Process for desulfurizing catalytically cracked gasoline

Description

FIELD OF THE INVENTION

[0001] The present invention relates to a process for desulfurizing catalytically cracked gasoline. More particularly, the present invention relates to a process for hydrodesulfurizing catalytically cracked gasoline containing sulfur compounds and olefin components in the presence of a catalyst.

BACKGROUND OF THE INVENTION

[0002] In the field of petroleum refining, catalytically cracked gasoline is a stock of high-octane number gasoline containing a certain amount of olefin components. Catalytically cracked gasoline is a gasoline fraction obtained by catalytically cracking a heavy petroleum fraction as a stock oil, such as a vacuum gas oil or an atmospheric residual oil, and recovering and distilling the catalytically cracked products. Catalytically cracked gasoline is a primary blending stock of automotive gasoline.

[0003] However, the stock oil for catalytic cracking has a relatively high content of sulfur compounds. When an untreated stock oil is subjected to catalytic cracking, the resulting catalytically cracked gasoline also has a high sulfur compound content. The resulting gasoline fraction would cause environmental pollution if used as a blending stock of automotive gasoline.

[0004] Consequently, the stock oil is usually subjected to a desulfurization process prior to catalytic cracking.

[0005] On the other hand, a naphtha fraction obtained by distilling crude oil is generally subjected to catalytic reforming to at least partially aromatize the same and increase its octane number. Because a reforming catalyst is generally poisoned by sulfur compounds, the naphtha fraction should also be desulfurized prior to catalytic reforming.

[0006] A hydrodesulfurization process has hitherto been carried out to achieve the above-noted desulfurization in the field of petroleum refining. A hydrodesulfurization process includes contacting a stock oil to be desulfurized with an appropriate catalyst for hydrodesulfurization in a pressurized hydrogen atmosphere at a high temperature.

[0007] Catalysts which are typically used for hydrodesulfurization of heavy petroleum fractions, such as a stock oil for catalytic cracking (e.g., a vacuum gas oil or an atmospheric residual oil) and a stock oil for thermal cracking (e.g., a vacuum residual oil), comprise a group VIII element (e.g., cobalt and nickel) and a group VI element (e.g., chromium, molybdenum and tungsten) supported on an appropriate carrier (e.g., alumina). The hydrodesulfurization process is usually conducted at a temperature of about 300 to about 400°C, a hydrogen partial pressure of about 30 to about 200 kg/cm², and a liquid hourly space velocity (hereinafter abbreviated as LHSV) of about 0.1 to about 10 1/hr.

[0008] Catalysts which are typically used for hydrodesulfurization of naphtha comprise a combination of a group VIII element and a group VI element (e.g., a combination of cobalt and molybdenum) supported on an appropriate carrier (e.g., alumina). The hydrodesulfurization process is usually carried out at a temperature of about 280 to about 350°C, a hydrogen partial pressure of about 15 to about 40 kg/cm², and an LHSV of about 2 to about 8 1/hr.

[0009] In the case of hydrodesulfurization of a heavy petroleum fraction such as a vacuum gas oil or an atmospheric residual oil, which is a stock oil for catalytic cracking, processing is carried out at high temperature and high pressure as described above. Consequently, strict conditions are imposed on the apparatus design. Furthermore, an extension of the apparatus to increase its capacity involves high construction costs.

[0010] On the other hand, when catalytically cracked gasoline is hydrodesulfurized under the above-described processing conditions, the olefin components present in the cracked gasoline fraction are hydrogenated to reduce the olefin content, and the resulting cracked gasoline fraction has a reduced octane number. Therefore, the cracked gasoline fraction following hydrodesulfurization is desirably subjected to catalytic reforming, isomerization, etc. so as to increase the octane number. That is, two processes are involved. The technique disclosed in the unexamined published Japanese patent application No. Hei. 6-509830 based on a PCT application is an example of such a two process system.

[0011] FR-A-2 476 118 relates to a process for lowering the sulfur content (or the content of sulfur compounds) in the effluent of catalytic cracking without reducing the amount of effluent obtained. The process involves the steps of:

• fractionating said effluent into one low boiling fraction (boiling temperature between 75°C and 185°C) and one high boiling fraction (mainly boiling above 185°C) ;
• hydrodesulfurizing the high boiling fraction in the presence of the catalyst, and
• recombining the product thereof with the low boiling fraction.

[0012] DE-A-1 030 952 discloses a process for improving the octane number of catalytically cracked gasoline. It comprises

• separating the following four fractions

  (i) a fraction boiling below 18°C;

  (ii) a pentane fraction boiling between 18°C and 46°C;

  (iii)a fraction boiling between 46°C and 120°C; and

  (iv) a fourth fraction boiling above 120°C;

• hydrogenating the olefinic double bonds contained in the second fraction to a degree of 30-100°C;
• hydrofining the fourth fraction to reduce the bromine number; and
• mixing the third fraction with the second and fourth fractions as treated.

[0013] Both documents do not teach determining the distribution of sulfur compounds by analysis in the catalytically cracked gasoline fractions after the separation step.

SUMMARY OF THE INVENTION

[0014] An object of the present invention is to provide a process for effectively hydrodesulfurizing catalytically cracked gasoline containing sulfur compounds and olefin components while minimizing the reduction of olefin components.

[0015] In order to solve the above-described problem, the present inventors sought to develop a hydrodesulfurization process for removing sulfur compounds to a permissible level while minimizing reduction in the content of olefin components. As a result, the present inventors found that various sulfur compounds contained in catalytically cracked gasoline are not equally hydrodesulfurized, and the ease or difficulty in desulfurization varies depending on the molecular structure of the sulfur compounds.

[0016] In view of the difference in the relative ease or difficulty in desulfurization among sulfur compounds, the present inventors have discovered a process for hydrodesulfurizing catalytically cracked gasoline containing sulfur compounds and olefin components, which comprises the steps of

• separating the catalytically cracked gasoline into a plurality of fractions including at least one of

  (i) a first fraction rich in sulfur compounds which are hard to desulfurize, selected from:
     thiophene and alkylthiophene, and

  (ii) a second fraction rich in sulfur compounds which are easy to desulfurize, selected from:
     thiacyclopentane, alkylthiacyclopentane,
     benzothiophene and alkylbenzothiophene,

• next hydrodesulfurizing at least one of the first and second fractions in the presence of a catalyst, and, then
• mixing hydrodesulfurized fraction(s) with the remaining fractions.

[0017] That is, the present invention relates to a process for desulfurizing catalytically cracked gasoline comprising separating the catalytically cracked gasoline into at least one of a fraction that has a high content of a single or a plurality of sulfur compounds that are difficult to desulfurize and a fraction that has a high content of a single or a plurality of sulfur compounds that are easy to desulfurize, subjecting at least one of the fractions to hydrodesulfurization under optimum conditions, and mixing the fractions.

DETAILED DESCRIPTION OF THE INVENTION

[0018] The catalytically cracked gasoline for use in the present invention is a gasoline fraction distilled at a temperature of from about 30 to about 250°C. The catalytically cracked gasoline is obtained by catalytically cracking a heavy petroleum fraction (e.g., a vacuum gas oil or an atmospheric residual oil) to mostly convert the heavy petroleum fraction into a broad range of petroleum fractions, and recovering and distilling the catalytically cracked products. The catalytically cracked gasoline is often separated into a light fraction and a heavy fraction which are used depending on the intended application as a gasoline base. The boiling point of the light fraction is from 30 to 180°C, and that of the heavy fraction is from 80 to 250°C.

[0019] These catalytically cracked gasoline fractions contain 10 to 1000 ppm of sulfur compounds, such as thiophene, alkylthiophenes, benzothiophene, alkylbenzothiophenes, thiacyclopentane, alkylthiacyclopentanes, mercaptanes and sulfides. Catalytically cracked gasoline which has been subjected to sweetening also contains disulfides. These sulfur compounds can be analyzed and quantified by a GC-AED (a gas chromatography with an atomic emission detector).

[0020] Of these sulfur compounds, thiophene and alkylthiophenes are compounds that are difficult to desulfurize. Alkylthiophenes are more difficult to desulfurize than thiophene. The alkylthiophenes become more difficult to desulfurize with an increase in the number of constituent alkyl groups. The present invention is characterized in that one or more sulfur compounds which are difficult to desulfurize are identified as such, and one or more fractions having a high concentration of sulfur compounds that are hard to desulfurize are handled separately from other fractions.

[0021] On the other hand, benzothiophene, alkylbenzothiophenes, thiacyclopentane, and alkylthiacyclopentanes, among the above-described sulfur compounds, are examples of sulfur compounds that are easy to desulfurize. Of these, benzothiophene is the easiest to desulfurize. The alkylbenzothiophenes become more difficult to desulfurize with an increase in the number of constituent alkyl groups.

[0022] Separating the catalytically cracked gasoline into a fraction that is rich in sulfur compounds that are hard to desulfurize and into a fraction that is rich in sulfur compounds that are easy to desulfurize may be accomplished by any of distillation, adsorption or crystallization, for example. Distilling is the most convenient of these methods.

[0023] The boiling points of typical sulfur compounds that are hard to desulfurize are as follows. Thiophene: 84.16°C; 2-methylthiophene: 112.56°C; 3-methylthiophene: 115.44°C; 2-ethylthiophene: 134.00°C; 3-ethylthiophene: 136.00°C; 2,5-dimethylthiophene: 136.70°C; 2,4-dimethylthiophene: 140.70°C; 2,3-dimethylthiophene: 141.60°C; 3,4-dimethylthiophene: 145.00°C; 2-isopropylthiophene: 153.00°C; 3-isopropylthiophene: 157.00°C; 3-ethyl-2-methylthiophene: 157.00°C; 5-ethyl-2-methylthiophene: 160.10°C; 2,3,5-trimethylthiophene: 164.50°C; and 2,3,4-trimethylthiophene: 172.70°C.

[0024] The boiling points of typical sulfur compounds that are easy to desulfurize are as follows. Thiacyclopentane: 121.12°C; 2-methylthiacyclopentane: 133.23°C; 3-methylthiacyclopentane: 138.64°C; 2,trans-5-dimethylthiacyclopentane: 142.00°C; 2,cis-5-dimethylthiacyclopentane: 142.28°C; 3,3-dimethylthiacyclopentane: 145.00°C; 2,3-dimethylthiacyclopentane: 148.00°C; 3-ethylthiacyclopentane: 165.00°C; benzothiophene: 219.90°C; methylbenzothiophene: 243.90°C.

[0025] Thus, some of the sulfur compounds that are hard to desulfurize and some of the sulfur compounds that are easy to desulfurize have boiling points that are close together. Accordingly, it is necessary to first determine the distribution of sulfur compounds by analysis, and to then select a distillation apparatus and distillation conditions that would provide the greatest degree of separation possible. After separation, the fraction that is rich in sulfur compounds that are hard to desulfurize desirably contains sulfur compounds that are hard to desulfurize in an amount of more than 50 mol%, preferably at least 60 mol%, of the total sulfur compound content. Likewise, the fraction that is rich in sulfur compounds that are easy to desulfurize desirably contains sulfur compounds that are easy to desulfurize in an amount of more than 50 mol%, preferably at least 60 mol%, of the total sulfur compound content. To separate a sample containing both sulfur compounds that are hard to desulfurize and sulfur compounds that are easy to desulfurize having close boiling points, a multi-stage distillation apparatus is preferred to a single distillation apparatus for carrying out separation and concentration at increased efficiency.

[0026] The method used for desulfurizing a fraction that is rich in sulfur compounds that are hard to desulfurize and a fraction that is rich in sulfur compounds that are easy to desulfurize is selected according to the intended purpose.

[0027] The language "rich in sulfur compounds that are hard to desulfurize" might be defined as a fraction containing sulfur compounds that are hard to desulfurize in an amount of more than 50 mol%, preferably at least 60 mol%, of the total content of sulfur compounds contained in the fraction.

[0028] The language "rich in sulfur compounds that are easy to desulfurize" might be defined as a fraction containing sulfur compounds that are easy to desulfurize in an amount of more than 50 mol%, preferably at least 60 mol%, of the total content of sulfur compounds contained in the fraction.

[0029] For example, where the sulfur content is to be reduced to a limited extent, only a fraction that is rich in sulfur compounds that are easy to desulfurize is subjected to hydrodesulfurization under mild conditions, for example, in the presence of a catalyst for hydrodesulfurization at a temperature of 200 to 300°C, a hydrogen partial pressure of 5 to 20 kg/cm², and an LHSV of 4 to 20 1/hr.

[0030] Hydrodesulfurization of the fraction that is rich in sulfur compounds that are easy to desulfurize can be performed while retaining the olefin components that are originally present in the fraction. More particularly, if proper reaction conditions are selected, a desulfurization rate as high as 70% or even more can be achieved while controlling hydrogenation of the olefins to 10% by volume or lower, thus minimizing a reduction in octane number.

[0031] It is necessary to select the conditions of hydrodesulfurization for each fraction, taking into consideration the kinds and amounts of sulfur compounds contained therein and the kinds and amounts of olefin components concurrently contained therein, in order to achieve the desired desulfurization rate and a permissible reduction in octane number.

[0032] The reaction conditions of hydrodesulfurization are selected from a temperature range of from 200 to 350°C, a hydrogen partial pressure range of from 5 to 30 kg/cm², an LHSV range of from 1 to 20 1/hr, and a hydrogen/oil ratio range of from 300 to 5000 scf/bbl. The lower the temperature or pressure, or the higher the hydrogen/oil ratio, the more effectively olefin hydrogenation can be suppressed to minimize a reduction in octane number.

[0033] On the other hand, where a high overall rate of desulfurization is required, both a fraction that is rich in sulfur compounds that are hard to desulfurize and a fraction that is rich in sulfur compounds that are easy to desulfurize are subjected to hydrodesulfurization. In this case, the conditions of hydrodesulfurization are optimized for each fraction to achieve the desired high rate of desulfurization while controlling hydrogenation of olefins to minimize a reduction in octane number.

[0034] The catalyst for use in the present invention includes those ordinarily used for hydrodesulfurization in the field of petroleum refining. That is, the catalyst generally comprises a desulfurization active metal supported on a porous inorganic oxide carrier.

[0035] The porous inorganic oxide carrier includes alumina, silica, titania, magnesia and mixtures thereof. Alumina and silica-alumina are preferred.

[0036] The desulfurization active metal includes chromium, molybdenum, tungsten, cobalt, nickel and mixtures thereof. Cobalt-molybdenum and nickel-cobalt-molybdenum are preferred. These metals can have the form of a metal, an oxide, a sulfide or a mixed form thereof on the carrier. The active metal can be supported on the carrier by a known method, such as impregnation or co-precipitation.

[0037] In the present invention, a catalyst comprising cobalt-molybdenum or nickel-cobalt-molybdenum supported on an alumina carrier is preferred. The amount of the active metal supported on the oxide carrier is preferably 1 to 30% by weight, more preferably 3 to 20% by weight, in terms of the oxide of the active metal. The metals may be preliminarily converted to sulfides in a known manner before use in hydrogenation.

[0038] The reaction tower for hydrogenation may be of a fixed bed type, a fluidized bed type or a boiling bed type. A fixed bed type reactor is preferred. The catalytically cracked gasoline fraction can be contacted with the catalyst in any of a parallel upward flow system, a parallel downward flow system or a countercurrent flow system. These operations are well known in the field of petroleum refining, and known techniques can be selected as appropriate.

EXAMPLES

[0039] The present invention will now be illustrated in greater detail by way of the following Examples. However, the present invention should not construed as being limited to those Examples.

COMPARATIVE EXAMPLE 1

[0040] A catalytically cracked gasoline light fraction (a 30 to 80°C fraction) was obtained by catalytically cracking a stock oil containing an atmospheric residual oil. The term "a 30 to 80°C fraction" as used herein is a nominal designation. This fraction actually contained 11.9% by weight of a fraction having a boiling point of 30°C or lower and 3.2% by weight of a fraction having a boiling point exceeding 80°C (hereinafter referred to as an 80+°C cut) as shown in Table 1 below. The a 30 to 80°C fraction had a density of 0.675 g/cm³ at 15°C, a sulfur content of 27 ppm, an olefin content of 65% by volume, and a research method octane number of 93.8.

[0041] A commercially available catalyst comprising an alumina carrier having supported thereon 5% by weight of CoO and 17% by weight of MoO₃ was used for hydrodesulfurization after it was preliminarily converted to a sulfide form in a usual manner. The above-described catalytically cracked gasoline fraction was hydrodesulfurized using a fixed bed parallel downward flow type hydrogenation reaction apparatus under relatively mild conditions, i.e., at a reaction temperature of 250°C, a partial hydrogen pressure of 10 kg/cm², an LHSV of 5 1/hr, and a hydrogen/oil ratio of 1000 scf/bbl.

[0042] As a result, a hydrodesulfurized catalytically cracked gasoline light fraction was obtained having a sulfur content of 12 ppm, an olefin content of 44% by volume, and a research method octane number of 86.1. There was no loss of liquid components due to the treatment.

EXAMPLE 1

[0043] The same catalytically cracked gasoline as used in Comparative Example 1 was distilled to divide the same into 7 cuts each by a difference in distillation temperature of 10°C. The yield, sulfur content and olefin content of each cut are shown in Table 1 below.

TABLE 1

Distillation Temperature (°C)	Yield (wt%)	Sulfur Content (ppm)	Olefin Content (vol%)
I.B.P. to 30	11.9	0	82
30 to 40	36.0	1	73
40 to 50	1.9	7	84
50 to 60	7.7	3	42
60 to 70	28.3	24	55
70 to 80	11.0	129	62
80+	3.2	154	51
total	100.0	27	65

[0044] On analysis of the sulfur content of the 70 to 80°C cut, it was found that 90 mol% of the sulfur content was thiophene, a sulfur compound that is hard to desulfurize. Analysis of the sulfur content of the 80+°C cut revealed that 94 mol% of the sulfur content also was thiophene. The 70 to 80°C cut and 80+°C cut which were rich in sulfur compounds that are hard to desulfurize were mixed together and hydrodesulfurized using the same reaction apparatus and the same catalyst as used in Comparative Example 1 at a temperature of 300°C, a hydrogen partial pressure of 30 kg/cm², an LHSV of 5 1/hr, and a hydrogen/oil ratio of 1000 scf/bbl.

[0045] The mixture of the 70 to 80°C cut and the 80+°C cut had a sulfur content of 145 ppm and an olefin content of 59% by volume. The hydrodesulfurization treatment reduced the sulfur content and the olefin content to 3 ppm and 5% by volume, respectively. The treated oil was added to the remaining cuts to obtain catalytically cracked gasoline having a sulfur content of 8 ppm, an olefin content of 62% by volume, and a research method octane number of 91.8. There was no loss of liquid components due to the treatment.

EXAMPLE 2

[0046] The same catalytically cracked gasoline as used in Comparative Example 1 was distilled into 7 cuts each by a difference in distillation temperature of 10°C in the same manner as in Example 1. The 70 to 80°C cut and the 80+°C cut rich in sulfur compounds that are hard to desulfurize were mixed and treated under the same conditions as in Example 1.

[0047] Separately, as a result of analysis, 95 mol% of the sulfur content of the 60 to 70°C cut was found to be n-propylmercaptane. The 60 to 70°C cut was hydrodesulfurized using the same apparatus and catalyst as used in Comparative Example 1 at a reaction temperature of 250°C, a hydrogen partial pressure of 5 kg/cm², an LHSV of 5 1/hr, and a hydrogen/oil ratio of 1000 scf/bbl.

[0048] The sulfur content and the olefin content of the 60 to 70°C cut were 24 ppm and 55% by volume, respectively, while those of the hydrodesulfurized oil were 5 ppm and 41% by volume, respectively.

[0049] The treated oil of the mixture of the 70 to 80°C cut and the 80+°C cut and the treated oil of the 60 to 70°C cut were added to the remaining cuts to obtain catalytically cracked gasoline having a sulfur content of 3 ppm, an olefin content of 57% by volume, and a research method octane number of 89.5. There was no loss of liquid components due to the treatment.

COMPARATIVE EXAMPLE 2

[0050] A catalytically cracked gasoline whole fraction (about a 30 to 210°C fraction) obtained by catalytically cracking stock oil containing an atmospheric residual oil was used as a catalytically cracked gasoline. The term "about a 30 to 210°C fraction" as used herein is a nominal designation. This fraction actually contained 4.9% by weight of a fraction having a boiling point of 30°C or lower and 1.5% by weight of a fraction having a boiling point exceeding 210°C (hereinafter referred to as 210+°C cut) as shown in Table 2 below. The whole fraction had a density of 0.731 g/cm³ at 15°C, a sulfur content of 92 ppm, an olefin content of 43% by volume, and a research method octane number of 92.0.

[0051] A commercially available catalyst comprising an alumina carrier having supported thereon 3.8% by weight of CoO and 12.5% by weight of MoO₃ was used for hydrodesulfurization after it was preliminarily converted to a sulfide form in a usual manner. The above-described catalytically cracked gasoline was hydrodesulfurized using the same reaction apparatus as used in Comparative Example 1 under mild conditions, i.e., at a reaction temperature of 240°C, a hydrogen partial pressure of 10 kg/cm², an LHSV of 7 1/hr, and a hydrogen/oil ratio of 1000 scf/bbl.

[0052] As a result, a hydrodesulfurized catalytically cracked gasoline whole fraction was obtained having a sulfur content of 63 ppm, an olefin content of 38% by volume, and a research method octane number of 90.3. There was no loss of liquid components due to the treatment.

COMPARATIVE EXAMPLE 3

[0053] The same catalytically cracked gasoline whole fraction as used in Comparative Example 2 was hydrodesulfurized under more severe conditions than those employed in Comparative Example 2, i.e., at a reaction temperature of 270°C, a hydrogen partial pressure of 10 kg/cm², an LHSV of 5 1/hr, and a hydrogen/oil ratio of 1000 scf/bbl. The apparatus and catalyst used were the same as those used in Comparative Example 2.

[0054] As a result, a hydrodesulfurized catalytically cracked gasoline whole fraction was obtained having a sulfur content of 27 ppm, an olefin content of 31% by volume and a research method octane number of 87.8. There was no loss of liquid components due to the treatment.

EXAMPLE 3

[0055] The same catalytically cracked gasoline as used in Comparative Example 2 was distilled to obtain 20 divided cuts each different in distillation temperature by 10°C. The yield, sulfur content and olefin content of each cut are shown in Table 2.

[0056] As a result of analysis, it was found that: 85 mol% of the sulfur content of the 120 to 130°C cut was thiacyclopentane, a sulfur compound that is easy to desulfurize; 70 mol% of the sulfur content of the 130 to 140°C cut was C1, C2 thiacyclopentane, sulfur compounds that are easy to desulfurize; and the proportion of benzothiophene, a sulfur compound that is easy to desulfurize, of the sulfur content of the 190 to 200°C cut, 200 to 210°C cut and 210+°C cut was 85 mol%, 95 mol%, and 73 mol%, respectively.

TABLE 2

Distillation Temperature (°C)	Yield (wt%)	Sulfur Content (ppm)	Olefin Content (vol%)
I.B.P. to 30	4.9	0	82
30 to 40	14.8	1	73
40 to 50	0.8	7	84
50 to 60	3.2	3	42
60 to 70	11.6	24	55
70 to 80	4.5	130	60
80 to 90	2.3	151	51
90 to 100	9.5	14	50
100 to 110	4.2	93	40
110 to 120	5.5	210	32
120 to 130	4.6	60	50
130 to 140	4.2	145	27
140 to 150	7.3	160	23
150 to 160	2.0	123	35
160 to 170	6.1	153	18
170 to 180	3.6	126	17
180 to 190	3.8	185	15
190 to 200	3.0	152	16
200 to 210	2.6	340	13
210+	1.5	324	12
total	100.0	27	65

[0057] The cuts that were rich in sulfur compounds that are easy to desulfurize, i.e., the 120 to 130°C cut, 130 to 140°C cut, 190 to 200°C cut, 200 to 210°C cut, and 210+°C cut were mixed together and subjected to hydrodesulfurization using the same apparatus and catalyst as used in Comparative Example 2 at a reaction temperature of 240°C, a hydrogen partial pressure of 10 kg/cm², an LHSV of 7 1/hr, and a hydrogen/oil ratio of 1000 scf/bbl.

[0058] The mixture of the cuts rich in sulfur compounds that are easy to desulfurize had a sulfur content of 171 ppm and an olefin content of 28% by volume, which were reduced by hydrodesulfurization to 33 ppm and 26% by volume, respectively. The oil thus treated was added to the remaining cuts to obtain catalytically cracked gasoline having a sulfur content of 69 ppm, an olefin content of 42.5% by volume, and a research method octane number of 91.7. There was no loss of liquid components due to the treatment.

EXAMPLE 4

[0059] The same catalytically cracked gasoline as used in Comparative Example 2 was distilled to obtain 20 divided cuts each different in distillation temperature by 10°C in the same manner as in Example 3. A mixture of the cuts rich in sulfur compounds that are easy to desulfurize, i.e., the 120 to 130°C cut, 130 to 140°C cut, 190 to 200°C cut, 200 to 210°C cut, and 210+°C cut, was treated under the same conditions as in Example 3.

[0060] As a result of analysis, it was found that: the proportion of thiophene, a sulfur compound that is hard to desulfurize, of the sulfur content of the 70 to 80°C cut and the 80 to 90°C cut was 85 mol% and 90 mol%, respectively; the proportion of methylthiophene, a sulfur compound that is hard to desulfurize, of the 110 to 120°C cut was 87 mol%; the proportion of dimethylthiophene, a sulfur compound that is hard to desulfurize, of the 140 to 150°C cut was 87 mol%; the total proportion of trimethylthiophene, methylethylthiophene, and propylthiophene, which are sulfur compounds that are hard to desulfurize, of the sulfur content of the 160 to 170°C cut was 69 mol%; and the total proportion of tetramethylthiophene, dimethylethylthiophene, diethylthiophene, and methylpropylthiophene, which are sulfur compounds that are hard to desulfurize, of the sulfur content of the 180 to 190°C cut was 56 mol%.

[0061] Those cuts rich in sulfur compounds that are hard to desulfurize, i.e., the 70 to 80°C cut, 80 to 90°C cut, 110 to 120°C cut, 140 to 150°C cut, 160 to 170°C cut, and 180 to 190°C cut were mixed and hydrodesulfurized using the same apparatus and catalyst as used in Comparative Example 2 at a reaction temperature of 300°C, a hydrogen partial pressure of 30 kg/cm², an LHSV of 5 1/hr, and a hydrogen/oil ratio of 1000 scf/bbl.

[0062] The mixture of the cuts rich in sulfur compounds that are hard to desulfurize had a sulfur content of 166 ppm and an olefin content of 31% by volume, which were reduced to 14 ppm and 4% by volume, respectively, by the hydrodesulfurization treatment. The treated oil was added to the remaining cuts to obtain catalytically cracked gasoline having a sulfur content of 25 ppm, an olefin content of 35% by volume, and a research method octane number of 89.2. There was no loss of liquid components by the treatment.

COMPARATIVE EXAMPLE 4

[0063] A catalytically cracked gasoline whole fraction (about a 30 to 230°C fraction) was obtained by catalytically cracking a stock oil containing an atmospheric residual oil. The whole fraction had a density of 0.748 g/cm³ at 15°C, a sulfur content of 352 ppm, an olefin content of 38% by volume, and a research method octane number of 91.7. The whole fraction was hydrodesulfurized using the same apparatus and catalyst as in Comparative Example 1 at a reaction temperature of 250°C, a hydrogen partial pressure of 10 kg/cm², an LHSV of 7 1/hr, and a hydrogen/oil ratio of 1000 scf/bbl.

[0064] As a result, a hydrodesulfurized catalytically cracked gasoline whole fraction was obtained having a sulfur content of 115 ppm, an olefin content of 33% by volume, and a research method octane number of 89.4. There was no loss of liquid components due to the treatment.

EXAMPLE 5

[0065] The same catalytically cracked gasoline as used in Comparative Example 4 was divided by distillation into a 30 to 100°C cut and a 100 to 230°C cut. The ratio of the 30 to 100°C cut to the whole fraction was 32% by weight, and the 30 to 100°C cut had a sulfur content of 62 ppm and an olefin content of 53% by volume. The ratio of the 100 to 230°C cut to the whole fraction was 68% by weight, and the 100 to 230°C cut had a sulfur content of 488 ppm and an olefin content of 31% by volume. The sulfur content of the 100 to 230°C cut was found by analysis to consist of 28 mol% of benzothiophene, 31 mol% of methylbenzothiophene, 2 mol% of thiacyclopentane, and 3 mol% of methylthiacyclopentane, which are sulfur compounds that are easy to desulfurize, and the balance of thiophene compounds which are sulfur compounds that are hard to desulfurize.

[0066] The 100 to 230°C cut rich in sulfur compounds that are easy to desulfurize was hydrodesulfurized using the same apparatus and catalyst as used in Comparative Example 1 at a reaction temperature of 250°C, a hydrogen partial pressure of 10 kg/cm², an LHSV of 5 1/hr, and a hydrogen/oil ratio of 1000 scf/bbl.

[0067] By carrying out the hydrodesulfurization treatment, the sulfur content and the olefin content were reduced to 135 ppm and 28% by volume, respectively. The treated oil was mixed with the 30 to 100°C cut to obtain catalytically cracked gasoline having a sulfur content of 112 ppm, an olefin content of 36% by volume, and a research method octane number of 90.5. There was no loss of liquid components due to the treatment.

[0068] The catalytic hydrodesulfurization process for treating catalytically cracked gasoline containing sulfur compounds and olefin components according to the present invention is characterized in that the catalytically cracked gasoline is separated into a fraction rich in sulfur compounds that are hard to desulfurize and a fraction rich in sulfur compounds that are easy to desulfurize. One or both of the fractions are subjected to hydrodesulfurization under optimum conditions, and the fractions are then mixed together again. The process of the present invention makes it possible to efficiently desulfurize stock oil while suppressing a reduction in olefin content, to thereby minimize a reduction in octane number.

Claims

1. A process for hydrodesulfurizing catalytically cracked gasoline containing sulfur compounds and olefin components, comprising the steps of

- separating the catalytically cracked gasoline into a plurality of fractions including at least one of

(i) a first fraction rich in sulfur compounds which are hard to desulfurize, selected from:
   thiophene and alkylthiophene, and

(ii) a second fraction rich in sulfur compounds which are easy to desulfurize, selected from:
   thiacyclopentane, alkylthiacyclopentane,
   benzothiophene and alkylbenzothiophene,

- next hydrodesulfurizing at least one of the first and second fractions in the presence of a catalyst, and, then

- mixing the fractions,

2. The process of claim 1, wherein said separating step comprising separating the catalytically cracked gasoline into a plurality of fractions including (i) at least one fraction rich in sulfur compounds that are hard to desulfurize and (ii) at least one fraction rich in sulfur compounds that are easy to desulfurize.

3. The process of claim 1 or 2, wherein said separating step comprises distilling.

4. The process of any one of claims 1 to 3, wherein the only fraction that is subjected to hydrodesulfurization is said second fraction.

5. The process of any one of claims 1 to 4, wherein said hydrodesulfurizing step comprises hydrodesulturizing said second fraction while controlling the degree of hydrogenation of the olefin components contained in said fraction to 10% by volume or lower.

6. The process of any one of claims 1 to 3, wherein the only fraction that is subjected to hydrodesulfurization is said first fraction.

7. The process of any one of claims 1 to 6, wherein said first fraction contains sulfur compounds that are hard to desulfurize in an amount of at least 60 mol% of the total content of sulfur compounds, and the second fraction contains sulfur compounds that are easy to desulfurize in an amount of at least 60 mol% of the total content of sulfur compounds.

8. The process of claim 1, wherein the alkyl group of said ethylthiophene, alkylthiacyclopentane and alkylbenzothiophene is selected from the group consisting of a methyl group, an ethyl group and a propyl group.

9. The process of any one of claims 1 to 3, 6 and 7, wherein said sulfur compounds that are hard to desulturize comprise at least one of thiophene and methylthiophene.

10. The process of any one of claims 1 to 5 and 7, wherein said sulfur compounds that are easy to desulfurize comprise at least one of benzothiophene and methylbenzothiophene.

Ansprüche

1. Verfahren zum Hydroentschwefeln von katalytisch gekracktem Benzin, welches Schwefelverbindungen und Olefinkomponenten enthält, umfassend die Stufen von

- Auftrennen des katalytisch gekrackten Benzins in eine Vielzahl von Fraktionen, enthaltend mindestens eine von

(i) einer ersten Fraktion, die reich ist an Schwefelverbindungen, die schwierig zu entschwefeln sind, ausgewählt aus
   Thiophen und Alkylthiophen, und eine von

(ii) einer zweiten Fraktion, die reich ist an Schwefelverbindungen, die leicht zu entschwefeln sind, ausgewählt aus
   Thiacyclopentan, Alkylthiacyclopentan,
   Benzothiophen und Alkylbenzothiophen,

- als nächstes Hydroentschwefeln von mindestens einer der ersten und zweiten Fraktionen in Gegenwart eines Katalysators, und anschließend

- Mischen der Fraktionen.

2. Verfahren gemäß Anspruch 1, worin die genannte Auftrennungsstufe das Auftrennen des katalytisch gekrackten Benzins in eine Vielzahl von Fraktionen, enthaltend (i) mindestens eine Fraktion, die reich ist an schwierig zu entschwefelnden Schwefelverbindungen, und (ii) mindestens eine Fraktion, die reich ist an leicht zu entschwefelnden Schwefelverbindungen, umfaßt.

3. Verfahren gemäß den Ansprüchen 1 oder 2, worin die genannte Auftrennungsstufe Destillieren umfaßt.

4. Verfahren gemäß jedem der Ansprüche 1 bis 3, worin die einzige Fraktion, die einer Hydroentschwefelung unterworfen wird, die genannte zweite Fraktion ist.

5. Verfahren gemäß jedem der Ansprüche 1 bis 4, worin die genannte Hydroentschwefelungsstufe Hydroentschwefeln der genannten zweiten Fraktion umfaßt, während der Grad der Hydrierung der Olefinkomponenten, die in der genannten Fraktion enthalten sind, auf 10 Vol.% oder weniger geregelt wird.

6. Verfahren gemäß jedem der Ansprüche 1 bis 3, worin die einzige Fraktion, die einer Hydroentschwefelung unterworfen wird, die genannte erste Fraktion ist.

7. Verfahren gemäß jedem der Ansprüche 1 bis 6, worin die genannte erste Fraktion schwierig zu entschwefelnde Schwefelverbindungen in einer Menge von mindestens 60 Mol% des Gesamtgehalts an Schwefelverbindungen enthält, und die zweite Fraktion leicht zu entschwefelnde Schwefelverbindungen in einer Menge von mindestens 60 Mol% des Gesamtgehalts an Schwefelverbindungen enthält.

8. Verfahren gemäß Anspruch 1, worin die Alkylgruppe des genannten Alkylthiophens, Alkylthiacyclopentans und Alkylbenzothiophens aus der Gruppe ausgewählt ist, die aus einer Methylgruppe, einer Ethylgruppe und aus einer Propylgruppe besteht.

9. Verfahren gemäß jedem der Ansprüche 1 bis 3, 6 und 7, worin die genannten schwierig zu entschwefelnden Schwefelverbindungen mindestens eine von Thiophen und Methylthiophen umfassen.

10. Verfahren gemäß jedem der Ansprüche 1 bis 5 und 7, worin die genannten leicht zu entschwefelnden Schwefelverbindungen mindestens eine von Benzothiophen und Methylbenzothiophen umfassen.

Revendications

1. Procédé d'hydrodésulfuration d'essence craquée catalytiquement contenant des composés soufrés et des composants oléfiniques, comprenant les étapes consistant à :

- séparer l'essence craquée catalytiquement en une pluralité de fractions comprenant au moins une de

(i) une première fraction riche en composés soufrés qui sont difficiles à désulfurer, choisis parmi :

le thiophène et un alkylthiophène, et

(ii) une seconde fraction riche en composés soufrés qui sont faciles à désulfurer, choisis parmi :
le thiacyclopentane, un alkylthiacyclopentane, le benzothiophène et un alkylbenzothiophène,

- puis hydrodésulfurer au moins une de la première et de la seconde fractions en présence d'un catalyseur, et, ensuite

- mélanger les fractions.

2. Procédé selon la revendication 1, caractérisé en ce que ladite étape de séparation comprend la séparation de l'essence craquée catalytiquement en une pluralité de fractions comprenant (i) au moins une fraction riche en composés soufrés qui sont difficiles à désulfurer et (ii) au moins une fraction riche en composés soufrés qui sont faciles à désulfurer

3. Procédé selon la revendication 1 ou 2, caractérisé en ce que ladite étape de séparation comprend une distillation.

4. Procédé selon l'une quelconque des revendications 1 à 3, caractérisé en ce que la seule fraction qui est soumise à l'hydrodésulfuration est ladite seconde fraction.

5. Procédé selon l'une quelconque des revendications 1 à 4, caractérisé en ce que ladite étape d' hydrodésulfuration comprend l'hydrodésulfuration de ladite seconde fraction en réglant le degré d'hydrogénation des composants oléfiniques contenus dans ladite fraction à 10% en volume ou moins.

6. Procédé selon l'une quelconque des revendications 1 à 3, caractérisé en ce que la seule fraction qui est soumise à l'hydrodésulfuration est ladite première fraction.

7. Procédé selon l'une quelconque des revendications 1 à 6, caractérisé en ce que ladite première fraction contient des composés soufrés qui sont difficiles à désulfurer en une quantité d'au moins 60% en moles de la teneur totale des composés soufrés, et la seconde fraction contient des composés soufrés qui sont faciles à désulfurer en une quantité d'au moins 60% en moles de la teneur totale des composés soufrés.

8. Procédé selon la revendication 1, caractérisé en ce que le groupe alkyle desdits alkylthiophènes, alkylthiacyclopentanes et alkylbenzothiophènes est choisi dans le groupe constitué par un groupe méthyle, un groupe éthyle et un groupe propyle.

9. Procédé selon l'une quelconque des revendications 1 à 3, 6 et 7, caractérisé en ce que lesdits composés soufrés qui sont difficiles à désulfurer comprennent au moins un du thiophène et du méthylthiophène.

10. Procédé selon l'une quelconque des revendications 1 à 5 et 7, caractérisé en ce que lesdits composés soufrés qui sont faciles à désulfurer comprennent au moins un du benzothiophène et du méthylbenzothiophène.