Hydrotreating Process, Environment Friendly Gasoline 3ase Oil and Unleaded Gasoline Composition
[Field of the Invention]
The present invention relates to a process for hydrotreating a feedstock containing a fat component originating from an animal or vegetable oil and an environment friendly gasoline base oil produced by the process. Further the present invention also relates to an unleaded gasoline composition containing the friendly gasoline base oil, which composition is excellent in exhaust gas purifying properties, fuel consumption and drivability.
[Background of the Invention]
Conventionally, gasoline has been produced by blending one or more types of base gasoline fractions produced by processing crude oil in various refining units such as a catalytic reformer or a catalytic cracker (see, for example, Non-Patent Document No. 1) .
Recently, an automobile has been required to reduce harmful substances contained in the exhaust gas for improving the atmospheric environment and to reduce the emissions of CO2 which is a gas causing the greenhouse effect in view of global warming prevention.

A gasoline-powered automobile is extremely low in the amount of harmful substances in the exhaust gas but has been required to reduce the CO2 emissions by improving thermal efficiency and fuel consumption. In the mid-and long-terms, the diversification of sources of fuels for transportation purposes and the establishment of sustainable mobility have been demanded.
Under these circumstances, an attention has been drawn to the use of a i n a t i ng fuel, which is capable of preventing life cycle CO2 emissions from increasing, contributive to the diversification of sources of fuels, and reproducible, as a fuel for gasoline-powered automobiles. Among biomass energies, those originating from vegetables in particular can make effectively the use of hydrocarbons converted from carbon dioxide by photosynthesis through the growth process of vegetables and thus have the so-called carbon neutral characteristics, which do not ieaQ "LO an increase in carbon dioxide in the atmosphere in view of the life cycle. If these biomass energies such as fuels originating from animals or vegetable oils can be used as gasoline fuel, it is expected to play an effective role for decreasing reducing carbon dioxide emissions in view of the fact that gasoline engines have been broadly used.

Samples of known biomass- originating base oils, which can be blended with gasoline include ethanol {biomass-origir.atmg ethanol) produced by fermenting a sugar component mainly containing starch of sugar cane or corn, and ETBE (ether ter11a 11y-buty1 ether) produced by reacting the biomsss-originating ethanol with isobutylene produced by separating mixed butylene produced in a fluid catalytic cracker (FCC) in a refinery or a steam cracker in an ethylene plant {see, for example, Non-Parent Document No. 2).
It has been studied to use a fatty acid alkyl ester mixture produced from a natural animal or vegetable fat, alone or in combination with an existing gas oil, as a fuel for diese1-powered automobiles fsee, for example, Non-Fatent Documient No. 3) . However, since the gasoline engine and the diesel engine are different from one another in and dis-illaticn range, required for their fuels, it is difficuli: to use such a fatty acid methyl ester originating from an animal or vegetable oil as a fuel for gasoline-powered automobiles. Further, the fatty acid methyl earer oil is produced by ester-exchange of the triglyceride structure that is a common structure for animal or vegetable oils, with methanol using alkalis. However, as described in Patent Document No. 1 below, it has been

pointed cut that the process of producing a fatty acid methyl eater oil requires disposal of glycerin formed as a by-product and that washing the produced oil is cost- and energy-consuming.
(1) Patent Document No.l: Japanese Patent Application Laid-Open Publication No. 20C5-154 6^7
(2) Non-Patent Document No. 1: "Shinhan Nenryou Binran" edited by The Fuel Society of Japan, published by CORONA PUBLISHING CO. , LTD., in March 1974, pp 264-267
(3) Non-Patent Docum.en- No. 2: Material No. 3 delivered at the 3rd Council on the Promotion of the Use of Renewable Fuels iOctober 10, 2003) hosted by Ministry of the Environment
(4) Non-Patent Document No. 3: 7th Report of the
Central Environment Council, July 29, 2 003
[Disclosure of the Invention]
In addition to the aforesaid problems, the use of animal or vegetable fat components or fuels produced therefrom arises the following problems. That is, since fat components originating from animal or vegetable oils generally contain oxygen in their molecules, oxygen components would adversely affect

m.aterials forming an engine and it is difficult to reduce the oxygen components to an extremely low concent rai: i on , When a fat component originating from an animal or vegetable oil is mixed with a petroleum hydrocarbon fraction, it is impossible to reduce sufficiently both the oxygen content in the fat component and the sulfur content in the petroleum hydrocarbon fraction with the conventional techniques. Further, when the fa. coinponent is used as a fuel base oil, it is preferably less in ncrrr.ai paraffin content and more in isoparaffin content. For an automobile gasoline, for e xample, higher normal paraffin content causes insufficient octane numbe r.
Therefore, the present invention has an object to provide a process for hydrotreating a feedstock enabling the production of a hydrotreated oil which is sufficiently reduced in oxygen and sulfur contents and sufficiently less in normal paraffin content when using the feedstock containing an oxygen-containing hydrocarbon compound or further containing a sulfur-containing compound, an environment friendly gasoline base oil produced by the process and an unleaded gasoline composition containing the environment friendly gasoline base oil.
That is, the present invention provides a process

for hydrotreatrng a feedscock, comprising bringing the feedstock into contact with a catalyst in "he presence of hydrogen, the feedstock containing an oxygen-containing compound, the catalyst comprising a support containing a crystalline metallosilicate and one or more types of metals selected from the Group 8 elerrients of the periodic table.
The present invention provides a process for hydrotreading a feedstock, comprising bringing the feedstock into contact with a catalyst in the presence cf hydrogen, the feedstock containing an cxygen-containing compound and a su1fur-containing compound, the catalyst comprising a support containing a crystalline metallosilicate and one or more types of metals selected from the Groups 6A and 8 elements of the periodic table.
According to the present invention, a hydrotreated oil which is sufficiently reduced in oxygen and sulfur contents and sufficiently less in normal paraffin content can be produced in an economically efficient manner by bringing a feedstock containing an oxygen-conta ining compound into contact with a specific catalyst.
In the hydrotreating processes of the present invention, the feedstock is preferably contacted with

the catalyst under such conditions that the oxygen content and norn^ial paraffin content of the fraction in a boiling point range of 3 0 to 135'C of the resultina hydrotreated oil are 0.2 percent by mass or less and 30 percent by mass or less, respectively. Hydrotreating of the feedstock under these conditions enables the production of a hydrotreated oil containing higher level of components effective as a gasoline base oil. In this case, the processes enable the economically efficient production of an environment friendly gasoline base oil which is sufficiently reduced in oxygen and sulfur contents and sufficiently less in normal paraffin content.
In the hydrotreating process of the present invention, when a feedstock containing an oxygen-containing hydrocarbon compound is contacted with a catalyst comprising a support containing a crystalline metallosilicate and one or more types of metals selected from the Group 8 elements of the periodic table, the oxygen and sulfur contents of the feedstock are preferably from 0.1 to 15 percent by mass and 50 ppm by mass or less, respectively on the basis of the total mass of the feedstock. When the oxygen and sulfur contents of the feedstock are within the above ranges, stable deoxidization activity can be

maintained for a long period of tim.e.
In the hydrotreating process of the present invention, when a feedstock containing an oxygen-containing hydrocarbon compound and a sulfur-containing hydrocarbon compound is contacted with a catalyst comprising a support containing a crystalline metallosilicate and one or rriore types of metals selected from, the Groups 6A and 8 elements of ~he periodic table, the oxygen and sulfur contents of the feedstock are preferably froiri 0.1 to 15 percent by mass and from 1 ppm by mi ass to 1 percent by mass, respecrively on the basis of rhe total mess of the feedstock. When the oxygen and sulfur contents of the feedstock are within the above ranges, stable deoxidization activity can be maintained for a long pe ri od of t ime.
In the hydrotreating process of the present invention, the oxygen-containing hydrocarbon com.pound is preferably a fat component originating from an animal or vegetable oil with the objective of using biomass energy efficiently.
The ratio of the compound having a triglyceride structure in the oxygen-containing hydrocarbon compound is preferably 90 percent by mole or more with the objective of reducing the energy required for

processing raw materials.
In the hydrotreating process of rhe present i n V e n t i c r., the Group 8 elements contained in the catalyst are preferably one or more metals selected from Pd, Pt, Rh, Ir, Au and Ni.
In the hydrotreating process of the present invention, the Group 6A and 3 elem>ents contained in the catalyst are preferably one or more metals selected from. Co, Mo and Ni.
In the hydrotreating process of the present invention, the crystalline meta 11osi1icate contained in the catalyst preferably has a structure of laujasite type .
Further, the crystalline metallosilicate is preferably an ultra-stable Y type zeolite having a molar ratio of the silica to the alumiina (silica/alumina) within the range of 10 to 10 0, When the molar ratio is less than 10, the formiation of coke would be facilitated, possibly resulting in a significant reduction in activity. When the miolar ratio is in excess of 100, hydrotreating activity would be insufficient, resulting in the likelihood that the yield of components useful for a fuel base oil would be reduced.
According to the present invention, there is also

provided an environment friendly gasoline base oil comprising a fraction with a boiling point range of 25 to 220° C of -Lhe hydrotreated oil produced by t:he foregoing hydrotreating process of the present invent ion,
The environment friendly gasoline base oil preferably has an oxygen content of 0.2 percent by mass or less and a norn^al paraffin content of 30 percent by mass or less.
Further, the present invention also provides an unleaded gasoline composition comprising the aforesaid environment friendly gasoline base oil. The unleaded gasoline coTtipos it i on corf.prising the aforesaid environment friendly gasoline base oil of the present invention can accomplish a reduction in carbon dioxide emissions effectively.
The unleaded gasoline comipos ition of the presenr invention is preferably an unleaded gasoline with a research octane number of 89.0 or greater and less than 96.0 and a sulfur content of 10 ppm by mass or less or an unleaded gasoline with a research octane number of 96.0 or greater and a sulfur content of 10 ppm by mass or less.
Preferably, the unleaded gasoline composition of the Dresent invention has a 10% distillation

temperature of 7 0°C or lower, a 50% distillation temperature of 75°C or higher and llO^C or lower, a 90% distillation cemiperature of 180^C or lower, an end point of 220°C or lower, a vapor pressure (37.8°C) of 44 kPa or greater and 93 kPa or less, a density (15"C) of 0.783 g/cm^ or less, an oxidation stability of 240 minutes or longer, a ooDper corrosion (50°C, 5 hours) of 1 or less, a washed existent gum content of 5 m,g/100 ml or less, an unwashed existent gum content of 20 mg/100 ml or less and a benzene content of 1 percent by volume or less.
Preferably, the unleaded gasoline composition of zhe present invention has an aromatic content of 45 percent by volume or less and an olefin content of 35 percent by volume or less.
Preferably, the unleaded gasoline com.position of the present invenricn has a m.anganese contenc of 2 ppm by mass or less, an iron content of 2 ppm by m.ass or less, a sodium content of 2 ppm by mass or less, a potassium content of 2 ppm by mass or less and a phosphorus content of 2 ppm by mass or less.
Preferably, the unleaded gasoline composition of the present invention contains an anti-oxidant and a metal deactivator or contains a detergent-dispersant and a friction modifier.

[Effects of -he Present Invention]
According ro the present invention, there is provided a process of hydrotreating a feedstock enabling the production of a hydrotreated oil which is Sufficiently reduced in oxygen and sulfur contents and Sufficiently less in normal paraffin content in an extremely eccnomicaily efficient manner when using a feedstock containing an oxygen-containing hydrocarbon ccrripound and alternatively further containing a sulfur-containing hydrocarbon compound. Further, according to the present invention, there is provided an environm.ent friendly gasoline base oil and an unleaded gasoline composition, which can efficiently accomplish a reduction in carbon dioxide emissions.
[Best Mode of Carrying cut the Invention]
The present invention will be described in more
detail below.
A feedstock containing an oxygen-containing
hydrocarbon compound or a feedstock further containing
a sulfur-containing hydrocarbon compound is used in the
present invention. The oxygen-containing hydrocarbon
compound is suitably an animal or
vegetable-originating fat component that is bioinass.

The fat ccrriponeni: used herein incorporates naturally or artificially r.ade or produced animal or vegetable fats, animal or vegeiable fat components and/or components mi ade or produced from these fats, and components to be added for the purpose of maintaining and improving the properties of the fat products.
Exam pies of the far. coir.ponenL s originating from animal or vegerable oils include vegetable oils such as rapeseed oil, corn oil, soy bean oil, grape seed oil and palm, oil and animal oils such as beef tallow and lard. Any fat may be used as the fat corriponent originating from animal or vegetable oils in the present invention. Alternatively, waste oils resulting from the use of these fats may be used. However, in view of carbon neutral, it is preferable to use vegetable fats, and in view of the carbon num.ber of the fatty acid alkyi chain and reactivity thereof, it is more preferable to use rapeseed oil, soy bean oil and palm oil. The foregoing fats may be used alone or in comb i nat ion.
In general, the fat components originating from animal or vegetable oils have a fatty acid triglyceride structure but may contain other fatty acids or fat components modified to an ester, such as fatty acid methyl ester. However, the vegetable fat preferably

contains mainly a com.ponent having a triglyceride str-jcture with the objective cf reducing carbon dioxide emissions because carbon dioxide is generated upon production of fatty acids or fatty acid esters from vegetable fats. In the present invention, the ratio of the compound having a triglyceride structure in the oxygen-containing hydrocarbon comipound concained in rhe feedstock is preferably 90 percent by m.oie or more, more preferatly 52 percent by mcle or more, more preferably 95 percent by mole or zriore.
The oxygen content of the feedstock is preferably fro.T. 0.1 to 15 percent by mass, mors preferably from 1 zo 15 oerceni: by mass, ir.ore preferably from 3 to 14 perceni by mass, particularly preferably from 5 to 13 percent by mass en the basis of the total mass of the feedstccJ^. If the oxygen content is less than 0.1 percent by xass, it would be difficult to maintain stable deo^^idi za t i on and desul f uri za t i on activities. Whereas, the oxygen content is in excess of 15 percent by mass, there may arise the necessity of facilities for disposal of by-produced water or water and the catalyst support would be excessively interacted, resulting in a reduction in activity or catalyst strength. The oxygen content can be measured with a conventional elemental analysis device. For example.

ihe oxygen content is measured by converring a sarr.ple on plarinum, carbon to carbon monoxide or further to carbon dioxide and measuring the amount thereof using a thermal conductivity detector.
In the present invenrion, the feedstock may contain a sulfur-containing hydrocarbon comipound. There is no particular restriction on the sulfur-connaining hydrocarbon compound . Ex arr.pl e s thereof include sulfide, disulfide, polysulfide, thiol, ihiophene, ben zorhiophene, dibenzothiophene, and derivatives thereof. The sulfur-containing hydrocarbon compound contained in the feedstock may be a single compound or a mixture of two or more types of these compounds. Alternatively, a petroleumi hydrocarbon fraction containing sulfur may be used as the sulfur-containing hydrocarbon c om.p o u n d ,
The petroleum hydrocarbon fraction m.ay be a fraction produced through general petroleumi-refining processes. For example, the fraction may be a fraction within a predetermined boiling point range produced from an atmospheric disrillation unit or a vacuum distillation unit or a fraction within a predetermined boiling point range produced from a
hydrodesulfurization unit, a hydrocracking unit, a residue direct hydrodesulfurization unit or a fluid

catalytic cracking unit. The fracrion produced from each of these units may be used alone or in combination.
Further, the feedstock may contain compounds originating from chemical products such as plastics or solvent and may contain a synthetic oil produced through a Fischer — Tropsch reaction using a feedstock which is a synthetic gas composed of carbon monoxide and hydrogen.
When the feedstock containing an oxygen-containing hydrocarbon compound is contacted with a catalyst comprising a support containing a crystalline metallosilicate and one or more types of metals selected from the Group S elements of the periodic table, in the hydrotreatment process of the present invention, the sulfur content of the feedstock is preferably 50 ppm by mass or less on the basis of the total mass of the feedstock. If the sulfur content is in excess of 50 ppm by mass, the hydrotreated oil is likely to be increased in sulfur content and thus would adversely affect the exhaust gas purification device of a gasoline engine when it is used therefor. When the feedstock containing an oxygen-containing hydrocarbon compound and a sulfur-containing hydrocarbon compound is contacted with a catalyst comprising a support containing a crystalline

rr.eta 1 los il icat e and one or more types of metals selected from, the Groups 6A and 8 elerr.ents of the periodic table, the sulfur ccnteno of the feedstock is preferably from 1 ppm by mass to 1 percent by mass, more preferably from 15 ppm by mass to 0.5 percent by mass, more preferably from 30 ppm by mass to 0.1 percent by m.ass on the basis of zhe toral mass of the feedstock. If the sulfur content is less rhan 1 ppm by mass, it would be difficult to maintain stable deoxidization activity. If the sulfur content is in ej^cess of 1 percent by mass, the hydrotreated oil is likely to be increased in sulfur content and thus would adversely affect the exhaust gas purification device of a diesel engine when it is used therefor. The sulfur conten" used herein denotes the mass content of sulfur measured in accordance with JIS K 2541 "Crude oil and oetroleum

S LI ( ~ U

method described in ASTM-5453.
The sulfur-containing hydrocarbon compound may be miixed with the feedstock beforehand and then int reduced into the reactor of a hydrotreating unit or alternatively may be supplied to a section before the reactor when the feedstock is introduced therein.
The feedstock used in the present invention preferably contains a fraction with a boiling point of

3 0C°C or higher and does not contain a heavy fraction with a boiling point of higher than ~ 0 0 "^ C . VJhen a feedstock not containing a fracricn wirh a boiling point of 300''C or higher is used, it would be difficult to obtain a sufficient yield because excess decomposition may occur. Whereas, when a feedstock containing a heavy fraction with a coiling point of higher than 7C0'^C is used, heavy components would accelerate precipitation of carbon in the catal^'st, possibly resulting in a reduction in activity. The boiling point used herein denotes the value measured in accordance with JIS K 2254 "Petroleum products-Determiriation of distillation characteristics" or the method described in ASTM-365.
The present invention provides a first hydrotreating process (hereinafter referred to as "hydr crrearm.ent A") wherein a feedstock conraining an oxygen-conraining hydrocarbon is contacted in the presence of hydrogen with a catalyst comprising a support containing a crystalline met allosi1icate and one or more types of metals selected from the Group 8 elements of the periodic table to be hydrotreated. The present invention also provides a second hydrotreating process (hereinafter referred to as "hydrotreatment B") wherein a feedstock containing an

oxygen-con-air. ing hydrocarbon and a sulfur-con ::aining hydrocarbon compound is contacted wirh a catalyst CO mi prising a support containing a crystalline metallosilicate and one or more types of mietals selected from the Groups 6A and 8 elements of the periodic table to be hydrotreated,
The suoDorzs of the caralysts used in the present invention are porous inorganic oxides having a crystalline metallosilicaoe. The crys-calline metallosilicate has a structure represented by a code preferably such as FAU , AEL, MFI, MKW, TON, MTW, *BEA, and MOR, more preferably FAU, *3EA, MOR cr MFI defined by International Zeolite Association. In the present invenrior., the metallosilicare has more preferably a strucrure represented by FAU also referred to as "faajasire type". Further, the metallosilicate is particularl'i' oreferably of y-oyps have been ultra-stabilized. The ulrra-stabilization indicates a hydrothermal treatment and/or a washing treatment with an acid solution and can provide the resulting catalyst with a pore volume which is defined as mesopore which must have a oore diameter of 2 to 50 nm by adjusting the content of aluminum if contained in the structure.
The metallosilicate contained in the support of the catalyst used in the present invention is

preferably a crystalline a 1 uir.in o s i 1 i cai e composed of three elements, i.e., aluminum, silicon and oxygen. The crysoallir.e a 1 um.ir.o s i 1 icaoe m.ay be the so-called zeolite containing silica and alumina. Preferable examples include Y-type zeolite, ultra stable Y-type zeolite (USY-type zeolite), (i-type zeolite, mordenite and ZSM-5. Among these zeolites, particularly preferred is USY zeolite. In the present invention, these crystalline aluminosilicares mi ay be used alone or in corTibinat ion .
When the crystalline metallosilicate contains silica and alumina, ohe molar ratio of the silica to the alum.ina ( s i 1 i oa / a lum.in a ) is preferably within the range of 10 to ICO. The molar ratio is less than 10, ihe forma-ion of coke would be accelerated and would ini^ite a reduction in activity. When the molar raoio is in excess of ICO, h y d r o o r e a t i n g activity would be insufficient, possibly resulting in a reduction in the yield of components useful as a fuel base oil. In the present invention, the support of the catalyst preferably contains the crystalline metallosilicate that is an ultra-stable Y-type zeolite with a molar ratio of the silica to the a lumina (silica/alumina) is within the range of 10 to 100.
There is no particular restriction on the method

of synthesizing the crystalline metallosilicate. Any conventional method rr.ay be used. For exam Die, the crysta.liine T.etaiio silicate may be synthesized by heating raw materials of constituting components if necessary in the coexistence of a structural indicator. Examples of the raw materials include
silicon-containing compounds such as sodium silicate, colloidal silica, and alkoxide silicate and a 1 c rr i n u mi - c o n t a i n i n g compounds such as aluminum oxide and sodium aluminate. Examples of che structural indicator include amine compounds such as tetrapropyl arrimon i urn salt.
The catalyst used in the present invention may contain constituting coiriponents ether than the abcve-described crystalline metallosilicate. Exam.ples of constituting components other than the

■ e - o - = c r
ribed crystalline cecalIcsilicate include

inorganic oxides containing elements selected from aluminum, silicon, zirconium, boron, titaniumi and magnesium. These inorganic oxides function as a binder for shaping the crystalline metallosilicate and also as an active component s for facilitating hyarodeoxidization and hydroisomerization. The inorganic oxides are preferably those containing two or more types of elements selected from aluminum.

silicon, zirconium, boron, t.itanium and magnesium wi'h the objective of ensuring the above-described functions.
The content of the metallosilicate in the whole cataiyst is preferably from 2 to 90 percent by mass, more preferably from 5 to 85 percent by m,ass, more preferably from 10 to 83 percent by rr.ass. When the m^etallcsilicate content is less ihan 2 percent by mass, the hydrodeoxidization and hydroisomerizaricn activities of the resulting catalyst would likely be insufficient. When the content is in excess of 90 percent by mass, -he mcldability of ine catalyst would be too lew, rendering it difiiculi: co produce the catalyst on commercial basis.
3 elerr.ents of the oeriodic table, suoDorted
In hydrotreatment A, the catalyst is used, which comprises one or rr,Gre types of metals selected frorr. the G r c".
the above-described porous inorganic oxide support. Among these metals, preferred are one or more metals selected from Pd, Pt, Rh, Ir, Au, and Ni. When two or more metals are used in combination, preferred combinations are Pd-Pt, Pd-Ir, Pd-Rh, Pd-Au, Pd-Ni, Pt-Rh, Pt-Ir, Pt-Au, Pt-Ni, Rh-Ir, Rh-Au, Rh-Ni, Ir-Au, Ir-Ni, Au-Ni, Pd-Pt-Rh, Pd-Pt-Ir, andPt-Pd-Ni. Among these combinations, more preferred are Pd-Pt, Pd-Ni,

Fr-Ni, Pd-Ir, Pt-Rh, Pt-lr, Rh-Ir, ?d-Pt-Rh, Pd-Pt-Ni, and Pd-Pt-Ir. Further m, ore preferred are Pd-Pt, Pc-Ni,

't-Ni,

.-ir ,

-_r, rd-?t-Ki, and ?d-?t-Ir. Upcr.

nydrotreatment, these metals are preferably used after being converted to reductants.
n
With regard to the content of the active mietalis) on the basis of the catalyst mass, the total content of metals selected from the Group 8 elerrients cf the periodic lable is preferably from. 0.1 to 2 percent by mass, m.cre preferably from 0.2 to 1.5 percent by mass, more preierably from 0.5 to 1.3 percent by mi ass. If the total content is less than 0.1 percent, the active sites are reduced, leading to a tendency ^hat a sufficient activity may not be attained. If the rotal content is more than 2 percent by mass, the mietals are dispersed effectively, leading to a tendency that

a s u r 11 c 1 e n t a c 12 v r t y m, a y

c De aztarnea.

In hydrotreatment B, the catalyst is used, which com.prises one or m.ore types of metals selected from the Groups 6A and 8 elements of the periodic table, supported on the above-described porous inorganic oxide support. Among these metals, one or more types of metals selected from Co, Mo and Ni are preferably supported. Two or more metals selected from Co, Mo and Ni are preferably supported in combination.

Preferable combinations are Co-Mo, Ni-Mo and Ki-Co-Mo. At least one or m.ore types selected from the Group 6A elements of nhe periodic table are preferably supported on the above-described porous inorganic oxide. Upon hydrotreatment, these metals are preferably used after being converted to reductants.
When one or more types of metals selected from Co, Mo and Ni are supported, the total content of the active metal !s) is preferably from, 15 to 55 percent by mass, more preferably from 17 to 30 percent by mass on the basis of the rriass of the catalyst. If the total content is less than 15 percent, the active sites are reduced, leading to a tendency that a sufficient activity may not be attained. If the total content is mere than 35 percent by mass, the metals are not dispersed effectively, leading to a tendency that a sufficient activity m-.ay not be attained. With regard to the contents of Co, Mo, and ISli, those in term.s of oxide are used herein.
There is no particular restriction on the method of supporting the active metals on the catalysts. Therefore, any conventional method for producing a usual desulfurization catalyst may be employed. A method is preferably employed in which a support is impregnated with a solution containing salts of the

active metals. Alternatively, an equilibrium adsorption method, pore-filling method, or inoipient-wetness method is also preferably used.
t or
example, the pore-filling method is a method in which the pore volume of a support is measured in advance, and then the support is impregnated with the same volume c; a metal salt solution. There is no particular restriction on the method cf impregnating the support with a solution. Therefore, any suitable method m.ay be used depending on the amount of the metals to be supported and physical properties of the support.
There is no particular restriction on the number of type of hydrotreatment catalyst in each h y d r o t r e a t mi e n t A and 3 c f the present invention. For example, one type of catalyst may be used alone, or a plurality of catalysts each having different active metal or suppcrt-constitcti ng components may be used. When a plurality of catalysts each having a different support ccmiponent are used in combination, , a catalyst with a metallosilicate content within the range of 2 to 90 percent by mass may be used in a stage after a catalyst with a rr'etallosilicate content of S percent by mass or less, both contents being on the basis of the total mass of the support.
If necessary, in addition to the hydrotreatment

catalysts, a guard catalyst, a demetallization catalyst, and an inert filler may be used alone or in combination for the purposes of trapping scale fractions flov^ing into the reactor, accompanied with the feedstock and supporting the hydrotreatment catalysts at portions segmenting the catalyst beds. Conditions under which the feedstock is contacted with the catalysts in the presence of hydrogen are a hydrogen pressure of 2 to 13 MPa, a liquid hourly space velocity ilHSV) of 0.1 to 3.0 h'* and a hydrogen oil pressure (hydrogen/oil ratio) cf 15G to 1500 NL/L, preferably a hydrogen pressure of 2 to 10 MPa, a liquid ncurly space velocity of 0.2 to 2.0 h'" and a h\'droger. til ratio of 200 to 1200 NL/L, more preferably a hydrogen pressure of 2 to 6 MPa, a liquid hourly space velocity

of 0.3 to 1.5 h"

and a hydrogen oil ratio of 250 to

T ■" 'I ,- H~ / -r "IT = " >■
_ ^ ^ ^ ,^ ^ / _ij . ZJ ^ ^ l-

n ^ '^ c

nditicns is a factor exertina

an influence on the reaction activity. For example, if the hydrogen pressure and hydrogen/oil ratio are less than the lower limits, the reactivity tends to reduce, and the activity tends to reduce rapidly. If the hydrogen pressure and hydrogen/oil ratio exceed the upper limits, an enormous plant investment for a compressor may be required. Lower liquid hourly space velocity tends to be more advantageous for the

reactions. H o w e -/ e r , if the liquid hourly space velocity is lower than the lower liryiit, an snorrrious plant investmenn for conscruction of a reactor with an extremely large volume may be required. If the liquid hourly space velocity exceeds the upper limit, the reaction tends to proceed insufficiently. The reaction temperature is preferably frorr, 25C to 55G=C, more preferably from 280 to 480°C, more preferably from 3 0 0 -o 46 0=C.
The reactor may be of a fixed bed mode. That is, supply of hydrogen to the feedstock, may be carried out in the form of counter flow or parallel flow. Alternatively, counter flow and parallel flow may be combined in a plurality of reactors. The supply ir.ode of the feedstock is generally down flow. Gas-liquid cocurrent flow may be em.plcyed. The reader miay be a sincle reactor or a combination of a plurality or reactors. A single reactor with the interior segmented into a plurality of catalyst beds may also be employed.
The feedstock hydrotreated in a reactor is fractionated into hydrotreated oils each containing a predetermined fraction through gas-liquid separation and rectification. For example, the hydrotreated feedstock is fractionated into a gas oil fraction or a residue fraction. If necessary, the hydrotreated

feedstock may be cf-en fracrionated into gas, a naphtha fraction and a kerosene fraction. There is the

pcssibiliiy that "^ater, carbon :n-ionoxide,

-V,

on

dioxide and hydrogen sulfide may be generated, accompanied with the reaction of oxygen or sulfur components contained in the feedstock. Therefore, a gas-liquid separation device or any ether by-produced gas removal device may be installed between the plurality of reactors or in the product recovering St ep .
Hydrogen is generally introduced into a first reactor via its inlet, accompanying the feedstock, before or after the feedstock passes through a heating furnace. Alternatively, nydrogen gas may be introduced from the spaces between the catalyst beds or between a plurality of reactors for the purposes of
maintaining the hydrogen pressure over the whole reactors. Hydrogen to be introduced in such a manner is referred to as "quenching hydrogen". The ratio of the quenching hydrogen to the hydrogen introduced, acoDm.panying the feedstock is preferably from 10 to 60 percent by volume, more preferably from 15 to 50 percent by volume. The ratio of less than 10 percent by volume would cause a tendency that the reaction at reaction

sites in the subsequent stages does not proceed sufficiently. The ratio in excess of 60 percent by volume would cause a tendency that the reaction near the inlet of the reactor does not proceed suffi. ciently.
The kerosene fraction and/or gas oil fraction and/or residue prod-jced by the hydrotreatment of the present invention may be recycled by being miixed with the feedstock in whole or part thereby increasing the yield of a gasoline fraction.
In the hydrotreatment process of the present invention, the base oil composed of the whole or part of a fraction with a distillation temperature range of 25 to 22 0^C has preferably an oxygen content of 0.2 percent by mass or less and a normial paraffin content of 30 percent by rr.ass or less. Further, the feedstock is preferably h^^'drotreated under such conditions that the fraction has an oxygen content of 0.2 percent by mass or less and a normal paraffin content of 25 percent by mass or less. In the hydrotreated oil produced by the hydrotreatment process of the present invention, the remaining oxygen components are present in the form, of any of functional groups such as hydroxy 1 group, aldehyde group or carboxyl group or a plurality of the functional groups. However, if the oxygen content of the fraction is in excess of 0.2 percent by mass.

ccrrosix'iiy would be high and the aldehyde concentration in the exhaust gas would be increased. If the normal paraffin consent of the fraction is in excess of 30 percent by mass, the octane number of the resulting gasoline base oil would be decreased, and thus the resulting gasoline product vjould be poor in anri-knocking properties during high speed driving. Among the conditions under which the feedstock is contacted wi::h the catalyst to satisfy the above requirements of the hydrotreated oil, the reaction temperature and liquid hourly space velocity are preferably adjusted for the hydrotreatment thereby producing a component useful as a gasoline base oil fron-. the feedstock. The normal paraffin content used herein can be measured in accordance with JI3 K2536-2 "Liquid r^etrcleum products-Testing method of components part
L,3_L ^^■il.K^w_.^.,„0
chromatography".
The hydrotreated oil comprising the whole or part of a fraction with a distillation temperature range of 25 to 220°C produced by the present invention is preferably used as a gasoline base oil. The unleaded gasoline composition of the present invention (may be hereinafter referred to as "the gasoline of the present invention") comprises the gasoline base oil (may be

hereinafter referred to as "the environment friendly gasoline base cil of the present in-.'ention"i.
Examples of the fracticn range include a 25 tc ^3°C light fraction, a 70 to 160°C middle fraction, and a 160 to 220°C heavy fraction. Other than these fractions, there may be used a remaining fraction produced by removing a part of fraction with a specific distillation temperature range from a 25 to 22D°C fraction.
In view of octane number, the fraction is preferably a light fraction. More specifically, the fraction is a liaht fraction with a distillation

emit)'

:referablv 15C°C or lower, iri;

preferably 120°C or lower, more preferably IQC^C cr lower.
e gasoline
When the environment friendly gasoline base oil of the present invention is blended icr com.position of the present invention, it may be desulfurized if necessary. The whole or a part of the fractions in the base oil m.y be desulfurized. The environment friendly gasoline base cil may be treated in a catalytic reforming unit so that the base oil may be blended as a gasoline base cil with a higher octane numbe r in the gasoline of the present invention.
The content of the environment friendly gasoline

base oil of che present invention in the

:a s ol 1 ne

c omp osition of the present invention is preferably 5 percent by volume or more, more preferably 5 percent by volum.e or rriore on rhe basis of the total mass of the gasoline with the objective of increasing the base oil originating from biomass. On the other hand, the base oil content is preferably 30 percent by volume or less, more preferably 2 5 percent by volume or less, 20 percent by volume or less in view of fuel consump-ion.
There is no pdrticular restriction on base oils to be blended, other than the environment friendly gasoline base oil of Lhe present invention. Therefore, any one or more types of gasoline base materials oroduced by any known process may be blended.
More specific examples of such base oils include straight procane fractions containing mainly propane and straight bucane fractions containing xainly butane, produced in a distillation unit of crude oil, a naphtha reforming unit and an alkylation unit; straight desulfurized propane fractions and straight desulfurized butane fractions, produced by desulfurizing the foregoing fractions; cracked propane fractions containing m.ainiy propane and propylene and cracked butane fractions containing mainly butane and butene, produced in a catalytic cracking unit; naphtha

fractions produced by atmospheric distilla::ion of crude oil (vj hole-range .-. aphtha!,■ light fractions of naphtha; heavy fractions of naphtha; desulfurized whole-range naphtha produced by desulfurization of whole-range naphtha; desulfurized light naphtha produced by desulfurization of lighr naphtha; desulfurized heavy naphtha produced by desulfurization of heavy naphtha; isomerized gasolines produced by converting light naphthas to isoparafiin in an isomerization unit; alkylates produced by addition (alkyiation) of lower olefins to hydrocarbons such as isobutane; reformed gasolines producea by a catalytic reforming orocess; raffinates which are residues produced by extracting aromatic components from reformed gasolines; ligh" reformed gasolines that are iiaht fractions of reformed gasolines; middle reform.ed
.re middle fractions
gasolines; heavy reformed gasolines that are heavy fractions of reformed gasolines; mixtures of two or more types of the foregoing reformed gasolines; catalytic cracked gasolines (whole-range cracked gasolines) produced by catalytic cracking; light cracked gasolines which are light fractions of catalytic cracked gasolines; heavy cracked gasolines which are heavy fractions of catalytic cracked

gasolines; hydrocracked gasolines produced by hydrocracking; polymerized gasolines produced by polymerizing olefin ccmponents; olefin fractions produced by dimerization of propylene or butene; paraffin fractions produced by hydrogenation of olefin fractions produced by dimerization of propylene or butene; de-n-paraffinizated oil; aromatic hydrocarbon corr.pounds (toluene, aromatics having 8 carbon atorr.s
(xylenes! and arcm.atics having 9 carbon atorr.s); and light fractions of GTL (Gas to Liquids) produced by F-T
(Fischer-Tropsch) synthesis of natural gas afrer decomposed to carbon monoxide and hydrogen.
The blend arf.ount of these base oils is optional

=3 long as the gasoline of the preS'

invention is

adjusted to have its properties in the requisite ranges

Typical examples of xhe blend amount of the base o:

Is

::; _^^_:_„vi(S

/ 1

reformed gasoline: 0 to 80 percent by volume;

(2) cracked gasoline: 0 to 60 percent by volume;
(3) alkylate: 0 to 40 percent by volume;
(4) isomerized gasoline: C to 30 percent by volume .
The gasoline of the present invention may contain an oxygen-containing compound.
Examples of the oxygen-containing compound

include alcohols having 2 to 4 carbon atoms and ethers having 4 to 8 carbon atoms. Specific examples of the cxygen-con t air. in c compound include e t hanol, mer:hyl-tert-buty]-ether (MTBE) , ethyl-tert-butyl ether (ETBE), tert-amyl methyl ether (TAME), and tert-amyl ethyl ether. Preferred are ethanol, MTBE, and ETBE. With the objective of inhibiting carbon dioxide emissions, ethanol originating from biomass and ETBE produced from ethanol originating from bicmass are particularly preferably used. Since methanol may increase corrosivity and the aldehyde concentration in the exhaust gas, preferably it is not detected (0.5 percent by volumie or less; when tesred in accoroance with JI3 K 2536 "Liquid petroleum products-Testing method of com.ponents".
The conoent of the oxygen-containing compound of the aascline is preferably 5.3 percent by r.ass or less, m.cre preferably 3.5 percent by mass or less, m^ore oreferably 2.1 percent by mass or less, and most preferably 1.3 percent by mass or less, in term of oxide, in view of compatibility to fuel system parts of an automobile and with the objective of preventing an increase in NOx in exhaust gas.
The research octane number (RON) of the gasoline of the present invention is necessarily 89.0 or greater,

preferably 30.0 or greater in view of anri-knccking properties, acceleration performance and drivability.
When the gasoline of the present invention is used for a regular gasoline-powered autorr.obile, the RON is necessarily less than 96.0 because an increase in the CO2 emissions upon production of the gasoline exceeds a reduction in the CO; emissions caused during automobile running. The m.otor octane number (MON) is preferably SO.O or greater, more preferably 81.3 or Greater with the ob:ective of preventing the deterioration of anti-knocking properties at a higher speed running.
When the gasoline of the present invention is used for a Dremium gasoline-powered automobile, the RON is preferably 96.0 or greater, more preferably 98.0 or greater, mi ore preferably 99.5 or greater, ir.ost

:referablv 10 3.j or greater with the

= 1 . '^ a

maximizing the anti-knocking properties, acceleration performance and drivability of the premium gasoline-powered automobile. The MGN is preferably B5.0 or greater, more preferably 87.0 or greater with the objective of preventing the deterioration of anti-knocking properties at a higher speed running. The research octane number (RON) and motor octane number (HON) referred herein denote those measured in

accordance with CIS K 228C "Petroleum
products- Fuels- Determination of octane number, cetane
number and calculaticn of cetane index".
The sulfur content of the gasoline of che present invention is necessarily 10 ppm by nass or less, preferably 8 ppm by mass or less, more preferably 5 ppm by mass or less. If the sulfur content is rr.ore than 10 ppm by mass, the gasoline adversely affects the performance of an exhaust gas purification catalyst, possibly leading to an increase in the concentrations of NOx, CO, and HC in the exhaust gas and an increase in the emissions of benzene.
The sulfur ccnten- referred herein denotes a value measured in accordance with JIS K 2541 "Crude oil and petroleum pr odu c t s - De t e rm.ina t i on of sulfur content".
The gasoline of the present ir;venticn is necessarily lead-free. The lead-free referred herein denotes that an alkyl lead compound sjch as tetraethyl lead is not added to gasoline and also means that the sulfur content is less or equal to the lower bounds (0.001 g/1} stipulated as acceptable in JIS K 2255 "Petroleum products-Gasoline-Determination of lead content" even though lead compounds are contained in an extremely trace amount.
The initial boiling point (IBP) of the gasoline

of the present invention is preferably 2C°C or higher, more preferably 23~C or higher. If zhe IBP is lower than 2 0 ^ C, t n e amount of hydrocarbons in the exhaust gas would be increased. The IBP is preferably 37'c or lower, more preferaoly 35°C or lower. If the IBP is higher than 31°C, low temperature drivability would be poor .
The 10% distillation temperature (TIO) of the gasoline of the oresent invention is preferably 55^C or higher, more preferably 40°C or higher. If the TIO is lower than 35" C, the amount of hydrocarbons in the exhaust gas would pe increased and high temperature drivability would be poor due to vapor lock. The TIO is o^referably ~C^C or lower, mi ore preferably 6 0^C or lower. If the TIC is higher than 70°C, low temperature startability would be poor.
The 2Ch disoillation temperature 'TSC) of one gasoline of the present invention is preferably 55°C or higher, more preferably 60°C or higher. If the T30 is lower than 55°C, fuel consumption would be poor, The T30 is preferably 77°C or lower, more preferably 75°C or lower, more preferably 70°C or lower. If the T30 is higher than 77°C, low and middle temperature drivability would be poor.
The 50^ distillation temperature (T50) of the

gasoline or the present invention is preferablv 75°C or higher, miore preferably 30°C or higher with the objective of pre \'en ting the deteriora-::ion of fuel consumption. The T50 is preferably llO^C or lower, more preferably 105°C or lower, more preferably 100°C or lower with the objective of preventing the deterioration of normal temperature drivability.
The 70% cistillanion temperature (T70> of the gasoline of the presen" inveniicn is preferably 95^C or higher. If the T70 is lower than 55°C, fuel consumption would be poor. The T70 is preferably 135°C or lower, more preferably 150°C or lower. If rhe T70 is higher than 13b^'C, low and rr-iddle temperature drivability of a cc^ld engine would be poor and the amoun"Ls of hydrocarbons in "::he exhaust gas and deposit on intake valves or in a combustion chamber would be
The 90% discillation temperature (T90) of the gasoline of the present invention is preferably 115" C or higher, more preferably 120°C or higher. If the T90 is lower than 115°C, fuel consumption would be poor. The T90 is preferably 180°C or lower, more preferably 175°C or lower, more preferably i70°C or lower, more preferably 165"C or lower with the objective of preventing the deterioration of low and normal

temperature drivaoility of a ccld engine, the dilution of an engine oil with the gasoline, an increase in nydrocarbon exhausi: gas, the degradation of an engine oil, and s]. udge formation.
The end point of the gasoline of the present invention is preferably 150°C or higher. The end point is also preferably 220°C or lower, mi ore preferably

21

J '_ LJ

r lower, more preferably 2C0°C or lower, itiore

preferably 195°C or lower. If the end point is higher than 220°C, deposits on an intake valve or in a combustion chamber tends to be increased and also sm.cldering of a spark plug m.ay occur.
The lE.P, TIG, T50, T50, T70, T90, and EP referred herein denote the values ;°C) measured in accordance with JI3 K 2254 "Petroleum products-Determination of distillation characteristics".

! CVO'- -,- i- b =
V ^ --. ^ ^ »_'

r e s s u r e ! K v i' ■ o t

the Dresent invention is preferably adjusted depending on the season or district where the gasoline is used. More specifically, for warrr, season and district use, the RVP is preferably from 44 to 72 kPa, more preferably from 44 to 65 kPa, more preferably from 50 to 65 k?a, most preferably from 55 tc 55 kPa. Fcr cold season and district use, the RVP is preferably from 60 to 93 kPa, more preferably from 65 to 93 kPa, more preferably from

"0 to S3 k?a, most preferably from 70 to 68 kPa . A too -lich RVP may cause some defects In drlvability due to vapor lock. A tec low RVP may cause the deterioration of startability of a cold engine. The vapor pressure (RVP) referred herein denotes the value (kPa) measured in accordance with JIS K 2258 "Testing Method for Vapor Pressure of Crude Gil and Petroleum Products (Reid Method) " .
Vihen the gasoline of the present invention is used in a regular gasoline-powered automobile, the density at 15" C of the gasoline is preferably 0.690 g/crri^ or greater, more preferably 0.700 g/ cm" or greater, mere preferably 0.710 g/ cm" or greater, most preferably 0.'^15 g/ ciTi" or greater with the objective of preventing the deterioration of fuel consurription and also preferably 0.783 g/cm'' or less, more preferably 0.760 :: / OX" or less, ~c-re preferably 0,750 g/ cm." or less, m.ost preferably 0.745 g/ cm" or less with the objective of preventing the deterioration of acceleration perform.ance or smioldering of a plug.
When the gasoline of the present invention is used in a oremium gasoline-powered automobile, the density at 15°C of the gasoline is preferably 0.700 g/ cm'' or greater, more preferably 0.710 g/ cm'^ or greater, more preferably 0.720 g,/ cm,'' or greater, most preferably

0. .'SO q/ cm' or greater and is preferably 0.783 g/ cm'^ or lower, more preferably 0.77 0 g/ cm' or lower, more preferably C.760 g/ cm' or lower with the objective of preventing the deterioration of acceleration performance or smoldering of a plug.
The density at 15'^C referred herein denotes the value (g/cm"; measured in accordance with JIS K 2249 "Crude petroleum and petroleum products-Determination of density and petroleurri measurement tables based on a reference temperature (15°C)".
The oxidation stability of the gasoline of the present invention is preferably 240 miinutes or longer, mere preferably 48C m,inures or longer, more preferably 1440 minutes or longer with the objective of preventing gum formation during storage.
The oxidatic^n stability referred herein denotes

one vaiue

...— d^j-t^^i _.-

■ = W T

2287 "Testing Method for Oxidation Stability of Gasoline (Induction Period Method]".
The corrosiveness to copper (50°C, 3 hours) of the gasoline of the present invention is preferably 1 or less, m.ore preferably la. If the co r r os i vene s s to copper is greater than 1, the conduits of a fuel system may be corroded.
The corrosiveness to copper referred herein

denotes che value n.easured in acccrdance with JIS K 2513 "Petroleum products-Corrosiveness ZQ copper-CooDer strip test" iTest temperature: 50^C, Test time: 3 h our s) ,
The washed existent gum content of the gasoline of the present in'/ention is preferably 5 mig/100 ml or less, m.cre preferably 3 mg/100 ir,l or less, m,ore preferably 1 mg/lCO ml or less. The unwashed existent gum content of the gasoline is preferably 2C r.g/lCO ir.l or less, more preferably 10 mg/100 ml or less, more preferably 5 mg/100 ml or less. If the washed and unwashed existent gum contents exceed the above values, deposit m.ay formed in a fuel introducing system, or intake valves maj' agglutinate.
The washed and unwashed existent gum contents referred herein denote the values (mg/100 ml) measured

iir -r oau

gasoline and aviation fue1s-Determinati on of existent gum-Jet evaporation method".
The benzene content of the gasoline of the present invention is preferably 1 percent by volume or less, more preferably C.5 percent by volume of less. If the benzene content is more than 1 percent by volume, the benzene concentration in the exhaust gas may be increased.

The benzene content referred herein denotes the benzene content (percent by volume) measured in accordance with JIS K 2536 "Liquid petroleumi products-Testing method of components-Determination of aromatic by gas chromatography".
When the gasoline of the present invention is used in a regular gasoline-powered automobile, the arcmatic content of the gasoline is preferably AO percent by vclum.e or less, more preferably 35 percent by volume or less, more preferably 30 percent by volume or less. If the aromatic content is more than 40 percent by volume, deoosits on an intake valve or in a combu stion chamber tends to be increased and also smoldering of a spark plug ir,ay occur. Further, the benzene concentration in the exhaust gas may oe increased. The arom.atic content is preferably 10 percent by volume or more, mere oreferably 15 oercent by vol urn e or mere. If the arom.atic content is lower than 10 percent by volume, fuel consum.ption would be poor.
When the gasoline of the present invention is used in a premium gasoline-powered automobile, the aromatic content of the gasoline is preferably 45 percent by volume or less, more preferably 42 percent by volume or less, more preferably 40 percent by vo lume of less. If the aromatic content is more than 45 percent by volume

or more, deposits on an intake valve or in a combustion chamber tends to be increased and also sncldering of a spark plug .may occur. further, the benzene concentration in the exhaust gas may be increased. The aromatic content is preferably 20 percent by volume or iTiOre, preferably 25 percent by volume or more. If the aromiatic content is lower than 20 percent by volume, fuel consumption would be poor.
The aromatic content referred herein denotes the arom.atic content (percent by volume) in a gasoline m.easured in accordance with JIS K 2 5 36 "Liquid petroleum oroducts-Testing miethod of com.ponent s-Fluore scent indicator adsorption method" .
The olefin content of the gasoline of the present invention is preferably 35 percent by volume or less, miore preferably 25 percent by volume or less. If the

.^ ^ _ — ■
: cy vo_ume, tne resulting gasoline would be poor in oxidation stability and increase deposits on an intake valve.
The olefin content referred herein denotes the olefin content (percent by volume) in a gasoline measured in accordance with JIS K 2536 "Liauid petroleum products-Testing method of components-Fluorescent indicator adsorption method".
The amount of entrained kerosene in the gasoline

of the present invention is preferably 4 percent by volume or less. If the enorair.ed amount exceeds 4 percent by volume, engine soartability would be poor.
The amoijnt of entrained kerosene referred herein is determined by the content of n-paraffinic hydrocarbons having 13 and 14 carbon atoms on the basis of the total mass of a gasoline and denotes that the corresponding value of kerosene obtained in accordance with JIS K 2535 "Liquid petroleum produets-Testing method of co rr.ponent s" is 4 percent by volume or less.
The manganese content of the gasoline is preferably 2 ppm by mass or less^ more preferably 1 ppm by mass. Z'h^^ iron content of the gasoline is preierabl;;" 2 ppm by mass or less, more preferably 1 ppm by r:,ass or less. The sodium content of the gasoline is preferably 2 pprri by mass or less, more preferably 1 ppm
is preferably 2 ppm by mass or less, more preferably 1 ppm by mass or less. The phosphorus content of the gasoline is preferably 2 ppm by m.ass or less, preferably 1 ppm by mass or less, more preferably 0.2 ppm by mass or less. If the contents of manganese, iron, sodium, potassium, and phosphorus exceed the above-described values, the efficiency of an exhaust gas purifying system may be degraded due to an increase in deposition

tnese substances on an exhaust

purifying

catalyse, degradacion cf a catalyst support, and dSLerioraiiior- of an air-fuel ratio sensor.
The manganese, iron, and sodiumi contents referred herein denote the values measured by "combustion ashing- inductively couplec plasma atomic emission spectre mi etry". Tne potassium content, referred herein denotes the value measured by " combus tion ashing-a-cn-, ic absorption spectrometry". The phosphorus content referred nerein denotes the value measured in accordance with ASTM D3231 "Standard Test Method for Phosphorus in Gasoline".
The procedures of "combustion ashing-induorive1y coupled plasm.a atom.ic emassion spe cr r ome t r y " and "corribustion ashing-at omiic absorption spectrometry" are as follows:
_ ^^ „ ^ Ci
d "i '-^ ^ ■
(2) 0.4 g of powdery sulfur is added so as to prevent sublimation of the constituent elements and the dish is placed on a sand bath at a temperature of 150°C for one hour so as to remove the volatile matters;
(3) the residue is combusted;
(4) line combusted residue is ashed in an electric furnace kept at a temperature of 500°C for 2 to 3 hours;

(5'! the ash is dissolved with 2 to 3 ml of concentrated sulfuric acid and diluted to be 2G mL in V c 1 u X, e ;
(6) the manganese, iron, and sodium con-ents are analyzed using an inductively coupled plasma atomic emission spectrometry analyzer (ICPS-8000 manufactured Dy SHIMADZU CORPORATION), and the phosphorus content is analyzed using an atomic absorption photometer (Z610C manufactured by Hitachi, Ltd. ) .
The gasoline of the present invention preferably contains an anti-oxidant and a metal deactivator for storage stability. Specific examples of the anri-oxidant include phenylene diam.ine-based anti-oxidants such as N,K'-diisGpropyl-p-phenyl&ne diamine and N ,!; ' - di i s obc t y 1-p-pheny 1 ene diam.ine and alkyl phenol-based anti-oxidants such as hindered phenols typically 2,6-di~t-butyl-4-methyl phenol. Examples of the metal deactivator include compounds known as metal deactivators, i.e., amiine carbonyl condensation compounds such as N,N'-disalicylidene-l,2-diamino propane.
There is no particular restriction on the amount of the anri-oxidant or metal deactivator to be added.

The anti-cxidart or metal, deactivator is added so that the above-described oxidation stability of the gasoline falls within the preferable range and the unwashed existent gum content of the gasoline after other additives are added thereto falls within the above-described preferable range. More specifically, ■::he anti-oxidani: is added in an amount of preferably 5 -0 ICO mg/1, more preferably 10 to 50 m!g/l. The ir.etal deactivator is adced in an amount of preferably 0.5 to 10 mg/1, iTiOre preferably 1 to 5 mg/1.
The gasoline of the present invention may contain a derergent-dispersant so as to preven":: the accum.ulat ion of deposits on an intake valine or rhe like. Z^he det e rgent-di spe r sant may be any compound known as a detergent-dispersanr for gasoline such es succinirnide, polyalkyl air.ine, and polyether amine.
decom.posed completely when subjected to therrrial decomposition at a temperature of 300°C . The detergent-dispersanr is more preferably polyisobuzenyl amine and/or polyether am.ine.
The content of rhe detergent-cispersant is preferably from 25 to 1000 mg per liter of the gasoline. With the objective of preventing the formation of deposits on an intake valve and reducing deposits in

a combustion chamber, the content is m^ore preferably frorr. 50 c o 500 mg, miost preferably from 100 ro 300 :r,q . The effecLive coiriponents contributive to detergency of scm.e detergent-dispersant s are diluted wi^h a suitable solvent. In the case of using such
detergent-dispersants, the above-described content rr.eans the con rent of 'he effective cosr.ponents.
The gasoline of zhe present invention may contain 3 iriczion modifier so as to imiprove its lubriciry. When the gasoline is used in a premium ga s o 1 ine-powe r ed automobile in particular, the gasoline preferably contains a friction modifier.
Exam.ples of the friction modifier include alcohols; alcohol comipounds of 1 to 30 carbon atons, having 1 to 4 hydrcxyl groups; carboxylic acids; hydroxyl group-containing esters which are reaction

■ X V „ 1

_^V_x^_l- '^^

trihydric alcohols; esters of polycarboxylic acids and polyhydric alcohols; esters of polyhydric alcohols and nitrogen compounds having a chemical composition containing >NR {R is a hydrocarbon group having 5 to 40 carbon atoms and having one or more substituents; and air.ide compounds of carboxylic acids and alcohol amines. These friction modifiers may be used alone or in combination. Preferred are hydroxyl

group-containing esters which are reaction products of monocarboxylic acids having IC ro 25 carbon atones and glycol or trihydric alcohols snd/or ar.ide com.pounds cf carboxyiic acids having 5 to 25 carbon atoms and alcohol amines. More preferred are esters of monocarboxylic acids having 10 to 25 carbon atoms and glycerin esters and/or air.ide compounds of monocarboxylic acids having 5 to 25 carbon atoms and diethanol arr. ine.
There is no particular res-criction on rhe amouni: of the friction modifier. However, the fricrion miodifier is preferably added so that the unwashed existent gum concent of the gasoline after ocher addicives are adoed thereto falls wirhin the above-described preferable range. "'he friction modifier is added in an amount of preferably 1 r,g, muore preferably 30 to 25C mg per liter o

"■-' — _ V ^

consumipr ion and an engine outouc and because a further improve mi ent may not be expected when it is added more. Some products in the name of friction modifier are commercially available in a state wherein the effective components contributing to wear resistance is diluted with a suitable solvent. in the case where such products are added to the gasoline of the present invention, the above-described amount means the amount

oi "he effective comoonen-s.
Examples of c^her additives which muay be added to ihe gasoline of rhe presen' invention include surface ignition inhibitors such as organic phosphorus compounds, anti-icing agents such as polyhydric alcohols and ethers thereof, combustion improvers such as alkali or alkaline metal salts of organic acids and sulfuric esters of higher alcohols, anti-staric additives such as anionic, cat:icnic, and air.phcteric surface active agents, coloring agents such as azo dye, rust inhibitors such as organic carbcxylic acids , rheir derivat:ives and alkenyl succinic acid esters, water draining agents such as sorbiran esrers, markers such as quinizarin and coumarin, and odorants such as perfuiT.es synthesized from natural essential oils.
These additives m.ay be added alone or in

„'^.._ ^ =1 L,_^_^.

percent by mass or less on the basis of the total mass of the gasoline.
The gasoline fraction produced by the nydrotreatment process of the present invention may also be used as a feedstock for the use in a catalytic reforming unit. When the feedstock contains biomass, io can advantageously provide an effect to reduce

csrbon dioxide emissions escimated in view ot life cycle (LCA-C0:I upon production of hydrogen, feel for gasoline engines and benzene, toluene and xylene, which are basi.c raw materials of petroleum chemical products. That is, the present invention can provide hydrogen, fuel for gasoline engines and basic raw materials of petroleum chemical products such as benzene, toluene and xylene, all of which can reduce LCA-CO2 sufficiently.
The fractions of rhe h\'droi:reated oil produced by the present invention may be partially reformed ir. a sceam reform: in g unit or a oaralycic refer rriing unit thereby producing hydrogen. When the feedstock contains biorriass, rhe resulting hydrogen has properties, so-called carbon neutral and T:hus can reduce envi ronm;enr loads upon production of hydrogen
With regard to the hydrotreaued oil produced by the present invention, a kerosene fraction with a boiling point of 220 to 350°C can be suitably used as diesel gas oil or heavy base oil. When rhis fraction is used as diesel gas oil, its sulfur content is preferably 10 ppm by mass or less. If the sulfur contenu exceeds the upper limit., the fraction would adversely affect a filter or catalyst used in the

exhaust gas processing device of a diesel engine. The hydrotreated oil may be used alone as diesel gas oil or heavy base oil but r.ay be used as diesel gas oil or heavy base oi]., mixed with componenrs such as other base oils. E X a rr,p les of the other base oils include gas oil fractions and/or kerosene fractions that are produced in a conventional nydroreiining process and residue fraczions produced by ths present invention. r'urther, the kerosene fraction rriay be mixed winh a synthetic gas oil or kerosene produced through a Fischer-Tropsch reaoricn using synthetic gas as the feedstock. The synthetic gas oil or kerosene contains little aromatic and contains safjrated hydrccarbcns as tne main comipcnent ana is high in cetane number. There is no particular restriction on the method of producing the synthetic gas. Therefore, any conventional method rr;ay
; Applicability in the Industry]
The present invention provides a process of hydrotreating a feedstock comprising a fat c omponent originating from, an animal or vegetable oil. The present invention also provides an environment friendly gasoline base oil and an unleaded gasoline composition, which are effectively accomplish a

reduction in carbon dioxide em. issions, through rhe hyarctreatmenz process.
[ Examp1e 3 j
Hereinafter, the present invention will be described in more details by way of the following examples and com.parative exam.ples, which should not be construed as limiting the scope of the invention, (■preparation of catalyst A)
A Y-tyoe zeolite with a ratio of the silica to the alumina (Si02/Al20s) of 5 was u11ra -stabi1ized by hydrothermal rreatment at 780°C for one hour under saturated steam armcsphere using a steaming device and

■n s uo "; e c t e ■

acid treatm.ent with a IN nitric acid

aqueous solution thereby producing 210 g of a prcton-tyoe ultra-stabilized Y-type zeolite wiuh s
diffraction and a ratio of the silica to the aimriina (SiOs/Al.O;) of 30.
On the other hand, 185 g of sodium, silicate No. 3 was added to 3000 g of an aqueous solution of 5 perceno by mass of sodium aluminate and then put into a vessel kept at a temperature of 65°C. In a separate vessel kept at a remperature of 65°C, 3000 g of an aqueous solution of 2.5 percent bymass of aluminum sulfate were

prepared. The foregoing sodium alurtiinate aaueous solution was added dropwise thereto. When the pH of the mixture reached "^.0, the addition was stopped. The resulting slurry product was passed through s filter thereby producing a cake-like slurry.
The resulting slurry was transferred to a vessel equipped witih a reflux condenser, and 150 ml of distilled water and 10 g of an aqueous solution of 27% £ mm on la "were added thereto, followed by 2C hour stirring at "^S^C. The slurry was put into a kneader and kneaded, while being heated at a temperature of 8G°C or higher to remove water, thereby producing a o^ay-like kneaded mi ass. To the kneaded mass were added Itc g of zhe foregoing ultra-stabilized Y-type zeolite, followed by further <.neading. The resulting kneaded

IT. ass was extruded into the form

cylinder with a

L_:^__."_r:r J_ _-„

-—■■' ^ - ^ ..

at a temiperature of 110°C for one hour and calcined at a temperature of 550°C thereby producing molded support A.
Into an eggplant type flak were put 50 g of the resulting molded support A and 35 ml of a mixed aqueous solution of tetramine platinum (II> chloride and tetamiine palladium (11) chloride. Whereby, the metals contained in the solution was impregnated into the

support while being deaera^ed wirh a rotary evaporator and dried ao a temperature of 110"C and then calcined at a temperaoure of 3 5 0^0 "hereby producing catalyst A. The amounts of platinurri and palladium supported on the catalyst were 0.5 percent by mass and 0.7 percent by mass, respectively, on the basis of the total mass of the catalyst. (Preparation of catalyst 3)
Into a vessel kept at a temperature of 6 5°C were put 30CO g of an aqueous solution of 5 percent by mass of sodiuiTi aluminate. In a separate vessel kept at a temperature of 6 5 "^ C were prepared 5000 g of an aqueous solution of 2.5 percent by mass of aluminumi sulfate, followed oy drop wise addition of the sodium alurr.inate aqueous solution. Tne addition was stopped when the pH of the miixture reached 7.0, and the resulting slurry
a cake-like slurry.
The resulting slurry was transferred to a vessel equipped with a reflux condenser, and 150 ml of distilled water and 10 g of an aqueous solution of 27% ammonia were added thereto, followed by 20 hour stirring at 75°C. The slurry was put into a kneader and kneaded, while being heated at a teraoerature of 80°C or higher to remove water, thereby producing a

clay-like kneaded T, ass . The resulting kneaded mass was extruded inro the form oi a cylinder with a diameter of 1,5 mm, chrough an extruder and then dried at a cemperarure of 110°C for one hour and calcined az a tem.perature of 5 5 0'^ C thereby producing molded support 3.
Into an eggplant type flak were put 50 g of the resulting rriolded support B and 35 rril cf a mixed aqueous solution of dinitroamiine platinum (II) and dinitroamiine palladiurri til) . Ihe m.etals contained in the solution was impregnated into the support while neing deaerated with a rotary evaporator and dried at a temoerature of 11C°C and then calcined at a

- err.Dera

thereby producing catalyst 3. The

amounts of plati nurri and palladium, supported on the catalyst were 0.5 percent by m.ass and 0.7 percent by

•■ — _ ^v ,

t a _L m. a s s

the catalyst.
''Preparation of catalyst C)
Into an eggplant type flak were out 50 g cf molded support A produced above and then a solution containing 10.0 g of molybdenum trioxide, 18.3 g of nickel (II) nittate hexahydrate, 0.9 g of phosphoric acid (85 percent concentration) and 4.0 g of malic acid. The metals contained in the solution was impregnated into

the support while being deaerating with a rotary evaporator and dried at a temperature of 12 0"C for one hour and calcined at a tem.perature of 55 0^C, tnerecy prod-jcing cszalyst C . The amounts of nickel and molybdenum supported on catalyst C were 4.0 percent by mass (in the form of nickel oxide) and 16.0 percent by mass lin the form ci molybdenum oxide), respectively, in terrr.s of oxide, on the basis of the total mass of the catalyst. (Preparation of catalyst D)
Into an eggplant type flak were put 50 g of molded support 5 produced above and a solution containing 10.0 g of m.olybdenum trioxide, IS. 3 q of nickel (11 ;■ nitrate hexahv-drate, 0.9 g ot phosphoric acid :85 percent concentration) and 4.0 g of malic acid. The metals contained in the solution was i mo regnated into the
ar.d dried at a terr.pera t u re of 12G°C for one hour and calcined at a temperature of 550°C, thereby producing catalyst D. The amounts of nickel and molybdenum supported on catalyst D were 4.0 percent by mass (in the form of nickel oxide) and 16.0 percent by mass (in the form of molybdenum oxide), respectively, in terms of oxide, on the basis of the total m^ass o£ the catalyst.

'Example 1!
Catalysr A (50 ril; was charged into each of a first reacricn tube (inner diarreter of 20rr.rri) and a second reaction tube (inner diameter of 2 0mm), both of which were installed in series in a fixed bed circulation type reactor. Thereafter, the catalyst was subjected to a reduction rreatir.ent under conditions where the average catalyst layer temperature was 300°C, the hydrogen partial pressure was 5 MPa, the hycrcgen gas rate was S3 ml/min, for 6 hours.
Thereafter, a feedstock that was palm oil (the ratio of the compound having a triglyceride structure in the oxygen-concaining compound: 96 percent by mole) was r. y d r o t r e a t e d using the catalyst . The f e e d s c o c K had a densiry at 15^C of C.516 g/ml and an oxygen ccntent of 11,■^ percent by mass. The hydrotreatment was
temperature, pressure and liquid hourly space velocity in the first and second reaction tubes were 415°C, 5 MPa and 0.45 h'^, respectively. The volume ratio of hydrogen gas introduced between the first and second reaction tubes (quenching hydrogen ratio) was 20 percent by volume of the total hydrogen introduced in the reactor, and the hydrogen/oil ratio determiined by the total hydrogen introduced in the reactor was 1010

Nl/'L. The resulting hydrotreatec ci_ was measured to determine the oxygen and sulfur contents, the yield of each fraction, and the oxygen and normal paraffin contents in the naphtha fraction with a boiling point range of 80 tc i35°C (fraction corresponding to hydrocarbons having 5 to 10 carbon atoms). The results are set forth in Table 1 belcw.
■; Ccm.para t ive Exam.ple 1)
Hydrotreatment was carried out with the same procedures of Examiple 1 except for using catalyst 3 instead of catalyst A. The resulting hydro treated oil was measured in the same respects as in Ex amp 1 e 1 . The results are set forth in Table 1.
( Ex am.D 1 e 2)
~ ^ ^ reaction tube (inner diameter of 20mm) and a second reaction tube (inner diameter of 20m.m), both of which were installed in series in a fixed bed circulation type reactor. Thereafter, the catalyst was pre-sulfided with a straight gas oil (sulfur content: 3 percent by mass) to which dimethy1disu1fide had been added, under conditions where the average catalyst layer temperature was 300°C, the hydrogen partial presjsure

was 6 M?a, the liquid hourly space velcxity was 1 h'', and the h y d r o g e n/o i1 ratio was 2 C 0 H L/L, for 4 hours.
Thereafter, a feedsiock prepared by adding dirriethylsulfide to palm oil {nhe ratio of the compound having a triglyceride structure in the
oxygen-containingccm,pound: 96 percent by rr.ole} so that the sulfur content of the feedstock was adjusted to 51 ppm by mass was subjected to hydrotreatment using the catalyst. The feedstock had a density at 15°C of 3.916 g/rr.l and an oxygen content of 11.4 percent byrr.ass. The hydrotreatment was carried out under conditions where the reaction temperature, pressure and liquid hourly space velocity m the first and second reaction tubes vjere 425°C, 5 M?a and C.4 h'', respectively. The vclumie ratio of hydrogen gas introduced between the first and second reaction tubes (quenching hydrogen ratio; was
- r^ S - - '^ j^
in the reactor, and the hydrogen/oil ratio determined by the total hydrogen introduced in the reactor was 1010 NL/L. The resulting hydrotreated oil was measured to determine the oxygen and sulfur contents, the yield of each fraction, and the oxygen, sulfur and normal paraffin contents in the naphtha fraction with a boiling point range of 80 to 135°C (fraction corresponding ho hydrocarbons having 5 to 10 carbon

atoms). Tne results are set forth in Table 2 belcw.
( C omp a r a t i V e :^ x a^.p 1 e 2 )
Hydrotreatner.t was carried out with the same procedures of Example 2 except that catalyst D was used instead of catalyst C and the reaction teraperature in the firsz and second reaction tubes was changed to 43 0°C The resulting hydrotrea~ed oil was measured in the same respe c~s as in Ex air.ole 2. The resul-s are set forth m Table 1.
i.Examples 3 to 6, and Comparative Examples 3 and 4)
Catalyst E was prepared by supporting C.5 percent bj-mass of platinum, and C,"^ percent by mi ass oipallsdiumi
3 the Group 3 of the periodic table, on
t: h a t belong
■rt comiposea of ZD percent oy m.ass oi an

m.et al ios i li oate with a faujasite type structure, 15.75 percent by !T:ass oz silica, and 29.25 percent by nass of alum.ina. The s i 1 ica / a lum.i na ratio of the ultra-stable Y-type zeolite was 33.
The feedstock to be hydrotreated was palm oil that was biomass vegetable oil. The palm oil had a triglyceride content of 98 percent by mole, an oxygen content of 11.4 percent by mass, and a sulfur content

of less ~r_an G.l nprr. ty m.ass.
After catalyst E was subjected to a pre-reduction treatment, hydrcureatmem: was carried OUT: cy contacting the catalyst with the feedstock that was palm oil, under conditions where the reaction temperature was 425°C, the hydrogen pressure was 5 MPa, ^ h e liquid hourly space velocity was 0.4 h ~", and -he hydrogen/oil racio was lOlC NL/'L-. The resulting oil was distilled thereby producing biomass hydrotreated bass oil E that is a fraction having a distillation temperature range of 55 to 135°C. The resulting biomass base oil E had a oxygen content cf less than 0.1 oercent by m.ass, a sulfur content of less than 0.1 ppm. by mass, and a norrrial paraffin content of 24.8 cercent by mass.

The qasolme com.Dosi

of Exem.ple 3 was prepared

hydrotreated base oil E, gasoline base oils such as a light reformied gasoline {distillation temperature range of 27 to 123°C, densiry of 0.690 g/cm^, aromatic content of 23 percent by volume), a middle-heavy reformed gasoline (distillation temperature range of 92 to 195°C, density of 0.853 g/cm'^, aromatic content of 90 percent by volume), a light catalytic cracked gasoline (distillation temperature range of 27 to 8l°C,

density cf C,656 q/'cm", olefin content of 47 percent by Vo 1 ■_:rrs I , s heavy catalytic cracked gasoline (distillation temperature range of 75 to 193'=C, density of 0.764 g/crri'^, olefin content of 33 percent by volume), an alkylate (distillation temperature range of 33 to 179=C, density of 0.656 g/cm\ saturate content of lOO percent by vcluiTie), a light naphtha ( di s til la t icn temperature range of 2 3 to 10 5° C, density of 0.637 g/cm^, and saturate content of 59 percent by volune), toluene, ana normal butane, an anti-oxidant, and a metal deactivator.
The gasoline corr.po s i t i on of Example 4 was prepared

-. V o r

■ d base oil

, ' iJt

■ent cy volume or 3TB!

produced from a biomass-originating ethanol, gasoline base oils such as a light reform.ed gasoline
of 0.690 g/cm^, aromatic content of 23 percent by volume), a middie-neavy reformed gasoline
(distillation temiperature range of 92 to 125°C, density of 0.853 q/cm\ aromatic content of 90 percent by volume), a light catalytic cracked gasoline
(distillation temperature range of 27 to 81°C, density of 0.656 a / cm'^, olefin content of 47 percent by volume) , a heavy catalytic cracked gasoline (distillation

^moersture rsnae

_.■ J- -^

tG 198°C, density cf C.764 c/cm' ,

olefin content of 33 percent by vclLme), an alkylate (distillation terriperature range of 33 to 179^C, density of 0.696 q/cm-*, saturate content of ICO percent by volume), a light naphtha ( disti11 ation temperature range of 26 tc 105°C, density of Q-oS"; g/crc,"', and saturate content of 99 percent by volume), toluene, and r.orm.al butane, an ant i - ox i dan t, and a metal deactivator.
ith a
Catalyst ? was prepared by supporting 4.0 percent by mass of nickel (in the form of nickel oxids) and 15.0 percent by mass of molybdenum (in the form, of molybdenum, trioxide) that belong to the Groups 3 and 6A of the periodic taole, respectively on a support com.posed of 55 oercent by n".as3 cf an ultra-stable y-type zeolite containing a crystalline metallcsilic.
: a t e w

— zi-—-^^^-^^^f — -J -

V ... CL i :3

silica, and 29.25 percent by mass of alumina. The silica/alumina ratio of the ultra-stable Y-type zeolite was 30.
The feedstock tc be hydrotreated was prepared by adding dime thy1disu1fide to palm oil that was biomass vegetable oil (triglyceride content of 98 percent by mole, oxygen content of 11.4 percent by mass, and sulfur content of less than 0.1 ppmbymass) so that the sulfur

consent of the feedstock was adjusted to 51 ppm by mass.
Thereafter, hydrotreatrr.enT: was carried cut by contacting z'r.e catalyst with the feedstock, i.e., the fcrgoing dimethy_disulfide~added palm oil, under conditions where the reaction temperature was 425^C, the hydrogen pressure was 5 MPa, the liquid hourly space velocity was 0.4 h'', and the h y d r o g e n/o i1 ratio was iCiC NL/L. The resulting oil was distilled thereby producing biom.ass hydrotreated base oil F that is a fraction having a distillation temperature range of 35 to 135°C. The resulting biomass base oil F had a oxygen content of less than 0.1 percent by mass, a sulfur content c f 1.3 p o m b \" m; a s s , a n d a n o r mi a ". paraffin content of 24.3 percent by m.ass.
The gasoline com.position of Example 5 was prepared oy blending 10 percent by volume of biom^ass
light reformed gasoline (distillation temperature range of 27 to 123°C, density of 0.690 g/cm.^, arom.atic content of 23 percent by vol um e), a miiddle-heavy reformed gasoline (distillation temperature range of 92 to 195°C, density of 0.8 53 g/cm'', aromatic content of 90 percent by volume), a light catalytic cracked gasoline (distillation temperature range of 27 to 31°C, density of 0.656 q/cm^, olefin content of 47 percent

by volume), a heavy catalytic c r a c k.ed gasoline ■distillation t e-T.pe r a t j re range of 75 to 1 9 8'^ C , density of 0.764 g/cn", olefin content of 33 percent by volur.e) , a:: alkylate (distillation temperature range of 33 to 179°C, density of 0.695 g/cn'', saturate content of 100 percent by volume), a light naphtha(distillation t em.pe rat u re range cf 28 to lOB'^C, density of u.657 g/cm'', anc saturate content of 99 percent by volurrie) , toluene, and ncrrral butane, ananti-oxidant, a m.etal deactivator, and a detergent-dispersant.
The gasoline coitiposi t i on of Example 6 was prepared by blending 10 percent by volume cf biomass hydrctreated base oil 7, 3 percent by vclum.e of a bioiTiass-originating ethane 1, gasoline base oils such as a light reformied gasoline ( c i s t i 1 la t i on temperature range cf 27 to 128''C, density of 0.690 g/cmi", arcrr.atic
refer m;ed gasoline (distillation t em^pe nature range of 92 to igs^'C, density cf 0.353 g/cm'\ aromatic content of 90 percent by volume), a light catalytic cracked gasoline (distillation temperature range of 27 to 81°C, density of 0.656 g/cm'', olefin content of 47 percent by volumis), a heavy catalytic cracked gasoline (distillation temperature range of 75 to 198''C, density of 0,764 g/cm^, olefin content of 33 percent by volume) ,

an alkylate fdisTiillaticn teiriperature range of 33 to 1"/9''C, density of 0.695 g/cm", saturate content of ICG percent by volu-ie;, a light naphcha^distillaricn temperature range of 23 to 105°C, density of 0.637 g/cm', and saturate content of 99 percent by volume), toluene, and normal butane, an anti-oxidant, a metal deactivator, a detergen--dLspersant, and a friction modifier.
The gasoline composition of Comparative Example 3 was prepared by blending 55 percent by volum.e of biomass hydrotreated base oil E, gasoline base oils such as a light reformed gasoline (distillation temiperacure range of 27 to 128'^C, density of C.69C a / cm', aromatic content of 25 percent by volume), a IT. iddle-heavv reformied gasoline (distillation temperature range of 92 to 195^C, density of 0.853 q/cm', arcmiatic content of 90 percent by volume), a light

^ „_„„i-;.-,-^

._5 L ^ = ^ J. o:. ^TTiLO'ers

range of 27 to 81°C, density of 3.656 g/'cm", olefin content of 47 percent by volume), a heavy catalytic cracked gasoline (distillation temperature range of 75 to 198°C, density of 0.764 g/cm^, olefin conrent of 33 percent by volume), an alkylate (distillation temperature range of 33 to 179°C, density of 0.696 g/cra^, saturate content of 100 percent by volume), a light naphtha{di3ti1lation temperature range of 28 to 105°C,

density cf 0.657 g/'cm", and saturate center t ct 99 percent by vcluir.ej, toluene, and normal butane, an ar. ti-oxidanr, and a metal deactivator.
The com.positjon of Comiparative Example 4 is a commercially available regular gasoline.
Table 3 sets forth the properties of each gasoline comcGsit ion .
^Exam.ples ~i to 10, and Comparative Exam.ples 5 and 6) The gasoline composition of Examiple 7 was prepared with the same procedures of Example 3 except that the amount of biomass hydrotreated base oil E was changed "o 5 percent by volume.
The gasoline con".position of Exam^ple 6 was prepared "with the sam.e procedures of Example 4 except that the amiount of biomiass hydrotreated base oil E was changed
The gasoline composition of Example 9 was prepared with the same procedures of Example 5 except that the amount of biomass hydrotreated base oil F was changed to 5 percent by volume.
The gasoline compo sition of Examp1e 10 was preoared with the same procedures of Example 6 except that the amount of biomass hydrotreated base oil F was changed to ~ percent by volume.

The gasoline composition of Comparative Example 5 was prepared wirh the same procedures of Comiparative ~xample 3 excepc chat the amount of tiiomass hydrctreated base oil E was changed to 4 0 percent by V o 1 u mi e .
The CO mi position of Ccm.parative Example 6 is a com.mier oia lly available premium gasoline.
Table 5 sets forth the properties of each gasoline comicos it ion .
i'Deter m: ins-ion of properties)
The orooerties of the gasoline com.positions of the ex.amiples and comparative examiples were determined by the following methods.
Research octane number and miotor octane numbers are values mi-asured in accordance with JIS K 22S0
numiber, cetane number and calculation of cetane index".
Sulfur content was measured in accordance with JIS K 2541 "Crude oil and petroleum products-Determination of sulfur content".
Lead content was measured in accordance with JIS K 2255 "Petroleum products-Gasoline-Determination of lead cont en t".
Distillation characteristics (IBP, TIG, T30, T50,

T"70, T90, ar.d EP are all measured in accordance wirh JIS K 2254 "Petroleum products-Determ.inaticn of distillation oharacteristios".
Vapor pressure (33"^.8°C) was rrieasured in accordance with JIS K 2258 "Testing Method for Vapor Pressure of Crude Oil and Petroleum Products (Reid Method) " .
Density (@15°C: was rrieasured in accordance with JIS K 2245 "Crude petroleum, ar.d petroleum products-Deter m,i nation cf density and petroleum measurement tables based on a reference temperature ( 1 5 = C ) " .
Cxication stabilirv was measured in accordance

w n ^ 1 i

K 223.■■ "Testing Met hoc for Cxidaoicn Soabllity

of Gasoline (Induction Period Method)".
Corrosivenes3 oo copper was measured in
products-Corrosiveness to copper-Ccpper strip test" (Test temperature: 50°C, Test time; 3 hours) .
Unwashed existent gum, and washed existent gum contents were measured in accordance wi::h JIS K 2261 "Petroleum Products-Motor gasoline and aviation f ue 1 s-Det erminat ion of existent gumi-Jet evaporation method".
Benzene content was measured in accordance with

CIS K 253 6 "Lig'jid peLrcleum prodiJC"S-Testing method of cc~ponents-Der. erm. inat^ion of arcm.atic conpcnents by gas c h r c m a t o g r s p h y" .
Arcrriatic and olefin contents v.'ere measured in accordance with JIS K 2536 "Liquid petroleuTi products-Testing rr.ethod of compone nts^Fluorescent indicator adsorption ir.ethcd".
Kerosene content was measured in accordance with "Liquid petroleum products-Testing method of c omponer. t s " .
Kanganese^ iron and sodiun contents were measured by "com.bustion a s h i ng - i ndu c t i ve ^ y coupled plasma atom.ic emission s oe ct r oir.e t ry " . Fctassium content was measured by "combustion a s r. ing - at om.i c absorption spectrom.etry". Phosphorus content was measured in accordance with ASTM D3231 "Standard Test !-^ethcd for
(Content of biomass-originating base oil)
For the compositions of the examples and comparative examples, the content of the biomass-originating base oils and the content of the vegetable oil-originating base oils of the biomasses were indicated from the blend ratio of the base oils. (Acceleration performance evaluation)
On a chassis dynamometer whose environment

eirperature and nuir.idity were kept at. 25° C and 5C%,

acceleration

formance was evaluated using the

following test vehicles ; vehicle 1 for regular gasolines and veh-'cle 2 for premium gasolines) . After the vehicles was sufficiently warmed up, full throttle acceleration from 50 km/h to 110 km/h in D-range (OD was en) was repeated 10 tim.es so as to m.easure the ~irre reqaired until the speed reached from 60 km. /h to 100 km/h. The average time of the 7 acceleration runs excluding the first 3 time run was defined as acceleration time.
[Test Vehicle^: vehicle 1
Engine: in-line four-cylinder ^regular
gasoline-powered)
Displacement: 14 98 cc
Injection rr.Dde: multi point injection
Exhaust-gas purifying system: ternary catalyst, air/fuel feedback control system Adopted to 2000 Exhaust Gas Emission Regulation ;Test Vehicle]: vehicle 2
Engine: in-line four-cy1inder (premium gasoline-powered with a supercharger) Displacement: 1998 cc

Injection mode: muiti point injection Transmission: automatic transmission Exhaust-gas purifying system: ternary catalyst, air/fuel feedba~k control system Adopted to 2D0O Exhaust Gas Emission Regulation (Exhaust gas test)
An exhaust gas test was carried out using the aoove vehicles by m.easuring the emissions of CO and KOx contained in the exhaust gas, in accordance with the technical guideline of the 10/15 mode exhaust em.issions measure mient for gasoline-powered automobiles supervised by Ministry of Land, Infrastructure, and Transport Japan. (Fuel con sum.pt ion test)
A fuel cor.sumotion test was carried out using the
accordance with the 10/15 m.ode fuel consumption test procedures for g a s o 1 ine-powe r ed autom.obiles supervised by Ministry of Land, Infrastructure, and Transport Japan.
As set forth in Tables 4 and 6, it is confirmed that the gasolines of the present invention (Examples 3 to 10) comprising biomass-criginating base oils are contributive to diversification of fuel sources and

prohibition of ar'. increase in life oycle CO: and car. achieve excellent acceleration performance and fuel c c n s u rr, p t i c n and reduced exhaust gas (CO, N 0 x ) level.

Claims
i. A process for hydroiireating a feedstock, feedstock into contact with a catalyst in the presence of hydrogen the feedstock containing an oxygen-containing compound, the catalyst c 0 m p r i s i r. g a support t a i n i n g a crystalline metallcsilicate and cm rc more types of metals selected Group elements of the periodic table.
2. A process for hydrotreating a feedstock,
comprising bringing the feedstock nit contact with a
catalyst in the presence of hydrogen, the feedstock
containing an ex y g e n-c not a i n i ng ccrr.pound and a
fur-containing compound, the catalyst comprising a curtaining a crystalline and

3. The process according to claim 1 or 2, wherein
the feedstock is contacted with the catalyst under such
conditions that the oxygen content and normal paraffin
content of the fraction in a boiling point range of 80
to 135°C of the resulting hydro treated oil are 0.2
percent by miss or less and 30 percent by mass or less,
respectively-