a gas containing hydrogen and carbon monoxide as main components in the presence of a hydrocarbon production catalyst composition comprising one or more metals exhibiting activity on the Fischer-Tropsch (FT) reaction, manganese carbonate, and zeolite exhibiting a solid acid, wherein the content of the zeolite in the catalyst composition is >65 and ≤80 mass%, wherein (a) RON (research octane number) is ≥89 and <93; (b) MON (motor octane number)is ≥79 and <84; (c) aromatic compound content is 10-40 vol.%; (d) the content of olefins is at most 40 vol.%; (e) the benzene content is at most 1 vol.%; (f) the sulfur content is at most 10 mass.ppm; (g) RVP (Reid vapor pressure) is >65 kPa and ≤93 kPa, and (h) the 50 vol% distillation temperature is 75-110°C.

Description

 The present invention relates to a gasoline composition and a gasoline composition containing a gasoline base material produced by a Fischer-Tropsch (FT) reaction from a mixed gas containing hydrogen and carbon monoxide as main components (hereinafter referred to as “synthesis gas”). It relates to the manufacturing method. More specifically, a gasoline composition and gasoline containing a gasoline base material obtained by an FT reaction using a catalyst composition for producing hydrocarbons containing an FT active metal, manganese carbonate, and a zeolite showing a solid acid. The present invention relates to a method for producing a composition.

 As a method for synthesizing hydrocarbons from synthesis gas, a Fischer-Tropsch reaction (hereinafter referred to as “FT reaction”), a methanol synthesis reaction, and the like are well known. The FT reaction is a catalyst that uses an iron group element of iron, cobalt, nickel, or a platinum group element such as ruthenium as an active metal. On the other hand, it is known that methanol synthesis reaction proceeds with a copper-based catalyst and C2 oxygen-containing (ethanol, acetaldehyde, etc.) synthesis proceeds with a rhodium-based catalyst (see, for example, Non-Patent Document 1).

By the way, in recent years, gas oil with low sulfur content has been desired from the viewpoint of the preservation of the air environment, and this trend is expected to become stronger in the future. In addition, from the viewpoint that crude oil resources are limited and from the viewpoint of energy security, the development of alternative fuels for oil is desired, and it is expected that this will become increasingly desirable in the future. As a technology to meet these demands, GTL (gas to liquids) is a technology that synthesizes liquid fuel such as kerosene from natural gas (main component methane), which is said to have recoverable reserves equivalent to crude oil in terms of energy. is there. Since natural gas does not contain sulfur or is hydrogen sulfide (H ₂ S) or the like that is easy to desulfurize even if it contains, liquid fuel such as kerosene obtained has almost no sulfur in it. In addition, because of the advantage that it can be used for high-performance diesel fuel having a high cetane number, this GTL has been increasingly attracting attention in recent years.

 As part of the GTL, methods for producing hydrocarbons from synthesis gas by the FT reaction have been actively studied. The hydrocarbons obtained by this FT reaction are a wide range of hydrocarbons ranging from methane to wax and trace amounts of oxygen-containing compounds such as various alcohols, and cannot selectively produce a specific fraction. Therefore, for example, in order to efficiently obtain a kerosene fraction by the FT reaction, in addition to the straight kerosene fraction produced by the FT reaction, a heavier wax fraction is hydrocracked. It is common practice to produce a kerosene fraction and increase the yield of the kerosene fraction.

 On the other hand, a gasoline fraction can also be obtained by FT reaction. However, since the hydrocarbons produced by the FT reaction are mainly composed of linear paraffin, the gasoline fraction obtained by the FT reaction has a very low octane number and is not practical. Normally, the octane number of hydrocarbons is the highest for aromatic hydrocarbons, and then decreases in the order of naphthenic hydrocarbons, olefinic hydrocarbons, and paraffinic hydrocarbons. In the case of the same family hydrocarbons, the lower the number of carbon atoms, the lower the boiling point, the higher the octane number, and the higher the number of carbon atoms with the same number of branches.

 Conventionally, a method for producing a gasoline fraction by decomposing and isomerizing a hydrocarbon produced by an FT reaction with a solid acid catalyst such as zeolite has been proposed. For example, using a FT synthesis catalyst containing FT active metal species such as ruthenium and cobalt (metal species showing activity in FT reaction) and a catalyst in which ZSM-5 and β zeolite coexist, the synthesis gas is converted into gasoline by a one-step reaction. A method for producing a fraction (one-stage method) has been proposed (see, for example, Patent Documents 1 and 2). In addition, a method (two-stage method) for producing a gasoline fraction by reacting at an optimum temperature by a two-stage reaction of a reaction with an FT synthesis catalyst and a reaction with a solid acid catalyst has also been proposed (for example, (See Patent Document 3). In addition, a method for highly selective synthesis of isoparaffin is proposed by using a catalyst for FT synthesis in which a FT active metal species such as cobalt or ruthenium is dispersed or supported by sputtering on the surface of a powdery carrier made of zeolite. (For example, refer to Patent Document 4).

 By the way, the production of product gasoline is made according to seasonal changes. For example, in winter, the vapor pressure of product gasoline is higher than in other seasons in order to improve cold startability. Specifically, in order to increase the vapor pressure, the blending ratio of the mixed butane fraction is increased. However, when the mixed butane fraction is added in an increased amount, there is a problem that the calorific value of the product gasoline decreases. Thus, there is a demand for a gasoline base material having a high vapor pressure, a high calorific value, and a high octane number, particularly in winter.

JP 62-109888 A JP 2007-197628 A JP 2001-288123 A JP 2009-106863 A

“C1 Chemistry”, edited by the Catalysis Society of Japan, published by Kodansha, 1984, page 25.

The conventional one-stage method has a problem that both reactions cannot be performed efficiently because the optimum reaction temperature ranges of the FT synthesis catalyst and the solid acid catalyst are different. For example, when the reaction is carried out at a relatively low temperature that is optimal for an FT synthesis catalyst, the production of lower hydrocarbons such as CH ₄ is suppressed and higher hydrocarbons having 5 or more carbon atoms are efficiently produced. The activity of the catalyst is low, the decomposition and isomerization reaction of the produced hydrocarbons are lowered, the gasoline yield is lowered, and the production of high octane hydrocarbons such as aromatic hydrocarbons and branched hydrocarbons is also lowered. Conversely, when the reaction is carried out at an optimum temperature for the solid acid catalyst, the FT reaction promotes the generation of gas components such as lower hydrocarbons such as CH ₄ and CO _2, resulting in a decrease in gasoline yield. .

 On the other hand, in the two-stage method, the reaction can proceed at the optimum temperature of each catalyst, and a gasoline fraction can be efficiently produced. However, since hydrogen is introduced before the second stage reaction to proceed with hydrocracking, isoparaffin in the product is produced, but there is a problem that the olefin content is reduced and the octane number is lowered.

 Moreover, although the hydrocarbons synthesized by the FT synthesis catalyst described in Patent Document 4 have a high isoparaffin content, the content of aromatic compounds is low and the octane number is not sufficient, and they are used as a gasoline base material. Is not enough.

 In the present invention, a gasoline composition and a gasoline composition containing a gasoline base material having a high content of high octane components such as aromatics, naphthenes, olefins, and branched paraffin hydrocarbons, which are products obtained by the FT reaction. It aims at providing the manufacturing method of a thing.

 As a result of researches to achieve the above-mentioned object, the inventors of the present invention contain a metal that exhibits activity in the FT reaction, manganese carbonate, and a zeolite that exhibits a solid acid, and the content of the zeolite relative to the catalyst composition. By using a catalyst composition with a specific ratio, it was found that a high-octane gasoline fraction rich in aromatics, naphthenes, olefins and branched paraffins can be produced by the FT reaction, and the present invention was completed. It came to do.

That is, the present invention
(1) It contains one or more metals that are active in the Fischer-Tropsch reaction, manganese carbonate, and a zeolite that shows a solid acid, and the content of the zeolite with respect to the catalyst composition is more than 65% by mass. A gasoline fraction of a product obtained by a Fischer-Tropsch reaction from a gas mainly composed of hydrogen and carbon monoxide using a catalyst composition for producing hydrocarbons having a mass% or less, and other gasoline base materials And the gasoline fraction is 1-60% by volume,
(A) The research octane number is 89 or more and less than 93,
(B) Motor method octane number is 79 or more and less than 84,
(C) Aromatic ratio is 10 to 40% by volume,
(D) at most 40% by volume of olefins,
(E) at most 1% by volume of benzene,
(F) At most 10 ppm by mass of sulfur,
(G) Reed vapor pressure is greater than 65 kPa and less than or equal to 93 kPa,
(H) 50 vol% distillation temperature is 75-110 ° C
A method for producing a gasoline composition, characterized by producing a gasoline composition that is
(2) containing at least one metal active in the Fischer-Tropsch reaction, manganese carbonate, and a zeolite showing a solid acid, and the content of the zeolite with respect to the catalyst composition is more than 65% by mass 1 to 60% by volume of a gasoline fraction of a product obtained by a Fischer-Tropsch reaction from a gas mainly composed of hydrogen and carbon monoxide using a catalyst composition for producing hydrocarbons having a mass% or less A gasoline composition contained,
(A) The research octane number is 89 or more and less than 93,
(B) Motor method octane number is 79 or more and less than 84,
(C) Aromatic ratio is 10 to 40% by volume,
(D) at most 40% by volume of olefins,
(E) at most 1% by volume of benzene,
(F) At most 10 ppm by mass of sulfur,
(G) Reed vapor pressure is greater than 65 kPa and less than or equal to 93 kPa,
(H) 50 vol% distillation temperature is 75-110 ° C
A gasoline composition, characterized in that
(3) The catalyst composition contains a Fischer-Tropsch synthesis catalyst containing one or more metals and manganese carbonate active in a Fischer-Tropsch reaction, and a zeolite showing a solid acid. (2) The gasoline composition according to
(4) The gasoline composition according to (2) or (3), wherein the metal is ruthenium,
(5) The gasoline composition according to any one of (2) to (4), wherein the zeolite is ZSM-5,
Is to provide.

 According to the present invention, the content of high-octane components such as aromatics, naphthenes, olefins, and branched paraffin hydrocarbons is not only contained, but also contains only sulfur content that does not contain sulfur or can be easily desulfurized. By including an excellent gasoline base material having a high value, it is possible to provide a gasoline composition that contributes to environmental problems and energy security problems, and a method for producing the gasoline composition.

<Gasoline composition>
The gasoline composition of the present invention contains one or more metals that are active in the FT reaction, manganese carbonate, and a zeolite that exhibits a solid acid, and the content of the zeolite relative to the catalyst composition is 65% by mass. A gasoline fraction (FT gasoline fraction) synthesized by a Fischer-Tropsch reaction from a gas mainly composed of hydrogen and carbon monoxide using a catalyst composition for producing hydrocarbons having a mass of 80% by mass or less 1 to 60% by volume of a gasoline composition having the following properties.
(A) The research octane number is 89 or more and less than 93,
(B) Motor method octane number is 79 or more and less than 84,
(C) Aromatic ratio is 10 to 40% by volume,
(D) at most 40% by volume of olefins,
(E) at most 1% by volume of benzene,
(F) At most 10 ppm by mass of sulfur,
(G) Reed vapor pressure is greater than 65 kPa and less than or equal to 93 kPa,
(H) 50 vol% distillation temperature is 75-110 ° C

Hereinafter, the contents of the present invention will be described in more detail.
The research method octane number (RON) of the gasoline composition of the present invention is 89 or more and less than 93, preferably 89 to 92, more preferably 89 to 91. Moreover, the motor method octane number (MON) of the gasoline composition of this invention is 79 or more and less than 84, Preferably it is 79-83, More preferably, it is 79-82. When the RON is 89 or more, it is possible to maintain high exercise performance, and when the MON is 79 or more, it is possible to prevent a decrease in anti-knock property during high-speed running. In addition, in this invention and this-application specification, RON and MON of a gasoline composition mean the value measured according to JISK2280.

 The aromatics ratio of the gasoline composition of the present invention is 10 to 40% by volume, preferably 15 to 40% by volume. The proportion of olefins in the gasoline composition of the present invention is at most 40% by volume, preferably 1 to 35% by volume. If the aromatic ratio is 40% by volume or less, an increase in harmful components in the exhaust gas can be prevented, the aromatics ratio is 10% by volume or more, and the olefin ratio is at most 40% by volume. As a result, the RON and MON of the gasoline composition of the present invention can be increased. In the present invention and the specification of the present application, the ratio of aromatics and olefins in the gasoline composition means values measured using a Capillary column (TC-1) and a flame ionization detector. .

 The 50 vol% distillation temperature (T50) of the gasoline composition of the present invention is 75 to 110 ° C, preferably 75 to 105 ° C. The 90% by volume distillation temperature (T90) is preferably at most 180 ° C, more preferably 120 to 175 ° C. Moreover, 70 degreeC distillation capacity | capacitance (E70) becomes like this. Preferably it is 18-45 volume%, More preferably, it is 20-45 volume%. When T50, T90, and E70 are in this range, it is possible to prevent a case where a problem occurs in startability, drivability, and acceleration. In addition, in this invention and this-application specification, the distillation property of a gasoline composition means the value measured according to JISK2249.

 The lead vapor pressure (RVP) of the gasoline composition of the present invention is greater than 65 kPa and less than or equal to 93 kPa, preferably 70 to 93 kPa. When RVP is 93 kPa or less, the amount of evaporative gas can be reduced, and when it is greater than 65 kPa, it is possible to prevent the low-temperature startability and warming-up from being deteriorated. In addition, in this invention and this-application specification, RVP of a gasoline composition means the value measured according to JISK2258.

 The gasoline composition of the present invention has a sulfur content of at most 10 ppm by weight, preferably at most 5 ppm by weight, and more preferably at most 1 ppm by weight. It is preferable that the sulfur content is as low as 10 ppm by mass because poisoning of the automobile exhaust gas catalyst can be suppressed. In addition, in this invention and this-application specification, the sulfur content of a gasoline composition means the value measured according to JISK2541.

The density at 15 ° C. of the gasoline composition of the present invention is preferably 0.680 to 0.783 g / cm ³ , more preferably 0.685 to 0.770 g / cm ³ . When the density at 15 ° C. is in this range, good fuel efficiency can be secured when blended with product gasoline. In addition, in this invention and this-application specification, the density in 15 degreeC of a gasoline composition means the value measured according to JISK2249.

 The benzene content of the gasoline composition of the present invention is at most 1% by volume, preferably at most 0.8% by volume. When the content ratio of benzene is as low as 1% by volume, an increase in the concentration of benzene in the atmosphere can be prevented and environmental pollution can be reduced. In addition, in this invention and this-application specification, the content rate of the benzene of a gasoline composition means the value measured according to JISK2536.

 The other hydrocarbon composition of the gasoline composition of the present invention is not particularly limited. For example, naphthenes are 2 to 15% by volume, preferably 4 to 15% by volume. It is preferable that the naphthene content is in this range because the fuel efficiency of the automobile may be improved. In the present invention and the present specification, the composition ratio of each hydrocarbon in the gasoline composition means a value measured according to JIS K2536.

The gasoline composition of the present invention contains 1 to 60% by volume, preferably 3 to 60% by volume, of a gasoline fraction obtained by FT reaction using the catalyst composition according to the present invention. By containing 1% by volume or more of the gasoline base derived from the FT reaction, it is preferable in terms of CO ₂ reduction by using the gasoline base derived from the FT reaction using biomass as a raw material, and by containing 60% by volume or less The distillation property, RVP, and composition are preferable because they can be within the preferable range of gasoline.

The base material used for producing the gasoline composition of the present invention is not particularly limited except for the gasoline base derived from the FT reaction. For example, various petroleum oils such as the following base materials (a) to (h) Various materials can be used so as to satisfy the properties defined above, using a fraction or a compound as a base material.
(B) Hydrogen stream by catalytic reforming method (Platforming method, Magnaforming method, Aromaizing method, Reforming method, Food reforming method, Ultraforming method, Powerforming method, etc.) In which the benzene fraction is removed by distillation from a reformed gasoline obtained by contact treatment with a catalyst (for example, platinum, rhodium and chlorine supported on an alumina carrier) at high temperature and pressure. Quality gasoline. When blended with debenzene-catalyzed reformed gasoline, it is preferable to blend 5 to 50% by volume.
(B) The reformed gasoline obtained by contact treatment by the above catalytic reforming method is separated into light fraction, benzene fraction, and heavy fraction by distillation. Gasoline) and heavy fractions (debenzene heavy catalytic reforming gasoline). When blending debenzene light contact reformed gasoline, it is preferable to blend 1-30% by volume. When blending debenzene heavy contact reformed gasoline, it is preferable to blend 10 to 50% by volume.
(C) Petroleum fraction from kerosene / light oil to atmospheric residual oil, preferably heavy gas oil or vacuum gas oil, is conventionally known catalytic cracking method, especially fluid catalytic cracking method (UOP method, shell two-stage type) Decomposition with solid acid catalyst (for example, silica-alumina blended with zeolite, etc.) by the method, flexi cracking method, ultra ortho flow method, texaco method, Gulf method, ultra cat cracking method, RCC method, HOC method, etc. Catalytic cracking gasoline. When blending catalytic cracking gasoline, it is preferable to blend 1 to 70% by volume.
(D) Alkylate obtained by reacting isobutane with lower olefins (butene, propylene, etc.) in the presence of an acid catalyst (sulfuric acid, hydrogen fluoride, aluminum chloride, etc.). When blending an alkylate, it is preferable to blend 1-20% by volume.
(E) A C4 fraction mainly composed of butane and butenes obtained by distillation during the atmospheric distillation of crude oil or crude oil, during the production of reformed gasoline, or during the production of cracked gasoline. When mix | blending a C4 fraction, it is preferable to mix | blend 2-15 volume%.
(F) Isomerate obtained by isomerization of straight-chain lower paraffin hydrocarbons, isopentane obtained by precision distillation of isomerate, toluene, xylene obtained from catalytically reformed gasoline, or aroma having 9 or more carbon atoms Ingredients mainly composed of tribes. When mix | blending a base material (f), it is preferable to mix | blend 1-20 volume%.
(G) Ethanol, ethyl tertiary butyl ether (ETBE), methyl tertiary butyl ether (MTBE), or tertiary aminomethyl ether (TAME), n-butanol, iso-butanol, sec-butanol, etc., which are generally used in gasoline Oxygenates. When blending an oxygen-containing compound, it is preferable to blend 1 to 25% by volume.
(H) Desulfurized light naphtha, which is a light fraction of light and heavy fractions obtained by distillation of desulfurized straight naphtha obtained by desulfurizing straight-run naphtha obtained by atmospheric distillation of crude oil. When blending desulfurized light naphtha, it is preferable to blend 5 to 45 vol%.

<FT gasoline fraction>
The FT gasoline fraction used in the gasoline composition of the present invention contains one or more metals showing activity in the FT reaction, manganese carbonate, and a zeolite showing a solid acid, and the zeolite for the catalyst composition A gasoline fraction of a product synthesized from a gas mainly composed of hydrogen and carbon monoxide using a catalyst composition for producing hydrocarbons having a content of greater than 65% by mass and not greater than 80% by mass. It has the following characteristics.
(A) Research method octane number of 85-97,
(B) Motor method octane number is 78-85,
(C) Aromatic ratio is 30-50% by volume,
(D) 1-10 volume% of olefin ratio,
(E) Oxygen content is 0.5 mass% or less,
(F) benzene is 0.5 volume% or less,
(G) C10-C11 aromatics ratio is 7-10 vol%,
(H) The sulfur content is 0.5 mass ppm or less, and (i) the naphthenes ratio is 11 to 15% by volume.

The research octane number (RON) of the FT gasoline fraction used in the gasoline composition of the present invention is 85 to 97, preferably 87 to 97, more preferably 93 to 97. Moreover, the motor octane number (MON) of the FT gasoline fraction of this invention is 78-85, Preferably it is 79-85, More preferably, it is 83-85. When RON and MON are within this range, the octane number of the gasoline containing the FT gasoline fraction used in the gasoline composition of the present invention can be increased. That is, the FT gasoline fraction used in the gasoline composition of the present invention is preferable from the viewpoint of CO ₂ reduction. In the present invention and the present specification, RON and MON of the FT gasoline fraction mean values measured according to JIS K 2280.

 The aromatic fraction of the FT gasoline fraction used in the gasoline composition of the present invention is 30 to 50% by volume, preferably 40 to 50% by volume. Moreover, the olefin ratio of the FT gasoline fraction used in the gasoline composition of the present invention is 1 to 10% by volume, preferably 1 to 5% by volume. Moreover, the ratio of naphthenes of this invention is 11-15 volume%, Preferably it is 12-15 volume%. The aromatics ratio is 30 to 50% by volume, the olefins content is 1 to 10% by volume, and the naphthenes ratio is 11 to 15% by volume. The FT gasoline fraction obtained is suitable as a gasoline base material because RON and MON are high and the calorific value is high. In addition, in this invention and this-application specification, an aromatics ratio and an olefins ratio mean the value measured according to JISK2536.

 In particular, the proportion of C10-C11 aromatics (aromatics having 10 or 11 carbon atoms) in the FT gasoline fraction used in the gasoline composition of the present invention is 7 to 10% by volume, preferably 8 to 10 volumes. %. When the C10-C11 aromatic content is within this range, the FT gasoline fraction used in the gasoline composition of the present invention is excellent in oxidation stability.

 The oxygen content of the FT gasoline fraction used in the gasoline composition of the present invention is 0.5% by mass or less, preferably 0.1% by mass. Many oxygen-containing compounds have low oxidation stability and may cause corrosion of metals and rubber. When the oxygen content is 0.5% by mass or less, the FT gasoline fraction used in the gasoline composition of the present invention has excellent oxidation stability and is suitable as a gasoline base material. In the present invention and the present specification, the oxygen content of the FT gasoline fraction means a value measured according to JIS K2536.

 The benzene content of the FT gasoline fraction used in the gasoline composition of the present invention is 0.5% by volume or less, preferably 0.4% by volume or less. Since the benzene content is as low as 0.5% by volume or less, the gasoline composition containing the FT gasoline fraction used in the gasoline composition of the present invention prevents an increase in the concentration of benzene in the atmosphere, and the environment. Contamination can be reduced. In addition, in this invention and this-application specification, the content rate of the benzene of a FT gasoline fraction means the value measured according to JISK2536.

 The sulfur content of the FT gasoline fraction used in the gasoline composition of the present invention is 0.5 mass ppm or less, preferably 0.2 mass ppm or less. Since the sulfur content is as low as 0.5 ppm by mass or less, the FT gasoline composition of the present invention is preferable because poisoning of the automobile exhaust gas catalyst can be suppressed. In addition, in this invention and this-application specification, the sulfur content of a FT gasoline fraction means the value measured according to JISK2541.

The density of the FT gasoline fraction used in the gasoline composition of the present invention at 15 ° C. is preferably 0.7300 to 0.7900 g / cm ³ , more preferably 0.7500 to 0.7900 g / cm ³ . . When the density at 15 ° C. is in this range, good fuel efficiency can be secured when blended with product gasoline. In addition, in this invention and this-application specification, the density in 15 degreeC means the value measured according to JISK2249.

 The 50 volume% distillation temperature (T50) of the FT gasoline fraction used in the gasoline composition of the present invention is preferably 90.0-125.0 ° C, more preferably 100.0-125.0 ° C. Yes, more preferably 110.0-125.0 ° C. Moreover, 90 volume% distillation temperature (T90) of the FT gasoline fraction used for the gasoline composition of this invention becomes like this. Preferably it is 165.0-180.0 degreeC, More preferably, it is 165.0-170.0. ° C, more preferably 166.0 to 170.0 ° C. Moreover, 70 degreeC distillate capacity | capacitance (E70) of the FT gasoline fraction used for the gasoline composition of this invention becomes like this. Preferably it is 18-45 volume%, More preferably, it is 20-45 volume%. When T50, T90 and E70 are within this range, the distillation properties of the FT gasoline fraction used in the gasoline composition of the present invention and the distillation properties of the product gasoline are equivalent. Therefore, even when the FT gasoline fraction used in the gasoline composition of the present invention is highly blended, it is possible to prevent the occurrence of problems in the startability, drivability, and acceleration of the obtained gasoline. In addition, in this invention and this-application specification, the distillation property of a gasoline composition means the value measured according to JISK2249.

 The RVP of the FT gasoline fraction used in the gasoline composition of the present invention is preferably 35.0 to 80.0 kPa, more preferably 44.0 to 80.0 kPa. In order to improve the cold startability of the product gasoline in winter, the RVP is usually increased by adding more mixed butane. When the RVP of the FT gasoline fraction used in the gasoline composition of the present invention is within this range, the FT gasoline fraction used in the gasoline composition of the present invention is added to the product without lowering the RVP of the product gasoline. Can be made. Furthermore, the compounding quantity of mixed butane can be suppressed by mix | blending more FT gasoline fractions used for the gasoline composition of this invention, and also the fall of the emitted-heat amount can also be suppressed.

 Since the FT gasoline fraction used in the gasoline composition of the present invention has both high RON and MON and low sulfur content, it can be used as it is by blending it into gasoline. In order to further reduce the sulfur content, the FT gasoline fraction used in the gasoline composition of the present invention may be further desulfurized and blended with gasoline.

 Since the present invention is an FT gasoline fraction having a high octane number, it can be blended at a high ratio even with a product gasoline having a defined octane number. Like the FT gasoline fraction used in the gasoline composition of the present invention, the gasoline fraction obtained from the FT reaction that obtains the gasoline fraction from carbon monoxide and hydrogen is blended with the product gasoline at a high ratio as a gasoline base. This is preferable from the viewpoint of energy security problems and environmental load reduction. When the FT gasoline fraction used in the gasoline composition of the present invention is produced, the above effect is further increased by using the biomass-derived raw material gas.

<Catalyst composition for hydrocarbon production>
The FT gasoline fraction used in the gasoline composition of the present invention comprises, for example, one or more metals that are active in the FT reaction, manganese carbonate, and a solid acid in a predetermined ratio, as shown below. It is possible to synthesize by a FT reaction by using a catalyst composition for producing hydrocarbons containing a zeolite having the following formula. Hereinafter, a hydrocarbon-producing catalyst composition suitable for producing an FT gasoline fraction used in the gasoline composition of the present invention (hereinafter, sometimes referred to as “catalyst composition used in the present invention”). explain.

 Examples of the FT active metal species constituting the catalyst composition used in the present invention include nickel, cobalt, iron, and ruthenium. Among them, ruthenium is preferably selected as a more active metal species. Moreover, these metal seed | species can also be used independently and can also be used in mixture of 2 or more types.

 As manganese carbonate which comprises the catalyst composition used for this invention, a commercially available reagent may be used and what was manufactured by the conventionally well-known method may be used. A conventionally known method for producing manganese carbonate includes a method of reacting a soluble manganese salt solution with ammonia or an alkali carbonate solution. Manganese carbonate can also be obtained by reaction of divalent manganese ions with carbonate ions or bicarbonate ions.

 The zeolite constituting the catalyst composition used in the present invention is not particularly limited as long as it is a zeolite showing a solid acid, and can be appropriately selected from known zeolites. The solid acid is one in which the surface of the solid exhibits Bronsted acidity or Lewis acidity, and is active in homogeneous or heterogeneous acid-catalyzed reactions. Hydrocarbons synthesized by the FT reaction are hydrocracked or isomerized by contacting the acid on the solid surface of the zeolite.

 Preferred zeolites include ZSM-5, β zeolite, Y-type zeolite, USY zeolite, mordenite and the like, with ZSM-5 being particularly preferred. As the zeolite, a commercially available product may be used, or a product hydrothermally synthesized by a known method may be used. These zeolites usually contain an alkali metal as an ion-exchangeable cation. However, the zeolite used in the catalyst composition used in the present invention contains 50% or more of protons, alkaline earth metal ions, transitions. Those substituted with metal ions or rare earth metal ions and having solid acidity are preferred, and H (proton) -ZSM-5 is particularly preferably used.

 The catalyst composition used for this invention should just contain FT active metal seed | species, manganese carbonate, and a zeolite, and may contain the other component, unless the effect of this invention is impaired. Further, the catalyst composition used in the present invention may be prepared using any conventionally known method. For example, the catalyst composition used in the present invention can be prepared by separately preparing an FT synthesis catalyst containing FT active metal species and manganese carbonate and a zeolite, and then physically mixing the two. . The catalyst composition used in the present invention can also be prepared by impregnating and supporting an FT active metal on a composite molded body of manganese carbonate and zeolite.

 As a method for synthesizing an FT synthesis catalyst containing FT active metal species and manganese carbonate, for example, there is a method of impregnating and supporting FT active metal species on manganese carbonate. The loading of the FT active metal species on the manganese carbonate is carried out by ordinary impregnation loading. For example, manganese carbonate is immersed in an aqueous solution of ruthenium salt so that the ruthenium salt is impregnated in manganese carbonate, and then dried and fired. When two or more metals are supported on manganese carbonate as the FT active metal species, an aqueous solution containing both a ruthenium salt and a cobalt salt is prepared, and the aqueous solution is impregnated with manganese carbonate, followed by drying and firing. There may be a stage system in which a ruthenium salt aqueous solution and a cobalt salt aqueous solution are impregnated separately in manganese carbonate and then dried and fired, and there is no particular limitation.

 Examples of the ruthenium salt include water-soluble ruthenium salts such as ruthenium chloride, ruthenium nitrate, ruthenium acetate, and ruthenium hexaammonium chloride. The ruthenium salt solution used for impregnation support can be replaced with an aqueous solution and an organic solvent such as alcohol, ether, or ketone. In this case, a salt that is soluble in various organic solvents is selected.

 The content of ruthenium in the FT synthesis catalyst is preferably 0.1 to 5% by mass, more preferably 0.3 to 4.5% by mass, and still more preferably 0.1% by mass in terms of the amount of metal with respect to the FT synthesis catalyst standard. It is 5-4 mass%. The ruthenium content is related to the number of active sites. If the ruthenium content is less than 0.1% by mass, the number of active sites may be insufficient and sufficient catalytic activity may not be obtained. On the other hand, when the content of ruthenium exceeds 5% by mass, the ruthenium is not sufficiently supported on the carrier such as manganese carbonate, and the dispersibility is reduced and the ruthenium species not interacting with the carrier component is expressed. Is likely to occur. Therefore, excessive loading of ruthenium is not preferable because it simply increases the catalyst cost.

 The FT synthesis catalyst constituting the catalyst composition used in the present invention may contain other components as long as the FT reaction by manganese carbonate and FT active metal species is not inhibited. Examples of other components include inorganic oxides that are usually used as carriers, such as silica, alumina, and silica-alumina. The content of these carrier (inorganic oxide) components in the FT synthesis catalyst can be appropriately set as long as the effects of manganese carbonate and FT active metal species are not impaired. Generally, the carrier (content of these carrier components) 5-50% by mass is appropriate on the basis of the sum of the total amount of manganese carbonate and the content of manganese carbonate.

 Furthermore, the FT synthesis catalyst constituting the catalyst composition used in the present invention may contain an alkali metal species in addition to manganese carbonate and FT active metal species. Examples of the alkali metal species include lithium, sodium, potassium, rubidium and the like, among which sodium and potassium are preferably selected. These alkali metal species can be used alone or in combination of two or more.

 A method for adding an alkali metal species to the FT synthesis catalyst in addition to the manganese carbonate and the FT active metal species is not particularly limited. For example, in the same manner as the FT active metal species, manganese carbonate can be impregnated with an alkali metal species. Specifically, for example, an aqueous solution of sodium salt or potassium salt is impregnated with manganese carbonate, and then dried and fired. The order in which the FT active metal species and the alkali metal species are supported on the manganese carbonate is not particularly limited, and the manganese carbonate may be immersed in an aqueous solution containing both and supported simultaneously. The sodium salt or potassium salt impregnated and supported on manganese carbonate is preferably a water-soluble salt such as chloride, nitrate, acetate or carbonate.

 The content of alkali metals such as sodium and potassium in the FT synthesis catalyst is preferably 0.05 to 3% by mass, more preferably 0.05 to 2% by mass, more preferably 0.05 to 2% by mass, based on the FT synthesis catalyst standard. Preferably it is 0.1-1.5 mass%. By making the content of sodium or potassium 0.05% by mass or more, the effect of suppressing the generation amount of gas components becomes remarkable. Moreover, by setting it as 3 mass% or less, it becomes possible to suppress the production amount of a gas component, without reducing FT activity.

 After impregnating manganese carbonate with an FT active metal species such as ruthenium, drying and firing are performed. The drying at this time is performed in order to evaporate a solvent such as water used when impregnating and supporting the FT active metal species in manganese carbonate, and the temperature is preferably 80 to 200 ° C, more preferably 100 to 150 ° C. . By setting the drying temperature to 80 ° C. or higher, transpiration of water or the like can be sufficiently promoted. On the other hand, by setting the drying temperature to 200 ° C. or less, it is possible to suppress non-uniformity of the active metal component due to rapid evaporation of water or the like.

 Moreover, 150-350 degreeC is preferable, as for baking temperature, 150-300 degreeC is more preferable, and 150-250 degreeC is further more preferable. If the calcination temperature greatly exceeds 350 ° C., manganese carbonate in the catalyst component decomposes into manganese oxide and carbon dioxide gas, which is not preferable. In order to produce the FT gasoline fraction used in the gasoline composition of the present invention, it is essential that manganese carbonate as the FT synthesis catalyst component be present in the form of a carbonate. It is difficult to obtain an FT-reactive organism with a high content ratio and a high octane number. On the other hand, if the firing temperature is too low, activation of the FT active metal species cannot be achieved, which is not preferable.

 The time for drying and firing is not generally determined depending on the amount of treatment, but is usually 1 to 10 hours. If the treatment time is less than 1 hour, the transpiration of moisture may be insufficient, and the activation of the FT active metal species is diluted, which is not preferable. Further, even if the treatment time exceeds 10 hours, the catalytic activity is almost the same as the case of 10 hours or less. Therefore, in consideration of workability and productivity, 10 hours or less is preferable. The drying or baking treatment may be performed in the air, or may be an inert gas atmosphere such as nitrogen or helium, or a reducing gas atmosphere such as hydrogen, and is not particularly defined.

 In addition to the impregnation support method described above, as a method for producing an FT synthesis catalyst containing manganese carbonate and FT active metal species, an aqueous slurry containing manganese carbonate and FT active metal species is prepared and spray-dried. Can be mentioned. The concentration of the slurry at this time is not particularly specified, but if the slurry concentration is too low, manganese carbonate precipitates and the catalyst components become non-uniform, which is not preferable. On the other hand, if the slurry concentration is too high, it becomes difficult to feed the slurry, so an appropriate slurry concentration is selected. Further, at this time, silica sol or the like can be added as a binder component for the purpose of adjusting the concentration of the slurry, improving the moldability of the catalyst, and spheroidizing. The amount of the binder added at this time is preferably such that the catalyst activity is not lowered, and is generally selected in the range of 5 to 20% by mass.

 When obtaining an FT synthesis catalyst by spray drying, a method of spraying a slurry containing manganese carbonate, an FT active metal species, and a binder component at the same time, or a slurry containing manganese carbonate and a binder is sprayed, and then the impregnation described above. In accordance with the loading method, there is a method of adding FT active metal species to the obtained spray-dried product. In addition, it is preferable to implement the ventilation temperature in spray-drying method within said drying and baking temperature.

 Other methods for preparing the FT synthesis catalyst constituting the catalyst composition used in the present invention include immersing manganese carbonate in an aqueous solution of FT active metal species to adsorb the active metal on manganese carbonate, Examples include a method of attaching an active metal to manganese carbonate by ion exchange, and a method of depositing an active metal on manganese carbonate by adding a precipitant such as an alkali when immersing manganese carbonate in an aqueous solution of an FT active metal species. It is done.

 Although the above-mentioned baking treatment has the objective of activating the FT active metal species, the activation can also be achieved by an alkaline aqueous solution treatment in addition to or in addition to the baking treatment. Specifically, a post-treatment is performed in which an FT synthesis catalyst in which FT active metal species is supported on manganese carbonate is immersed in an alkaline aqueous solution. As the alkaline aqueous solution, ammonia water, sodium hydroxide aqueous solution, potassium hydroxide aqueous solution, sodium carbonate aqueous solution, potassium carbonate aqueous solution and the like can be used, and preferably ammonia water can be used. The alkali concentration in the alkaline aqueous solution is 0.05 to 1N, preferably 0.05 to 0.5N, more preferably 0.05 to 0.2N. When the alkali concentration is less than 0.05N, the effect of treating the alkaline aqueous solution becomes dilute, and there is a possibility that the catalytic activity is not so much improved even if the calcination treatment is performed thereafter. Conversely, if it exceeds 1N, the amount of unreacted alkali increases, which is uneconomical and increases the amount of water and time required for the cleaning treatment. In addition, although the time of alkaline aqueous solution treatment is based also on the density | concentration of an alkali component, 1 to 10 hours are preferable normally.

 After the treatment with an alkaline aqueous solution, the product is washed with water and the excess alkali content is sufficiently washed, and then the above-described drying and baking treatments are performed. The alkaline aqueous solution treatment is not particularly limited, and may be performed after drying or after firing after impregnating and supporting FT active metal species in manganese carbonate. Furthermore, it can also implement with respect to the catalyst obtained by performing spray drying, and the shape | molded catalyst.

 As a method of mixing the separately prepared FT synthesis catalyst and zeolite, for example, the FT synthesis catalyst and zeolite may be physically mixed to form a uniform mixture. The FT synthesis catalyst and zeolite are laminated in one container. It is good also as the laminated body filled up. In the case of a laminated body, it is sufficient that both of them are formed at least one layer. One container is filled with FT synthesis catalyst and zeolite alternately, and a layer made of FT synthesis catalyst and a layer made of zeolite are formed. It may be a laminated body laminated alternately.

 Moreover, when using a catalyst composition for an actual apparatus, shaping | molding is required, However A conventionally well-known method can be used also about shaping | molding. For example, the catalyst composition used in the present invention can be molded by subjecting a mixture of FT synthesis catalyst and zeolite to a known molding method. In addition, a catalyst composition obtained by impregnating and supporting an FT active metal on a composite molded body of manganese carbonate and zeolite by the above-described method is subjected to a known molding method, whereby the catalyst composition used in the present invention is obtained. Can be molded. Examples of such known molding methods include tableting molding, extrusion molding, and beading. In addition, these molding methods can be performed by a conventional method.

 When molding, the catalyst composition is mixed with silica or alumina as a binder component in order to improve moldability, or in order to improve extrudability, cellulosic molding aid or epoxy molding aid. It is also possible to add a molding aid such as PVA as long as it does not affect the catalytic activity.

 As a catalyst composition used for this invention, content of the zeolite in a catalyst composition is larger than 65 mass%, and is 80 mass% or less. By setting the content of the zeolite in the catalyst composition within the above range, hydrocarbons produced by the FT synthesis catalyst in the catalyst composition are efficiently decomposed or isomerized on the zeolite, and a high octane number i -As a result of conversion to paraffins, naphthenes, and aromatics, a gasoline base material having a high octane number and a large total calorific value can be produced.

 When the catalyst composition used in the present invention is a composition containing an FT synthesis catalyst and a zeolite, the content of the FT synthesis catalyst in the catalyst composition is 10% by mass or more and less than 35% by mass, preferably 20% by mass. % Or more and less than 30% by mass. When the FT synthesis catalyst is contained in an amount of 10% by mass or more, hydrocarbon generation by the FT reaction proceeds sufficiently, which is preferable. When the content of the FT synthesis catalyst is less than 35% by mass, a sufficient amount of zeolite can be contained in the catalyst composition.

By using the catalyst composition used in the present invention, the CO conversion rate of the raw synthesis gas is high, the production of gas components is small, and high octane number components such as aromatics, naphthenes, olefins, and branched paraffin hydrocarbons are used. A gasoline fraction with high selectivity can be obtained in high yield from the synthesis gas by a one-stage reaction. Details regarding the ability to produce a high-octane gasoline fraction very efficiently as compared with the conventionally known methods using the catalyst composition have not yet been elucidated and are currently under intensive investigation, It is guessed as follows. In the reaction using the catalyst composition used in the present invention, the hydrocarbons synthesized from the synthesis gas by the FT synthesis catalyst are appropriately decomposed or isomerized by contacting with the zeolite showing the solid acid. In general, in order to efficiently perform the decomposition or isomerization reaction of hydrocarbons with zeolite, it is preferable to react the zeolite at 230 ° C. or higher. In the present invention, the use of an FT synthesis catalyst containing manganese carbonate as the FT synthesis catalyst suppresses the generation of gas components such as lower hydrocarbons having 1 to 4 carbon atoms and CO ₂ even at a high reaction temperature. In addition to being able to produce hydrocarbons, it is presumed that the solid acid catalyst (zeolite) acts effectively at high temperatures, making it possible to produce a high-octane gasoline fraction.

<Method for producing FT gasoline fraction>
FT gasoline used in the gasoline composition of the present invention is a gasoline fraction (20-200 ° C.) obtained from the one-step FT reaction using the catalyst composition used in the present invention. It can be used as a fraction. The gasoline fraction can be recovered by a conventional method such as distillation.

 Examples of the type of the reactor for the FT reaction using the catalyst composition used in the present invention include a fixed bed, a fluidized bed, a suspension bed, and a slurry bed, and are not particularly limited. As an example, a method for producing hydrocarbons using a fixed bed will be described below.

 When evaluating the activity of the catalyst in a fixed bed, since the powder catalyst is concerned about the occurrence of differential pressure in the reactor, the shape of the catalyst is preferably a molded product such as an extruded product or a bead product. . The size of the catalyst composition depends on the scale of the reactor, but the particle size of the catalyst shape is preferably 0.5 mm to 5 mm, more preferably 1.0 mm to 3 mm. When the particle diameter is 0.5 mm or more, an increase in the differential pressure in the reactor can be sufficiently suppressed. On the other hand, when the particle diameter is 5 mm or less, the effectiveness factor of the catalyst can be improved, and the reaction can proceed efficiently.

 The catalyst composition used in the present invention is subjected to a reduction treatment (activation treatment) in advance before being subjected to the reaction. By this reduction treatment, the catalyst is activated so as to exhibit a desired catalytic activity in the reaction. If this reduction treatment is not performed, the FT active metal species are not sufficiently reduced and do not exhibit the desired catalytic activity. The reduction treatment temperature is preferably 140 to 350 ° C, more preferably 150 to 300 ° C. If it is less than 140 degreeC, FT active metal seed | species will not fully be reduced, and sufficient reaction activity will not be obtained. Further, at a high temperature significantly exceeding 350 ° C., there is a high possibility that decomposition of the catalyst component, manganese carbonate, into manganese oxide proceeds, leading to a decrease in activity.

 For this reduction treatment, a reducing gas mainly containing hydrogen can be preferably used. The reducing gas to be used may contain a certain amount of components other than hydrogen, for example, water vapor, nitrogen, rare gas, etc. within a range that does not hinder the reduction. This reduction treatment is affected by the hydrogen partial pressure and the treatment time as well as the treatment temperature. The hydrogen partial pressure in the reduction treatment is preferably 0.1 to 10 MPa, more preferably 0.5 to 6 MPa, and most preferably 0.9 to 3 MPa. The reduction treatment time varies depending on the amount of catalyst, the amount of hydrogen flow, etc., but is generally preferably 0.1 to 72 hours, more preferably 1 to 48 hours, and most preferably 3 to 48 hours. If the treatment time is less than 0.1 hour, the activation of the catalyst may be insufficient. On the other hand, even if the reduction treatment is performed for a long time exceeding 72 hours, there is no adverse effect on the catalyst, but no improvement in the catalyst performance is observed.

The FT reaction can be carried out by passing a synthesis gas through the catalyst composition used in the present invention subjected to the reduction treatment as described above.
The synthesis gas used may be mainly composed of hydrogen and carbon monoxide, and other components may be mixed as long as the reaction is not hindered. For example, in order to produce the FT gasoline fraction used in the gasoline composition of the present invention, a synthesis gas obtained by gasifying biomass can be used. The types of biomass in this case include agricultural, forestry and fishery resource biomass such as food, building materials and pulp, waste biomass such as agriculture, forestry and livestock waste, and plantation biomass such as sugar cane, palm palm and seaweed. Among them, it is preferable to use unused waste biomass that does not compete with food. There is no particular limitation on the biomass gasification method. For example, biomass gasification methods include various types such as direct gasification, indirect gasification, atmospheric pressure gasification, and pressurized gasification. Gasification furnace types include a variety of types such as fixed bed, fluidized bed, and spouted bed. . In the case of producing the FT gasoline fraction used in the gasoline composition of the present invention using the catalyst composition used in the present invention, biomass gasified using any of these methods may be used.

Since the reaction rate (k) depends on the hydrogen partial pressure in the first order, the partial pressure ratio of hydrogen and carbon monoxide (H ₂ / CO molar ratio) is desirably 0.6 or more. Since this reaction is a reaction accompanied by volume reduction, it is preferable that the total value of the partial pressures of hydrogen and carbon monoxide is higher. The partial pressure ratio of hydrogen and carbon monoxide varies in the biomass gasification described above depending on the type of raw material and the gasification method, but when producing the FT gasoline fraction used in the gasoline composition of the present invention. The upper limit is not particularly limited.

 As a practical range of the hydrogen / carbon monoxide partial pressure ratio, 0.6 to 2.7 is appropriate, preferably 0.8 to 2.5, and more preferably 1 to 2.3. If the partial pressure ratio is less than 0.6, the yield of the generated hydrocarbons tends to decrease, and if the partial pressure ratio exceeds 2.7, the generated hydrocarbons tend to increase in gas components. It is done.

 Further, when the FT gasoline fraction used in the gasoline composition of the present invention is produced using the catalyst composition used in the present invention, there is no problem even if carbon dioxide coexists in the synthesis gas. As carbon dioxide to be coexisted in the synthesis gas, for example, those obtained from a reforming reaction of petroleum products or natural gas can be used without any problem. Carbon dioxide mixed with other components that do not interfere with the FT reaction can also coexist in the synthesis gas. For example, carbon dioxide containing water vapor, partially oxidized nitrogen, or the like, such as that from a steam reforming reaction of petroleum products or the like, may be used.

 A gas obtained by positively adding such carbon dioxide to synthesis gas not containing carbon dioxide may be passed through the catalyst composition used in the present invention. Further, the catalyst composition used in the present invention as it is, without subjecting the synthesis gas containing carbon dioxide obtained by reforming natural gas by the self-thermal reforming method or the steam reforming method to the carbon dioxide. It can also be made to react by making it ventilate. By subjecting the synthesis gas containing carbon dioxide to the reaction as it is, it is possible to reduce the equipment construction cost and operation cost required for the decarboxylation treatment, and it is possible to reduce the production cost of the resulting hydrocarbons.

 The total pressure (total value of partial pressures of all components) of the synthesis gas (mixed gas) subjected to the reaction is preferably 0.3 to 10 MPa, more preferably 0.5 to 7 MPa, and further preferably 0.8 to 5 MPa. Low pressure is not preferable because chain growth becomes insufficient and the yield of gasoline, kerosene, wax, etc. tends to decrease. In terms of equilibrium, the higher the partial pressure of hydrogen and carbon monoxide, the more advantageous. However, the higher the partial pressure, the more expensive the plant construction costs, and the larger the compressors required for compression, the higher the operating costs. Tend to rise. Therefore, the upper limit of the partial pressure is restricted from an industrial viewpoint.

 The contact time between the synthesis gas and the catalyst in the FT reaction (hereinafter referred to as W / F: weight / flow [g · h / mol]) is preferably 1 to 100, more preferably 1.5 to 90, and even more preferably. 2-80. Although the value of W / F varies depending on the throughput and the performance of the catalyst used, generally, when W / F is 1 or more, a sufficient CO conversion is obtained and the yield of the liquid product is improved. Moreover, if W / F is 100 or less, an unnecessary increase in the size of the reactor due to an increase in the amount of catalyst used can be suppressed.

On the FT synthesis catalyst, generally, if the H ₂ / CO molar ratio of the synthesis gas is the same, the lower the reaction temperature, the higher the chain growth probability and C 5 + selectivity (selectivity for synthesis of hydrocarbons having 5 or more carbon atoms). Increases, but the CO conversion decreases. Conversely, if the reaction temperature increases, the chain growth probability and C5 + selectivity decrease, but the CO conversion increases. Also, the higher the H ₂ / CO ratio, the higher the CO conversion rate, the lower the chain growth probability and C5 + selectivity, and vice versa when the H ₂ / CO ratio is low. The effects of these factors on the FT reaction vary depending on the type of catalyst used, etc., but the FT gasoline fraction used in the gasoline composition of the present invention is produced using the catalyst composition used in the present invention. In this case, the reaction temperature is 230 to 350 ° C, preferably 240 to 310 ° C, more preferably 250 to 300 ° C. If the reaction temperature is 230 ° C. or higher, both the FT synthesis catalyst and the zeolite work effectively, and it becomes possible to produce a high-octane gasoline fraction by the generation of hydrocarbons and their decomposition and isomerization reactions. . In addition, by setting the reaction temperature to 350 ° C. or lower, it is possible to suppress generation of undesirable gas components on the FT synthesis catalyst and to suppress generation of gas components due to overdecomposition on zeolite.

 In addition, CO conversion rate and the selectivity of various products are defined by the following formula. In the following formula, “C2-4 product” means a product having 2 to 4 carbon atoms.

[CO conversion rate]
CO conversion rate = [(number of CO moles in raw material gas per unit time) − (number of CO moles in outlet gas per unit time)] / (number of CO moles in raw material gas per unit time) × 100
[CH ₄ selectivity]
CH ₄ selectivity = (number of moles of CH _{4 in} outlet gas per unit time) / [(number of moles of CO in raw material gas per unit time) − (number of moles of CO in outlet gas per unit time)] × 100
[CO ₂ selectivity]
CO ₂ selectivity = (number of moles of CO _{2 in} the outlet gas per unit time) / [(number of moles of CO in the raw material gas per unit time) − (number of moles of CO in the outlet gas per unit time)] × 100
[C2-4 selectivity]
C2-4 selectivity = (number of C moles in C2-4 product in outlet gas per unit time) / [(number of CO moles in raw material gas per unit time) − (outlet gas per unit time) Number of CO moles in]] × 100
[C5 + selectivity]
C5 + selectivity = 100 − [(CH ₄ selectivity) + (CO ₂ selectivity) + (C2-4 selectivity)]
[Gasoline selection rate]
Gasoline selectivity = C5 + selectivity x gasoline fraction ratio / 100
[C5 + yield]
C5 + yield = (CO conversion) × (C5 + selectivity) / 100
[Gasoline yield]
Gasoline yield = (C5 + yield) x gasoline fraction ratio / 100

<Method for producing gasoline composition>
The gasoline composition of the present invention can be obtained by mixing the above FT gasoline fraction and other gasoline base materials (the above base materials (a) to (h) and the like).

 Furthermore, various additives can be appropriately blended in the gasoline composition of the present invention as necessary. Such additives include phenolic and amine antioxidants, metal deactivators such as thioamide compounds, surface ignition inhibitors such as organophosphorus compounds, succinimides, polyalkylamines, polyetheramines. Detergents such as polyisobutylene amine, anti-freezing agents such as polyhydric alcohols and ethers thereof, organic metal alkali metal and alkaline earth metal salts, auxiliary alcohols such as higher alcohol sulfates, anionic surfactants, Known fuel additives include antistatic agents such as cationic surfactants and amphoteric surfactants, rust inhibitors such as alkenyl succinates, and colorants such as azo dyes. These can be added singly or in combination. The addition amount of these fuel additives is arbitrary, but usually the total addition amount is preferably 0.1% by mass or less.

 Next, the present invention will be described in more detail with reference to examples, but the present invention is not limited to these examples.

In the following examples, CO analysis was performed using a thermal conductivity gas chromatograph (TCD-GC) using Active Carbon (60/80 mesh) as a separation column. As the source gas, a synthesis gas (mixed gas of H ₂ and CO) added with 25% by volume of Ar as an internal standard was used. Qualitative and quantitative analysis was performed by comparing the peak position and peak area of CO with Ar. The composition analysis of the product was performed using a capillary column (TC-1) and a flame ion detector gas chromatograph (FID-GC). The chemical component of the catalyst was identified by ICP emission spectroscopy (CQM-10000P, manufactured by Shimadzu Corporation).

[Examples 1-2, Comparative Examples 1-4]
C4 fraction (butane, butenes) produced from debenzene heavy catalytic reforming gasoline, catalytic cracking gasoline, light naphtha, catalytic cracking device, catalytic reforming device, atmospheric distillation device, etc., as shown in Table 1, and By blending GTL gasolines 1, 2, 3, and 4, which are FT gasoline fractions, at a blending ratio shown in Table 3, gasoline having properties shown in Table 3 was obtained.

[GTL gasoline 1]
Manganese carbonate (II) n hydrate manufactured by Wako Pure Chemical Industries, Ltd. was used as manganese carbonate. 15.5 g of manganese carbonate was weighed, and 18.8 g of silica sol SI-550 (SiO ₂ content: 20.6%) manufactured by JGC Catalysts & Chemicals Co., Ltd. and ruthenium chloride (manufactured by Kojima Chemical Co., Ltd., Ru Assay: 40.79% by mass). ) After mixing with 1.47 g and allowing to stand for 1 hour, it was fired in air at 200 ° C. overnight. The obtained fired product was pulverized in a mortar to obtain catalyst a which is an FT synthesis catalyst. As a result of chemical composition analysis of the catalyst a by ICP emission spectroscopic analysis, ruthenium was 3.2% by mass in terms of metal.
12 g of catalyst a and 3 g of zeolite H-ZSM-5 (manufactured by Zude Chemie, MFI-90) showing a solid acid were sufficiently mixed to obtain catalyst A as a catalyst composition.
The total amount of catalyst A was diluted with 34.6 g of 100 mesh silicon carbide, filled into a reaction tube having an inner diameter of 15.5 mm, hydrogen partial pressure 0.9 MPa · G, temperature 170 ° C., flow rate 100 (STP) ml / min (STP : Standard temperature and pressure) for 3 hours. After the reduction, the reaction was carried out at a temperature of 280 ° C. and a total pressure of 0.9 MPa · G by switching to a synthesis gas having an H ₂ / CO ratio of about 2 (containing about 25% by volume of Ar).
The contact time (W / F: weight / flow [g · h / mol]) of the synthesis gas (H ₂ + CO) to the catalyst A was about 13.4 g · hr / mol. Since the mixed H-ZSM-5 does not show any activity for the FT reaction, W / F is represented by the contact time of the synthesis gas with the FT synthesis catalyst. Tables 1 and 2 show the results of the reaction and the fraction composition of the obtained liquid product, and Table 3 shows the results of composition analysis (including RON and MON) in the gasoline fraction of the liquid product.
A fraction having a boiling point of 20 to 200 ° C. was defined as a gasoline fraction. The fraction contains hydrocarbons having 5 to 11 carbon atoms.

[GTL gasoline 2]
The reaction was performed in the same manner as in Example 1 except that the amount of H-ZSM-5 mixed with the catalyst a was 0.33 g. Tables 1 to 3 show the reaction results, the fraction composition of the obtained liquid product, and the composition analysis results in the gasoline fraction.

[GTL gasoline 3]
The reaction was performed in the same manner as in Example 1 except that the amount of H-ZSM-5 mixed with the catalyst a was 27 g. Tables 1 to 3 show the reaction results, the fraction composition of the obtained liquid product, and the composition analysis results in the gasoline fraction.

In the gasoline of Example 1, heavy contact reformed gasoline is reduced from the conventional gasoline of the reference example, and GTL gasoline is blended. The density, RON, MON, T50, T90, and RVP of the gasoline of Example 1 are the same as those of the normal gasoline of the reference example. Furthermore, the gasoline of Example 1 is preferable because the aromatic content is reduced as compared with the gasoline of Reference Example. Aromatics are known to affect automobile exhaust and cleanliness. Since GTL gasoline used in the present invention has a high octane number, it can be blended in gasoline as in Example 2. Since GTL gasoline has a low sulfur content, the sulfur content in gasoline is reduced. Since it can reduce, it is preferable. The comparative example 1 of the gasoline which mix | blended GTL gasoline outside the range of this invention has the octane number outside the prescription | regulation of this invention. Moreover, the comparative example 2 of the gasoline which mix | blended GTL gasoline outside the scope of the present invention is outside the definition of the present invention in terms of octane number, RVP, and T50. Further, in Comparative Example 3 of gasoline containing GTL gasoline outside the scope of the present invention, RVP is not within the scope of the present invention. Moreover, the comparative example 4 which mix | blended GTL gasoline 1 more than the regulation amount also has the octane number and T50 which are outside the regulation of the present invention.

Claims (5)

It contains one or more metals that are active in the Fischer-Tropsch reaction, manganese carbonate, and a zeolite that exhibits a solid acid, and the content of the zeolite with respect to the catalyst composition is greater than 65 mass% and less than 80 mass% The gasoline fraction of the product obtained by the Fischer-Tropsch reaction from the gas mainly composed of hydrogen and carbon monoxide and the other gasoline base material are mixed using the catalyst composition for producing hydrocarbons. And the gasoline fraction is 1-60% by volume,
(A) The research octane number is 89 or more and less than 93,
(B) Motor method octane number is 79 or more and less than 84,
(C) Aromatic ratio is 10 to 40% by volume,
(D) at most 40% by volume of olefins,
(E) at most 1% by volume of benzene,
(F) At most 10 ppm by mass of sulfur,
(G) Reed vapor pressure is greater than 65 kPa and less than or equal to 93 kPa,
(H) 50 vol% distillation temperature is 75-110 ° C
A method for producing a gasoline composition comprising producing a gasoline composition which is It contains one or more metals that are active in the Fischer-Tropsch reaction, manganese carbonate, and a zeolite that exhibits a solid acid, and the content of the zeolite with respect to the catalyst composition is greater than 65 mass% and less than 80 mass% Gasoline containing 1 to 60% by volume of a gasoline fraction of a product obtained by a Fischer-Tropsch reaction from a gas mainly composed of hydrogen and carbon monoxide, using the catalyst composition for producing hydrocarbons A composition,
(A) The research octane number is 89 or more and less than 93,
(B) Motor method octane number is 79 or more and less than 84,
(C) Aromatic ratio is 10 to 40% by volume,
(D) at most 40% by volume of olefins,
(E) at most 1% by volume of benzene,
(F) At most 10 ppm by mass of sulfur,
(G) Reed vapor pressure is greater than 65 kPa and less than or equal to 93 kPa,
(H) 50 vol% distillation temperature is 75-110 ° C
A gasoline composition characterized in that  3. The catalyst composition contains a Fischer-Tropsch synthesis catalyst containing one or more metals and manganese carbonate exhibiting activity in a Fischer-Tropsch reaction, and a zeolite showing a solid acid. The gasoline composition described.  The gasoline composition according to claim 2 or 3, wherein the metal is ruthenium. The gasoline composition according to any one of claims 2 to 4, wherein the zeolite is ZSM-5.