Title of Invention	A SYSTEM FOR THE PREPARATION OF A HIGH QUALITY GASOLINE THROUGH THE RECOMBINATION OF CATALYTIC HYDROCARBON AND ITS PROCESS
Abstract	This invention relates to a system for the preparation of a high quality gasoline through the recombination of catalytic hydrocarbon and its process. The characteristics are as follows: the upper part of the fractionator is connected with light petrol hydrogenation unit through th5 e light petrol pipeline. The lower part of the fractionator is connected with the extractor through the heavy petrol pipeline. The upper part of the extractor directly extracts the product through the pipeline and the lower part of the extractor is connected to the light petrol pipeline behind the light petrol hydrogenation unit. Compared with the prior art, this invention has the following advantages: the volume of used catalyst is greatly reduced. In addition, the sulfur reduction and olefin reduction effect are remarkable by using the hydrogenation units with special catalysts and parameters regarding different petrol fractions. Figure 1 is the representative figure.

Title of Invention

A SYSTEM FOR THE PREPARATION OF A HIGH QUALITY GASOLINE THROUGH THE RECOMBINATION OF CATALYTIC HYDROCARBON AND ITS PROCESS

Abstract

This invention relates to a system for the preparation of a high quality gasoline through the recombination of catalytic hydrocarbon and its process. The characteristics are as follows: the upper part of the fractionator is connected with light petrol hydrogenation unit through th5 e light petrol pipeline. The lower part of the fractionator is connected with the extractor through the heavy petrol pipeline. The upper part of the extractor directly extracts the product through the pipeline and the lower part of the extractor is connected to the light petrol pipeline behind the light petrol hydrogenation unit. Compared with the prior art, this invention has the following advantages: the volume of used catalyst is greatly reduced. In addition, the sulfur reduction and olefin reduction effect are remarkable by using the hydrogenation units with special catalysts and parameters regarding different petrol fractions. Figure 1 is the representative figure.

Full Text	FORM 2 THE PATENTS ACT, 1970 (39 of 1970) & The Patent Rules, 2003 COMPLETE SPECIFICATION 1. TITLE OF THE INVENTION: A SYSTEM FOR THE PREPARATION OF A HIGH QUALITY GASOLINE THROUGH THE RECOMBINATION OF CATALYTIC HYDROCARBON AND ITS PROCESS 2. APPLICANT: Name: DING, Ranfeng Nationality: A Chinese National Address: B-1805, Jinma Building, No.38, Xueqing Road, Haidian District, Beijing, China . 3. PREAMBLE TO THE DESCRIPTION: The following specification particularly describes the invention and the manner in which it is to be performed: Field of the invention This invention relates to a system for the preparation of a high quality gasoline and its process. and more particularly to a system for the preparation of a high quality gasoline through the recombination of catalytic hydrocarbon and its process. BACKGROUND OF THE INVENTION Catalvtie cracking, catalytic schizolvsis and heavy oil catalytic schizolysis technology is the key technology of Lhe oil refining, catalytic schizolysis is classified into the catalytic schizolysis of wax oil and the catalytic schizolysis of heavy oil, The generated oils produced from these processes are collectively called catalytic hydrocarbons. Through the processing & handling, generally fractionation with fractionation fractionator. the obtained catalytic hydrocarbons can be fractionated into the products such as dry petroleum gas liquefied petroleum gas, gasoline, dicscl oil and heavy oil etc. Among them, the gasoline and diesel oil occupy above 70% of the supply volume of the gasoline and diesel oil in the market, As the environmental protection requirements become more and more strict, the standard of gasoline & diesel oil will be increased continuously, The current processing method wherein The catalytic hydrocarbons go throught tractionator has the following shortcomings the first is That the quality of the produced gasoline and diesel oil should be improved, the alkene content, is too high, octane value (RON) is too low, the octane number of the diesel oil is, too low, the stability does not conform to the requirements. The second is that the above processing method can not produce multiple grades of gasoline simultaneously in addition, there is only one product type The third is that the proportion between produced gasoline and diesel oil docs not conform to the market need, the diesel oil can not satisfy the need, whereas Lhe gasoline is in oversupply status. In order to solve the above problem, Chinese patent with patent N=03148181.7 namely trealmenl method of catalyzing the hydrocarbon recombination" has provided a type of treatment method of catalyzing the hydrocarbon recombination, furthermore, the Chinese palents with palenL N=200310103541.9 and 2003 10103540.4 have given publicity to the improved patents concerning the water rinsing system and solvent recycling, however, the methods of reducing sulfur and oletin have not been touched upon in these publicized patents. The current GB17930 gasoline standard requires that the sulfur content is below 0-05% (wt), the olefin content is below 35%(v) and the benzend content is below 2.5%(v). Most of the refineries can assure the quality of the gasoline, However, the National Gasoline Standard III that will be implemented in 2010 requires the following: the sulfur content is below 0.015% (wt), the olefin content is below 25%(v) or even lower and the benzene content is below l%(v). For must of the refineries, they must be confronted with the requirements of higher standard, i.e., the National Gasoline Standard IV: the sulfur content is below 0.005% (wt), the olefin content is below 25%(v) or even lower, Gasoline quality solution must consider the transition from National Gasoline Standard III to National Gasoline Standard IV. The better planning is to follow National Gasoline Standard IV in single step. Since the proportions of blended components in the gasoline products of our country differ greatly with those of the developed countries, the catalytic cracking gasoline (hereafter called catalytic gasoline) occupies a high proportion while reformed gasoline and gasoline alkyl ate only occupies a little proportion, Furthermore. this condition will exist for a long time, Therefore, the method of reducing sulfur and olefin mainly touches upon the problem of catalyzed gasoline, it is generally acknowledged that 5-10% of the general sulfur in the catalytic cracking material will enter the gasoline fraction. According to the eharacterislics of the refineries in our country that catalytic material hydrogenation purification capability is low, secondary processing catalytic cracking capability is high and there is residual oil coking, the sulfur content of the catalytic gasoline in the refinery processing the crude oil with low sulfur content (sulfur content 0.3%) is about 200ppm. if the crude oil with sulfur content of 0 8%, the sulfur content of the catalytic gasoline is about 900ppm. Therefore, the difficult point in the upgrade of gasoline quality has changed from the problem of olefin to the problem of sulfur, It is impossible lo radically solve the problem of sulfur through the improvement of catalytic cracking process or catalyst The catalytic cracking material hydrogenation and desulfurization cannot be applied in large scale due lo big investment, high operation cost and current condition in the refineries, Furthermore, it is inapplicable lo the refineries processing rude oil with low sulfur content. In the meantime, the catalytic cracking equipment excessively reduces the olefine therefore, it will aggravate the loss of benzoline and the octane number (RON) of the gasoline, Therefore, it is a technical problem that how to provide a system for blended gasoline having low sulfur content, low olefin contenl and high octane number (RON) with low cost. Summary of the invention One of the object of the invention is to provide a gasoline catalytic hydrocarbon recombination system having low salfur content, low olefin conlenl and high octane number (RON ) with low cost is provided. In order to realize the shove purpose, this invention adopts the following technical resolution: A system for the preparation of a high quality gasoline through the recombination of catalytic hydrocarbon, including fractionator, wherein the upper part of the said fractionator is connected with light petrol hydrogenation equipment through the light petrol pipeline. The lower part of the said fractionator is connected with the extractor through the heavy petrol pipeline. The upper part of the said extractor directly extracts the product through the pipeline and the lower part of the said extractor is counseled to the light pelrol pipeline behind the light pelrol hydrogenalion unit. A preferred system, wherein the lower part of the said fraetionator is connceeted with the heavy petrol hydrogenation unit through heavy petrol pipeline, the said heavy petrol hydrogenation unit is then connected to the extractor through the pipeline. A preferred system, wherein the lower part of the said extractor is connected with the aromatic hydrocarbon hydrogenation unit through the pipeline, the said aromatic hydrocarbon hydrogenation unit is then connected to the light petrol hydrogenstion unit through the pipeline, Another object of the invention is to provide the process of said high quality gasoline preparation through catalytic hydrocarbon recombination, The technical resolution as follows: A process for the preparation of a high quality gasoline through catalytic hydrocarbon recombination, wherein lhe stabilized gasoline is put into the fractionator to carry out the distilling and fractionaize into the light petrol and heavy pelrol, The above light pelrol enters the light petrol hydrogenation unit to carry out the hydrogenation. The above heavy petrol is extracted in the extractor and separate inlo aromatic hydrocarbon and rallinate oil, the above aromatic hydrocarbon is blended with the light petrol after the hydrogenation treatment through the pipeline and the shove raffinatcoil will he directly extracted as chemical light oil. A preferred process, wherein hydration treatment is first carried out in the heavy petrol hydration unil to the said heavy petrol before the extraction is earned out in the extractor. A preferred process, wherein first hydration treatment is carried out to the above aromatic hydrocarbon, then it is blended with and used together with the light petrol after the hydration treatment through the pipeline. A preferred process, wherein the fractionator overhead temperature of the above fractionator is 100-110oC, the fractionator bottom temperature is 206-226oC, the fractionator overhead pressure of the above fractionator is 0.11-0.28MPa(absolute pressure), the fractionator bottom pressure is 0.12-0.30MPa(absolute pressure), the distillation range of the above light petrol is controlled to 30oC-100oC and the distillation range of the above heavy gasoline is controlled to 100°C-205oC. A preferred process, wherein The fractionator overhead Temperature of the above tractionator is 105oC, the fractions tor bottom temperature is 216oC. the fractionator overhead pressure of the above fractionator is 0.11-0.28MPa(absolute pressure), the fractionator bottom pressure is 0.12-0,30MPa(absolute pressure), the distillation range of the above light petrol is controlled to 30oC- 100oC and the distillation range of the above heavy gasoline is controlled to 100o C -205oC. A preferred process, wherein the catalyst of the above light petrol hydrogenation unit is selective hydro genation catalyst GHT-20. the volume airspeed ratio of the above light petrol hydrogenation unit is 2-4, hydrogen/oil volume ratio is 250-350, the operature is 240~260oC the operation pressure is 1.4-1.6MPa (absolute pressure). A preferred process, wherein the physical and chemical characteristics of the catalyst of the said light petrol hydrogenalion unit. i.e.. selective hydrogenalion catalyst GHT-20 are as shown in the following table: Name of the index Unit GHT-20 Appearance Grey three-leaf type Specification mm ф1.5-2.0 Intensity N/cm 170 Bulk density g/ml 0.70 Specific surface m2/g 180 Pore volume ml/g 0.5-0.6 wo3 m% 6.6 NiO m% 2.1 CoO m% 0.16 A preferred process, wherein the catalyst of the said heavy gasoline hydrogenalion unit is full hydrogenation catalyst, GHT-22. the volume airspeed ratio of the said heavy gasoline hydrogenalion unit is 2-4, hydrogen/oil volume ratio is 250-350. the operation temperature is 290~330oC, the operation pressure is 1.2~3MPa (absolute pressure). A preferred process, wherein the physical and chemical characteristics of the said heavy gasoline hydrogenalion unit GHT-22 are as shown in the following table: Name of the index Unit GHT-22 Appearance Grey three-leaf type Specification mm ф1.5-2.0 Intensity N/cm 180 Bulk densily g/ml 0.73 Specific surface m /g 180 Pore volume ml/g 0.5-0.6 W03 m% 15 NiO m% 1.7 CoO m% 0,15 Na2O m% Fe2O3 m% Si02 m% Carrier m% 824 A preferred process, wherein the catalyst of the above aromatic hydrocarbon hydrogenation unit is full hydrogenation catalyst GHT 22, the volume airspeed ratio of the said aromatic hydrocarbon hydrogenation unit is 2-3, hydrogen/oil volume ratio is 250-300, Lhe operation temperature is 285-352oC the operation pressure is 1.5-2.5 MPa (absolute pressure). A preferred prosscess wherein the physical and chemical characteristics of thee catalyst of the said aromatic hydrocarbon hydrogenation unit, i.e.. full hydrogenation catalyst GHT-22 are as shown in the following table: Name of the index Unit GHT-22 Appearance Grey three-leat type Specifics Lion mm ф 1.5-2.0 Intensity N/cm 180 Bulk density g/ml 0,73 Specific surface m2/g 180 Pore volume ml/g 0.5 0.6 wo3 m% 15 NiO m% 1.7 CoO m% 0.15 Na2O m% Fe2O3 m% SiO2 m% Carrier m.% 82/1 The fartionator used in this invention is the fractionator disclosed in the China patent 0314S181.7 namely 'catalytic hydrocarbon recombination treatment method". the said extractor uses the estractor disclosed in the China patebts 200310103541,9 and 200310103540.4. induding solvent recycling and water rinsing system, the hydrogenation unit used in this invention is the current hydrogenation unit including healing furnace, heal exchanger, high-presure separator, air condenser and wafer condenser etc. Brief description of the description of the drawing In the following, we will further explain this invention through attached drawings and embodiments, but this does not mean the limitation to this invention. Figure 1 is lhe schematic flow sheet of embodiment 1, Figure 2 is lhe schematic flow sheet of embodiment 2 and 3, Figure 3 is the schematic flow sheet, of embodiment. 4 and 5. Detailed description of the preferred Embodiment Embodiment 1 See figure 1. it is the schematic flow sheet of this embodiment. The gasoline is fractionated at fractionator 1 with the flow rate of 100,000 ton/year to the stabilized agsolinot catalytic gasoline) wherein the distilling range is 30-205oC. sulfur content is 85ppm. mercaptan content is 15ppm, olefin content is 25%(v), diolefin content is 0.1%(v), aromatic hydrocarbon content is 13%(v), octane number (RON) is 87, density is 728 kg/m3 the overhead temperature of the fractionator 1 is 105oC. the fractionator bottom temperature is 216oC, fractionator overhead pressure is 0.2MPa(absolute pressure), fractionator bottom pressure is 0.25MPa(absolute pressure), light petrol and heavy petrol can be separately obtained. The above light petrol(di tilling range 30-100°C) is vaporized through the overhead of fractionator 1, the total vaporization volume is 50,000 tons/year, then it enters the light petrol hydrogenalion apparatus 3 to carry out hydrogenalion treatement. The catalyst of the above light petrol hydrogenation apparatus 3 is selective hydrogenation catalyst GHT-20,The volume airspeed ratio of the above light petrol hydrogenation unit 3 is 4. hydrogen/oil volume ratio it 300. [he operation temperature is 250oC, the operation pressure is 1.5MPa (absolute pressure) (selective hydrogenation) . The above heavy petrol (distilling range is 100-205oC) enters the heavy petrol extractor 2 for solvent extraction with the flow rale of 50000 tons/year and aromatic hydrocarbon and raffinate oil are separated out The solvent used in the above extractor 2 is sulfolane, the extraction tempera lure is 120 C. the ratio of solvent (sol vent/feed material lis 4.0, the rinsing ratio of the raffinate oil is 0.2(mass), the recovered temperature of the solvent is 175oC, the recovered pressure of the solvent is 0.065MPa(absolute pressure), Lhe above aromatic hydrocarbon is blended with Lhe hydrogen tiled light petrol with the flow rale of 11000 tons/year, the above raffinate oil is extracted out as the chemical light petrol with the flow rale of 39000 tons/year, The distilling range of lhe obtained blended petrol is 30-205 oC. the sulfur content is 102.8ppm, the mercaptan content is 4 3ppm, the olefin content is 17.9%(v), the diolefin content is 0,05%(v),the aromatic hydrocarbon content is 20.0%(v), the octane number(RON) is 91,8, the density is 700.6kg/m3, the oil produced is 39000 tons/year. The distilling range of the obtained chemical light petrol is 100-205°C, the sulfur content is 29.0ppm, the mercaptan content is 1.0ppm, the olefin content is 28.2%(v). the diolcfin content is 0.01% (v), the aromatic hydrocarbon content is 3.0%(v), the octane number(RON) is 78.5, the density is 775.5kg/m3, the oil produced is 39,000 lons/year, The physical and chemical characteristics of the selective hydrogenation catalyst GHT-20 are as shown in the following table: Name of the index Unit GHT-20 Appearance Grey three-leaf type Specification m m ф 1.7 Intensity N/cm 170 Hulk density G/ml 0.70 Specific surface M2/g 180 Pare volume ml/g 0.55 WO3 NiO M% 6.6 2.1 CoO M% 0.16 The measuring methods used in this invention arc as follows: 1. Distilling range: G B/T6536-1997 petroleum products-determination of distillation 2. Sulfur content: SH/T0689-2000 light hydrocarbon & engine fuel and other petroleum products-determination of total sulfur contend ultra-luminescence method) 3. Mercaplan sulfur: GB/T1792-1988 Distillate fuck-Determination of mercaptan sulphur--Potenliametric titration method. 4. Olcfin; GB/T 11132-2002 Liquid petroleum products-Determination of hydrocarbon types -Fluorescent indicator absorption method 5. Aromatic hydrocarbon: GB/TI1132-2002 Liquid petroleum products-Determination of hydrocarbon types-Fluorescent indicator absorption method 6, Octane number GB/T5487 gasoline-testing menthods for octane number -research method 7, Density; GB/T18834-2000, method for laboratory measurement of crude oil and liquid petroleum productst densitometer method) 8, Measurement of the diolefin: titration method 9. Hydroge nation catalyse analysis method: Chemical Analytical procedure Applied petrochemical industry component standard NiO Colonmetric analysis SH/T0346-1992 CoO Colori metric analysis SH/T0345-1992 WO3 Colorimetric analysis Physical Analytical procedure Applied instrument characteristics Surface area Low temperature nitrogen adsorption 2-100 model sorption analyzer Pore volume Mercury inrusion method Auto Pore II 9200 Intensity Cold Crushing Strength DI. II type intelligent granular measurement method intensity measuring gauge Bulk density Weighing method Embodiment 2 See figure 2. it is the schematic flow sheet of this embodiment. The gasoline is fractionated at fractionator 1 with the flow rate of 100,000 ton/year in the tractionator 1 to the stabilized gasoline(catalytic gasoline) wherein low sulfur content whose distillinng range is 30-205oC, the sulfur content is 100ppm, the mercaptan content is. 5ppm, the olefin content is 30%(v), the diolcfin content is 0.1%(v), the aromatic hydrocarbon content is 15%(v), the octane number(RON) is 89, density is 728 kg/m3, the fractionator overhead temperature of fraclionalor 1 is 82oC, the fraelionalor bottom temperature is 186oC. fractionator overhead pressure is 0.2MPa(absolute pressure), fraction ator bottom pressure is 0.25MPa(absolute pressure), light petrol and heavy petrol can be separately obtained. The above light pctrol(distilling range 30-80oC) is vaporized through the upper of fraetionator 1, the total vaporization volume is 40,000 tons/year, then it enters the light petrol hydrogenation apparatus 3-1 to carry out hydrogenation treatment The catalyst of the above light petrol hydrogenation apparatus 3-1 is selective hydrogenation catalyst GHT-20.The volume airspeed ratio of the ahove light petrol hydrogenation unit 3 1 is 2, hydrogen/oil volume ratio is 150, the operation temperature is 220oC, the operation pressure is 0.6MPa (absolute pressure). The above heavy petrol(distilling range is 80 205oC) enters the heavy petrol hydrogenation unit 3-2 to carry out hydrogenation treatment with the flow rate of 60000 Lons/year Lhe catalyst of the above heavy petrol hydrogenation apparatus .3 2 is full hydrogenation catalyst GHT 22. The volume airspeed ratio of the above heavy petrol hydrogenation unit 3-2 is 2, hydrogen/oil volume ratio is 250, the operation temperature is 290oC the operation pressure is l.2MPa (absolute pressure). Then it passes through the pipeline into the heavy petrol extraetor 2 LO carry out Lhe extraction separation and the aromatic hydrocarbon & raffinate oil can be separated, The solvent used in extractor 2 is N-pyrrolidone, the extraclion temperature is 115 oC the solvent ratio(solvent/feed material) is 3.5 (mass), the rinsing ratio of the raffinate oil is 0,2(mass), the solvent recovered temperalture is 151 oC the recovery pressure of the solveut is 0.112MPA (absolute pressure). The above aromatic hydrocarbon is blended with the above-hydrogenated light petrol with the flow rate of 15000 tons/year, the above raffimale oil is extracted out with the flow rate of 45000 tons/year as the fine quality ethylene material. The distilling range of the ohtained blended gasoline is 30-205oC. the sulfur content is 5.27ppm, the mereaplan content is lower than lppm, olefin content is 17.8%(v), the diolefin content is 0.01 %(v), the aromatic hydrocarbon content is 25.6%(v), the octane number(RON) is 94.1, the density is 703.8 kg/m3, the extraction volume is 55000 tons/year. The distilling range of the obtained fine quality ethylene material is 80-205oC, the sulfur content is 2.0ppm. the merecaptan content is lower than lppm. olefin content is 0.1%(v), the dioJcfin content is 0.01%(v), the aromatic hydrocarbon content is 3.0%(v), the octane number (RON) is 81 0. the density is 760.0 kg/m3 the extraction volume is 45000 tons/year. The physical and chemical characteristics of the se leetive hydrogenalinn calnlyst GHT-20 are as shown in the- following table: Name of the index Unit GHT-20 Appearance Grey three-leaf type Specification mm 01,7 Intensity N/cm 170 Bulk density g/ml 0.70 Specific suffice m2/g 180 Pore volume ml/g 0.55 WO3 NIO m% m% 6.6 2.1 C0O m% 0.16 The physical and chemical characteristics of the full hydrogenation talalyst GHT-22 are as shown in the following table: Name of the index Unit GHT-22 Appearance Grey three-leat type Specification mm ф1.7 In tensity N/cm 180 Bulk density g/ml 0.7.1 Specific surface m/g 180 Pore volume ml/g 0.57 WO3 m% 15 NiO m% 1.7 CoO m% 0.15 Na2O Fe2O3 m% SiO2 m% Carrier m% 82.4 The measuring methods used in this invention are as follows (same below): 1. Distilling range: GB/T6536-1997 petroleum products -determination of distillation 2. Sulfur content: SH/T0689-2000 light hydrocarbon & engine fuel and other petroleum products-deierminadon of total sulfur contenlfultra-luminescence method) 3. Mercaptan sulfur: GB/T1792-1985 Distillate fuels--Determination of mercaptan sulphur Potentiantptric titration method 4. Olefin: GB/T111.32-2002 Liquid patroleum products-Determination of hydrocarbon types-Fluoresceni indicator absorption method 5. Aramaic hydrocarbon: GB/T11 132-2002 Liquid petroleum products-Determination of hydrocarbon types-Fluorescent indicator absorption method 6. Octane number: GB/T5487 gasoline- testing methods for octane number -research method 7. Density: GB/T1884-2000, method for laboratory measurement of crude oil and liquid petroleum products (densitometer method ) 8. Measurement of the diolefin: titration method 9. Hydrogenation catalyst analysis method: Chemical component. Analytical procedure Applied petrochemical industry standar d NiO Colorimetric analysis SH/T034G-1992 CoO Colorimetric analysis SH/T034-1992 WO3 Colorimetric analysis Physical characteristics Analytical procedure Applied instrument Surface area Low temperature nitrogen adsorption 2400 model sorption analyzer Pore volume Mercury intrusion method Auto Pore II 9200 Intensity Cold Crushing Strength DL II type intelligent granular intensity measurement method measuring gauge Bulk density Weighing method Embodiment 3 As shown in figure 2, it is the schematic flow sheet of this embodiment, The gasoline is fractionated at fractionator 1 with the flow rate of 100.000 ton/year to the stabilized gaiolinc(catalytic gasoline) with high sulfur content whose distilling range is 30-205oC. the sulfur content is 2000ppm, the mercaptan content is 50ppm, the olefin content is 40%(v), the diolefin content is l.0%(v), the aromatic hydrocarbon content is 19%(v), the octane number (RON) is 91 density is 728 kg/m3, the fractionator overhead temperature of fractionator 1 is 86oC, the fractionator bottom temperature is 192oC, fractionator overhead pressure is 0.2MPa(absolute pressure), fractionator bottom pressure is 0.25MPa(absolute pressure), light petrol and heavy petrol can be separately obtained. The above light petrol(distilling range 30-80oC) is vaporized through the upper of fractionalor 1, the total vaporization volume is 43,000 tons/year, then it enters lhe light petrol hydrogenation apparatus 3-1 to tarry out hydrogenation treatment, The catalyst of the above light petrol hydrogenation apparatus 3-1 is selective hydrogenation catalyst GHT-20. The volume airspeed ratio of the above light patrol hydrogenation unit 3-1 is 4, hydrogen/oil volume ratio is 300, the operation temperature is 280°C. the operation pressure is 2.0MPa (absolute pressure). The above heavy petrol(distilling range 90-203 °C) enters heavy petrol hydrogenation unit 3-2 TO carry out hydrogenation treatment with the flow rate of 57000 tons/year, The catalyst of lhe light petrol hydrogenation apparatus 3-2 is selective hydrogenation catalyst GHT-20, lhe volume airspeed ratio af the above light petrol hydrogenation unit 3-2 is 4, hydrogen/oil volume ratio is 350, the operation temperature is 330oC, the operation pressure is 3.0V1Pa (absolute pressure). Then it passcs through the pipeline into the heavy petrol extractor 2 to carry out the extraction separation and the aromatic hydrocarbon & raffinate oil can be separated/The solvent used in extractor 2 is N- pyrrolidine, the extraction temperature is 115 °C, the solvent ratio(solvent/feed material) is 3,5(mass), the rinsing ratio of the raffinate oil is 0.2(mass) the solvent recovered temperature is 151 oC, The recovery pressure of the solvent is 0.112MPa (absolute pressure). The above aromatic hydrocarbon is blended with the above hydrogenated light petrol with the flow rate of 19000 tons/year, the above raffinate oil is extracted out with the flow rate of 38000 as The fine quality ethylene: material. The distilling range of the obtained blended gasoline is 30-205oC the sulfur content is 7.52ppm. the mercaptan content is lower than 1ppm, olefin content is 17.99%(v), the diolefin content is 0.01%(v), the aromatic hydrocarbon content is 29-1 %(v), the octane number(RON) is 95.2, the density is 720.1 kg/m3. the extraction volume is 62000 Lous/year. The distilling range ol the obtained fine quality ethylene material is 00-205oC. the sulfur content is 2.0ppm, the mercaptan content is lower than 1ppm, olefin content is 6%(v), the diolefin content is lower than 0.01%(v), the aromatic hydrocarbon content is 3.0%(v), the octanc number(RON) is 81.5. the density is 740.0 kg/m3, the extraction volume is 38000 tons/year. Embodiment 4 As shown in figure 3, it is the schematic flow sheet of this embodiment. The gasoline is fractionated at fractionator I with the flow rale of 100,000 ton/year lo the stabilized gasolinc(catalytic gasoline) with low sulfur content whose distilling range is 30-205 oC the sulfur content is 100ppm, the mcrcaptan content is 5ppm, the olefin content is 30%(v), the diolefin conlent is 0.1%(v), lhe womatic hydroearbon content is 15%(v). the octane number(RON) is 89, density is 728 kg/m3. the fraelionator overhead temperature of fractionator 1 is 86oC, the fractionator bottorm temperature is 192oC, fractionator overhead pressure is 0.2MPa(absolute pressure), fractionator bottom pressure is 0.25MPa(absolute pressure), light petrol and heavy petrel can be separately obtained, The above light petrol(distilling range 30-80oC) vaporized through the upper of fraetronator 1, then it enters tlte light petrol hydrogenation apparatus 3-1 to carry out hydrogention treatment, the total vaporization volume after the hydrogcnation is 40.000 tons/year. The catalyst of the above light petrol hydrogenation apparatus 3-1 is selective hydrogenation catalyst GHT-20. tlte volume airspeed ratio of the above light petrol hydrogenation unit 3-1 is 2, hydrogen/oil volume ratio is 150, the operation temperature is 230oC, the operation pressure is l.0MPa (absolute pressure). Then the above heavy pelrol (distilling range 80~205oC) passes through the pipeline into the heavy pelrol extractor 2 with the flow rate of 60000 tons/years to carry out the extraction separation and the aromatic hydrocarbon & raffmate oil can be separated.The solvent used in extractor 2 is N-formyl-morpholine, the extraction temperature is 115oC the solvent ratio(solvent/feed material) is 3-5(mass), the rinsing ratio of the raffinate oil is 0.2(mass)„ the solvent recovered temperature is 151oC, the recovery pressure of tlte solvent is 0.112MPa [absolute pressure).The above aromatic hydrocarbon enters the aromatic hydrocarbon hydrogenation unit 3-2 with the flow rale of 15000 tons/year to carry out the aromatic hydrocarbon hydrogenation. The catalyst of the above aromatic hydrocarbon hydrogenation unit 3-2 is full hydrogenation catalysl GHT-22.The volume airspeed ratio of the above light petrol hydrogenation and 3-2 is 2, hydrogen/oil volume ratio is 250, the operation temperature is 295oC. the operation pressure it 2.0MPa (absolute pressure). Then it will be blended with Ihe above hydrogenaled light petrel, the above raffmate oil will be extracted out as the chemical light petrol with tlte flow rate of 15000 tons/year. The distilling range of the obtai ncd blended gasoli nc is 30-205oC, the sulfur content is 4.2ppm. tlte mercaptan content is lower than 1ppm olefin content is l7.8%(v), the diolefin content is lower than 0.01 %(v), the aromatic hydrocarbon content is 25.6%(v) the octane numher(RON) is 94.1. the density is 703.8 kg/m3, the extraction volume is 55000 tons/year. The distilling range of the oblained chemical light petrol is 80-205oC, the sulfur content is l0.0ppm, the mercaplan content is l.0ppm. olefin content ii 35.5%(v), the diolefin content is 0.01 %(v), the aromatic hydrocarbon content is 3.0%(v), the octane number(RON) is S 1.0, the density is 760.0 kg/m3, the extraction volume is 45000 urns/year. The physical and chemical characteristics of Lhe selective hydrogenation catalyst GHT-20 are as shown in the following table: Name of lhe index Lnil. GHT-20 Appearance Grey three-leal' type Spue ifi cation mm 1.7 Intensity NVcm 170 Tiulk denshy g/rri 1 0.70 Specific surface inVg ISO Pore volume ml/& 0.55 WO; m% 6.6 NiO m'ft 2.1 OP mfl 0.1S hmbodimem 5 AH shown in figure 3, it is Lhe schematic How shucLof this embodiment. The gasoline is fractionaLed ML fracLionaLor 1 with Lhe How rate of 100,000 ton/year in Lhe to ihe stabilized gas olintifcii Inly tic gasoline) with high sulfur content whose distilling range is 30-205 T. Lhe sulfur content is 2O00ppm, lhe mere apian content ii 50ppni, the olefin eonLenl is 40%(v). the dioletin content is l.0%(v). the aromatic hydrocarbon content is I9%(v), the octane mimbcn(RO\) is 91, density is 7'2S kp/m , Hie fraction ator overhead temperature of fractionator I is 86 °C. the fractionator bottom temperature is 1921, fractionator overhead pressure is 0.2\TPa(absoluije pressure), fracLionaloT hoLLom pressure is 0.2.H1Pa[ahsoluLe pressure), li^ht petrol and heavy petrol can be separately obtained. The above light petrol (distilling range 30-90oC) is vaporized through the upper of fractionator 1, then it enters the light peirol hydrogenation apparatus 3-1 to carry out hydrogenation treatment, the total vaporization volume after the hydrogenation is 43,000 cons/year. The catalyst of the above light petrol hydrogenation apparatus 3-1 is selective hydrogenation catalyst GHT-20, the volume airspeed ratio of the above light petrol hydrogenation unit 3-1 is 4. hydrogen/oil volume ratio is. 300, the operation temperature is 250oC, the operation pressure is 1.0MPa (absolute pressure).Then the ahove heavy petrol (distilling range 90-205oC) passes through the pipeline into the heavy petrol extractor 2 with the flow rate of 57000 tons/years to carry out the extraction separation and the aromatic hydrocarbon &. raffinate oil can be separated. The solvent used in extractor 2 is N -formyl-morphline, the extraction temperature is 115oC. the solvent ratio(solvent/feed material) is 3.5(mass), the rinsing ratio of the raffinate od is 0.2(mass), the solvent recovered temperalure is 151oC, the recovery pressure of the solvent is 0.112MPa (absolute pressine).The above aromatic hydrocarbon enters the aromatic hydrocarbon hydrogenation unit 3-2 with the flow rate of 15000 tons/year to carry out the aromatic hydrocarbon hydro venation, The catalyst of the above aromatic hydrocarbon ■■ ■■ 4.- p- p hydrogenation unit 3-2 is full hydrogen at ion catalyst GHT-22.The volume airspeed ralio of the above aromatic hydrocarbon hydrogenation unil 3-2 is 3. hydrogen/oil volume ratio is 300. the operation temperature is 325oC, the operation pressure is 2.5MPa (absolute pressure), Then it will be blended with the above-hydrogcnated light petrol, the above raffinate oil will be extrated out as the chemical light petrol with the flow rate of 15000 tons/year. The distilling, range of the obtained blended gasoline is 30-205oC, the sulfur content is l0.0ppm, the mercaptan content is lower than 1ppm. olefin content is 17.84%(v). the dioletin content is lower than 0.01%(v), the aromatic hydrocarbon content is- 28.2%(v), the octane number(RON) is 04.05, the density is 721.4 kg/m3 the extraction volume is 64000 tons/year. The distilling range of the obtained chemical light petrol is 90-205oC, the sulfur content is 10.0ppm, the mercaptan content is l.0ppm, olefin content is 58.3%(v), the diolefin content is 0.01%(v), the aromatic hydrocarbon content is 3.0%(v), the octane number(ROM) is 82.0. the density is 740.0 kg/m3 the extraction volume is 36000 tons/year. Industrial applicability The advantage of this invention is as the following: Compared with the pre-hydrogenation (hydrogenation before the stabilized gasoline enters the distilling unit, it must use great volume of catalyst, in addition, it can only reduce the volume of diolefin and mercapalan), the advantage of the catalytic hydrocarbon recombination system and method is as follows: first, because it is specially used for light petrol and/or heavy petrol, and/or aromatic hydrocarbon to carry out the hydrogenalion treatment, the volume of used catalyst is greatly reduced. Secondly, regarding light petrol, and/or heavy petrol, and/or aromatic hydrocarbon, the volume of used catalyst is greatly reduced. Tn addition, the content of olefin and diolefin can be reduced, we can not only reduce the content of the mercaptan, but can also reduce the general sulfur content. Finally, as for the selective hydrogenation. specific catalysts and parameters are used, mainly through removal of mercaptan, we can solve the olefin and diolefin problem, the effect is remarkable, I Claim: 1. A system for preparation of a high quality gasoline through recombination of catalytic hydrocarbon, comprising a fractionator, wherein an upper part of the fractionator is connected with a light petrol hydrogenation equipment through a light petrol pipeline; a lower part of the fractionator is cotinected with an extractor through a heavy petrol pipeline: the upper part of the extractor directly extracts the produce through a pipeline and rhe lower part of the extractor is connected to a light perrol pipeline behind a light petrol hydrogenation unit. 2. A system according to claim 1, wherein a lower part of a distilling unit is first connected to a heavy petrol hydrogenation unit through the heavy petrol pipeline, then the heavy petrol hydroge nation unit is connected to the extractor through a pipeline. 3. A system according to claim 1, wherein the lower part of the extractor is first connected to an aromatic hydrocarbon hydroge nation unit through the heavy petrol pipeline, then the aromatic hydrocarbon hydragenation unit is connected to the light petrol pipeline behind the light petrol hydroge nation unit. 4. A process for preparation of a high quality gasoline through recombination of catalytic hydrocarbon comprising: putting stabilized gasoline into a fractionator to carry out distilling and fractionizing into light petrol and heavy petrol; the light petrol enters a light petrol hydroge nation unit through an upper part of a distilling unit to carry out hydrogenation; the heavy petrol is extracted in an extractor and separated into aromatic hydrocarbon and raffinate oil; the aromatic hydrocarbon is blended and used with the light petrol after the hydrogenatecl light petrol, the raffinate oil is directly extracted as chemical light oil. 5. A process according to claim 4, wherein hydrogeiiation is first carried out in the heavy petrol hydrogenation unit before the heavy petrol enters the extractor to carry out the extraction separation. 6. A process according to claim 4, wherein first the aromatic hydrocarbon is hydrogenated through an aromatic hydrocarbon hydrogenation unit and then it is blended and used with the hydrogenated light petrol. 7. A process according to any claims 4-6. wherein a temperature at overhead at overhead of the fractionator is 100-110oC, a termperature at bottom the fractionator is 206-225oC, a pressure at overhead of thefractionator is 0.11-028MPa(absolute pressure), a pressure a bottom of the fractionator is 0.12-030MPa(absolute pressure). a distillation range of the light petrol is controlled to 30oC-100oC and a distillation range of the heavy gasoline is controlled to 100oC-205oC 8. A process according to any claims 4-6. wherein a temperature at overhead of the fractionator is 105oC a temperature at bottom of the fractionator is 216oC. a pressure at overhead of the fraction ator is 0.11-0.28MPa(absolute pressure), a pressure at bottom of the fractionator is 0. 12-0.30MPa(absolate pressure), a distillation range of the light petrol is controlled to 30oC-100oC and a distillation range of the heavy gasoline is controlled lo 100oC-205oC, 9. A process according to claim 4 wherein a catalyst of the light petrol hydrogenation unit is selective hydrogenation catalyst GHT-20. volume airspeed ratio of the light petrol hydrogenation unit is 2-4, hydrogen/oil volume ratio is 250-350, operation temperature is 240-260oC, operation pressure is 1.4~1.6MPa (absolute pressure). 10. A process according to claim 9 wherein physical and chemical characteristics of the catalyst of the light petrol hydrogenation unit, i.e., selective hydrogenation catalyst GHT-20 are is shown in the following table: Name of the index Unit CHT-20 Appearance Grey three-leaf type Specification mm ф1.5-2.0 Intensity N/cm 170 Bulk density g/ml 0.70 Speufk surface m% 180 Pore volume ml/g 0. 5-0.6 wo3 m% 6.6 NiO m% 2.1 CoO m% 0.16 11. A process according to claim 5, wherein a catalys of the heavy petrol hydrogenation unit is lull hydrogenation catalys GHT-22, volume airspeed ratio of the heavy petrol hydrogenation unit is 2-4, hydrogen/oil volume ratio is 250-350, operation temperature is 290-330oC, operation pressure is 1.2~3MPa (absolute pressure). 12. A process according to claim 11, wherein physical and chemical characteristics of the catalyst of the heavy petrol hydrogenation unit, i.e., full hydro genation catalyst GHT-22 are as shown in the follow ins table: Name of the index Unit GHT-22 Appearance Grey three-leaf type Specification m m ф1.5-2.0 Intensity N/cm 180 Bulk density g/ml 0.73 Specific surface m2/g 180 Pore volume ml/a ■_ 0.5-0.6 WO3 m% 15 NiO m% 1.7 CoO m% 0.15 Na2O m% Fe2O3 m% SiO2 m% Carrier m% 82.4 13. A process according to claim 6. wherein the catalyst of the heavy petrol hydrogenation unit is fullhydrogenation catalyst GHT-22, volume airspeed ratio of the heavy petrol hydrogenation unit is 2-3, hydrogen/oil volume ratio is 250-300, operation lempeiaiure is 285-325oC, operation pressure is 1.5-2.5MPa (absolute pressure). 14. A process according to claim 13, wherein physical and chemical characteristics of the catalyst of the heavy petrol hydro genation unit. i.e.. full hydrogenaation catalyst GHT-22 arc as shown in the following table: Name of the index Unit GHT-22 Appearance Grey three-leaf type Specification m m ф 1.5-2.0 Intensity N/cm 180 Bulk density g/ml 0.73 Specific surface m2/g 180 Pore volume ml/g 0.5-0.6 WO3 m% 15 NiO m% 1.7 CoO m% 0.15 Na2O m% Fe2O3 m% SiO2 m% Carrier m% 82.4

Full Text

FORM 2
THE PATENTS ACT, 1970
(39 of 1970)
&
The Patent Rules, 2003
COMPLETE SPECIFICATION
1. TITLE OF THE INVENTION:
A SYSTEM FOR THE PREPARATION OF A HIGH QUALITY GASOLINE THROUGH THE RECOMBINATION OF CATALYTIC HYDROCARBON AND ITS PROCESS
2. APPLICANT:
Name: DING, Ranfeng
Nationality: A Chinese National
Address: B-1805, Jinma Building, No.38, Xueqing Road, Haidian District, Beijing, China
.
3. PREAMBLE TO THE DESCRIPTION:
The following specification particularly describes the invention and the manner in which it is to be performed:

Field of the invention
This invention relates to a system for the preparation of a high quality gasoline and its process.
and more particularly to a system for the preparation of a high quality gasoline through the recombination of catalytic hydrocarbon and its process.
BACKGROUND OF THE INVENTION
Catalvtie cracking, catalytic schizolvsis and heavy oil catalytic schizolysis technology is the
key technology of Lhe oil refining, catalytic schizolysis is classified into the catalytic schizolysis of wax oil and the catalytic schizolysis of heavy oil, The generated oils produced from these processes are collectively called catalytic hydrocarbons. Through the processing & handling, generally fractionation with fractionation fractionator. the obtained catalytic hydrocarbons can be fractionated into the products such as dry petroleum gas liquefied petroleum gas, gasoline, dicscl oil and heavy oil etc. Among them, the gasoline and diesel oil occupy above 70% of the supply volume of the gasoline and diesel oil in the market,
As the environmental protection requirements become more and more strict, the standard of gasoline & diesel oil will be increased continuously, The current processing method wherein The catalytic hydrocarbons go throught tractionator has the following shortcomings the first is That the quality of the produced gasoline and diesel oil should be improved, the alkene content, is too high, octane value (RON) is too low, the octane number of the diesel oil is, too low, the stability does not conform to the requirements. The second is that the above processing method can not produce multiple grades of gasoline simultaneously in addition, there is only one product type The third is that the proportion between produced gasoline and diesel oil docs not conform to the market need, the diesel oil can not satisfy the need, whereas Lhe gasoline is in oversupply status.

In order to solve the above problem, Chinese patent with patent N=03148181.7 namely trealmenl method of catalyzing the hydrocarbon recombination" has provided a type of treatment method of catalyzing the hydrocarbon recombination, furthermore, the Chinese palents with palenL N=200310103541.9 and 2003 10103540.4 have given publicity to the improved patents concerning the water rinsing system and solvent recycling, however, the methods of reducing sulfur and oletin have not been touched upon in these publicized patents.
The current GB17930 gasoline standard requires that the sulfur content is below 0-05% (wt), the olefin content is below 35%(v) and the benzend content is below 2.5%(v). Most of the refineries can assure the quality of the gasoline, However, the National Gasoline Standard III that will be implemented in 2010 requires the following: the sulfur content is below 0.015% (wt), the olefin content is below 25%(v) or even lower and the benzene content is below l%(v). For must of the refineries, they must be confronted with the requirements of higher standard, i.e., the National Gasoline Standard IV: the sulfur content is below 0.005% (wt), the olefin content is below 25%(v) or even lower, Gasoline quality solution must consider the transition from National Gasoline Standard III to National Gasoline Standard IV. The better planning is to follow National Gasoline Standard IV in single step.
Since the proportions of blended components in the gasoline products of our country differ greatly with those of the developed countries, the catalytic cracking gasoline (hereafter called catalytic gasoline) occupies a high proportion while reformed gasoline and gasoline alkyl ate only occupies a little proportion, Furthermore. this condition will exist for a long time, Therefore, the method of reducing sulfur and olefin mainly touches upon the problem of catalyzed gasoline,
it is generally acknowledged that 5-10% of the general sulfur in the catalytic cracking

material will enter the gasoline fraction. According to the eharacterislics of the refineries in our country that catalytic material hydrogenation purification capability is low, secondary processing catalytic cracking capability is high and there is residual oil coking, the sulfur content of the catalytic gasoline in the refinery processing the crude oil with low sulfur content (sulfur content 0.3%) is about 200ppm. if the crude oil with sulfur content of 0 8%, the sulfur content of the catalytic gasoline is about 900ppm. Therefore, the difficult point in the upgrade of gasoline quality has changed from the problem of olefin to the problem of sulfur, It is impossible lo radically solve the problem of sulfur through the improvement of catalytic cracking process or catalyst The catalytic cracking material hydrogenation and desulfurization cannot be applied in large scale due lo big investment, high operation cost and current condition in the refineries, Furthermore, it is inapplicable lo the refineries processing rude oil with low sulfur content. In the meantime, the catalytic cracking equipment excessively reduces the olefine therefore, it will aggravate the loss of benzoline and the octane number (RON) of the gasoline,
Therefore, it is a technical problem that how to provide a system for blended gasoline having low sulfur content, low olefin contenl and high octane number (RON) with low cost.
Summary of the invention
One of the object of the invention is to provide a gasoline catalytic hydrocarbon recombination system having low salfur content, low olefin conlenl and high octane number (RON ) with low cost is provided.
In order to realize the shove purpose, this invention adopts the following technical resolution: A system for the preparation of a high quality gasoline through the recombination of catalytic hydrocarbon, including fractionator, wherein the upper part of the said fractionator is connected with light petrol hydrogenation equipment through the light petrol pipeline. The lower part of the said fractionator is connected with the extractor through the heavy petrol

pipeline. The upper part of the said extractor directly extracts the product through the pipeline
and the lower part of the said extractor is counseled to the light pelrol pipeline behind the
light pelrol hydrogenalion unit.
A preferred system, wherein the lower part of the said fraetionator is connceeted with the
heavy petrol hydrogenation unit through heavy petrol pipeline, the said heavy petrol
hydrogenation unit is then connected to the extractor through the pipeline.
A preferred system, wherein the lower part of the said extractor is connected with the
aromatic hydrocarbon hydrogenation unit through the pipeline, the said aromatic hydrocarbon
hydrogenation unit is then connected to the light petrol hydrogenstion unit through the
pipeline,
Another object of the invention is to provide the process of said high quality gasoline preparation through catalytic hydrocarbon recombination,
The technical resolution as follows:
A process for the preparation of a high quality gasoline through catalytic hydrocarbon recombination, wherein lhe stabilized gasoline is put into the fractionator to carry out the distilling and fractionaize into the light petrol and heavy pelrol, The above light pelrol enters the light petrol hydrogenation unit to carry out the hydrogenation. The above heavy petrol is extracted in the extractor and separate inlo aromatic hydrocarbon and rallinate oil, the above aromatic hydrocarbon is blended with the light petrol after the hydrogenation treatment through the pipeline and the shove raffinatcoil will he directly extracted as chemical light oil.
A preferred process, wherein hydration treatment is first carried out in the heavy petrol hydration unil to the said heavy petrol before the extraction is earned out in the extractor.
A preferred process, wherein first hydration treatment is carried out to the above aromatic

hydrocarbon, then it is blended with and used together with the light petrol after the hydration treatment through the pipeline.
A preferred process, wherein the fractionator overhead temperature of the above fractionator is 100-110oC, the fractionator bottom temperature is 206-226oC, the fractionator overhead pressure of the above fractionator is 0.11-0.28MPa(absolute pressure), the fractionator bottom pressure is 0.12-0.30MPa(absolute pressure), the distillation range of the above light petrol is controlled to 30oC-100oC and the distillation range of the above heavy gasoline is controlled to 100°C-205oC.
A preferred process, wherein The fractionator overhead Temperature of the above tractionator is 105oC, the fractions tor bottom temperature is 216oC. the fractionator overhead pressure of the above fractionator is 0.11-0.28MPa(absolute pressure), the fractionator bottom pressure is 0.12-0,30MPa(absolute pressure), the distillation range of the above light petrol is controlled to 30oC- 100oC and the distillation range of the above heavy gasoline is controlled to 100o C -205oC.
A preferred process, wherein the catalyst of the above light petrol hydrogenation unit is selective hydro genation catalyst GHT-20. the volume airspeed ratio of the above light petrol hydrogenation unit is 2-4, hydrogen/oil volume ratio is 250-350, the operature is 240~260oC the operation pressure is 1.4-1.6MPa (absolute pressure).
A preferred process, wherein the physical and chemical characteristics of the catalyst of the said light petrol hydrogenalion unit. i.e.. selective hydrogenalion catalyst GHT-20 are as shown in the following table:

Name of the index Unit GHT-20
Appearance Grey three-leaf type
Specification mm ф1.5-2.0
Intensity N/cm 170
Bulk density g/ml 0.70
Specific surface m2/g 180
Pore volume ml/g 0.5-0.6
wo3 m% 6.6
NiO m% 2.1
CoO m% 0.16
A preferred process, wherein the catalyst of the said heavy gasoline hydrogenalion unit is full hydrogenation catalyst, GHT-22. the volume airspeed ratio of the said heavy gasoline hydrogenalion unit is 2-4, hydrogen/oil volume ratio is 250-350. the operation temperature is 290~330oC, the operation pressure is 1.2~3MPa (absolute pressure).
A preferred process, wherein the physical and chemical characteristics of the said heavy gasoline hydrogenalion unit GHT-22 are as shown in the following table:

Name of the index Unit GHT-22
Appearance Grey three-leaf type
Specification mm ф1.5-2.0
Intensity N/cm 180
Bulk densily g/ml 0.73
Specific surface m /g 180
Pore volume ml/g 0.5-0.6
W03 m% 15

NiO m% 1.7
CoO m% 0,15
Na2O m% Fe2O3 m% Si02 m%
Carrier m%
824
A preferred process, wherein the catalyst of the above aromatic hydrocarbon hydrogenation unit is full hydrogenation catalyst GHT 22, the volume airspeed ratio of the said aromatic hydrocarbon hydrogenation unit is 2-3, hydrogen/oil volume ratio is 250-300, Lhe operation temperature is 285-352oC the operation pressure is 1.5-2.5 MPa (absolute pressure).
A preferred prosscess wherein the physical and chemical characteristics of thee catalyst of the said aromatic hydrocarbon hydrogenation unit, i.e.. full hydrogenation catalyst GHT-22 are as shown in the following table:

Name of the index Unit GHT-22
Appearance Grey three-leat type
Specifics Lion mm ф 1.5-2.0
Intensity N/cm 180
Bulk density g/ml 0,73
Specific surface m2/g 180
Pore volume ml/g 0.5 0.6
wo3 m% 15
NiO m% 1.7
CoO m% 0.15

Na2O m% Fe2O3 m% SiO2 m% Carrier m.% 82/1
The fartionator used in this invention is the fractionator disclosed in the China patent 0314S181.7 namely 'catalytic hydrocarbon recombination treatment method". the said extractor uses the estractor disclosed in the China patebts 200310103541,9 and 200310103540.4. induding solvent recycling and water rinsing system,
the hydrogenation unit used in this invention is the current hydrogenation unit including healing furnace, heal exchanger, high-presure separator, air condenser and wafer condenser etc.
Brief description of the description of the drawing
In the following, we will further explain this invention through attached drawings and
embodiments, but this does not mean the limitation to this invention.
Figure 1 is lhe schematic flow sheet of embodiment 1, Figure 2 is lhe schematic flow sheet of embodiment 2 and 3, Figure 3 is the schematic flow sheet, of embodiment. 4 and 5.
Detailed description of the preferred Embodiment
Embodiment 1
See figure 1. it is the schematic flow sheet of this embodiment. The gasoline is fractionated at
fractionator 1 with the flow rate of 100,000 ton/year to the stabilized agsolinot catalytic
gasoline) wherein the distilling range is 30-205oC. sulfur content is 85ppm. mercaptan content

is 15ppm, olefin content is 25%(v), diolefin content is 0.1%(v), aromatic hydrocarbon content is 13%(v), octane number (RON) is 87, density is 728 kg/m3 the overhead temperature of the fractionator 1 is 105oC. the fractionator bottom temperature is 216oC, fractionator overhead pressure is 0.2MPa(absolute pressure), fractionator bottom pressure is 0.25MPa(absolute pressure), light petrol and heavy petrol can be separately obtained. The above light petrol(di tilling range 30-100°C) is vaporized through the overhead of fractionator 1, the total vaporization volume is 50,000 tons/year, then it enters the light petrol hydrogenalion apparatus 3 to carry out hydrogenalion treatement. The catalyst of the above light petrol hydrogenation apparatus 3 is selective hydrogenation catalyst GHT-20,The volume airspeed ratio of the above light petrol hydrogenation unit 3 is 4. hydrogen/oil volume ratio it 300. [he operation temperature is 250oC, the operation pressure is 1.5MPa (absolute pressure) (selective hydrogenation) . The above heavy petrol (distilling range is 100-205oC) enters the heavy petrol extractor 2 for solvent extraction with the flow rale of 50000 tons/year and aromatic hydrocarbon and raffinate oil are separated out The solvent used in the above extractor 2 is sulfolane, the extraction tempera lure is 120 C. the ratio of solvent (sol vent/feed material lis 4.0, the rinsing ratio of the raffinate oil is 0.2(mass), the recovered temperature of the solvent is 175oC, the recovered pressure of the solvent is 0.065MPa(absolute pressure), Lhe above aromatic hydrocarbon is blended with Lhe hydrogen tiled light petrol with the flow rale of 11000 tons/year, the above raffinate oil is extracted out as the chemical light petrol with the flow rale of 39000 tons/year,
The distilling range of lhe obtained blended petrol is 30-205 oC. the sulfur content is 102.8ppm, the mercaptan content is 4 3ppm, the olefin content is 17.9%(v), the diolefin content is 0,05%(v),the aromatic hydrocarbon content is 20.0%(v), the octane number(RON) is 91,8, the density is 700.6kg/m3, the oil produced is 39000 tons/year.
The distilling range of the obtained chemical light petrol is 100-205°C, the sulfur content is 29.0ppm, the mercaptan content is 1.0ppm, the olefin content is 28.2%(v). the diolcfin content is 0.01% (v), the aromatic hydrocarbon content is 3.0%(v), the octane number(RON)

is 78.5, the density is 775.5kg/m3, the oil produced is 39,000 lons/year,
The physical and chemical characteristics of the selective hydrogenation catalyst GHT-20 are
as shown in the following table:

Name of the index Unit GHT-20
Appearance Grey three-leaf type
Specification m m ф 1.7
Intensity N/cm 170
Hulk density G/ml 0.70
Specific surface M2/g 180
Pare volume ml/g
0.55
WO3
NiO M% 6.6 2.1
CoO M% 0.16
The measuring methods used in this invention arc as follows:
1. Distilling range: G B/T6536-1997 petroleum products-determination of distillation
2. Sulfur content: SH/T0689-2000 light hydrocarbon & engine fuel and other petroleum products-determination of total sulfur contend ultra-luminescence method)
3. Mercaplan sulfur: GB/T1792-1988 Distillate fuck-Determination of mercaptan sulphur--Potenliametric titration method.
4. Olcfin; GB/T 11132-2002 Liquid petroleum products-Determination of hydrocarbon types -Fluorescent indicator absorption method
5. Aromatic hydrocarbon: GB/TI1132-2002 Liquid petroleum products-Determination of hydrocarbon types-Fluorescent indicator absorption method

6, Octane number GB/T5487 gasoline-testing menthods for octane number -research method
7, Density; GB/T18834-2000, method for laboratory measurement of crude oil and liquid petroleum productst densitometer method)

8, Measurement of the diolefin: titration method
9. Hydroge nation catalyse analysis method:

Chemical Analytical procedure Applied petrochemical industry
component standard
NiO Colonmetric analysis SH/T0346-1992
CoO Colori metric analysis SH/T0345-1992
WO3 Colorimetric analysis
Physical Analytical procedure Applied instrument
characteristics
Surface area Low temperature nitrogen adsorption 2-100 model sorption analyzer
Pore volume Mercury inrusion method Auto Pore II 9200
Intensity Cold Crushing Strength DI. II type intelligent granular
measurement method intensity measuring gauge
Bulk density Weighing method
Embodiment 2
See figure 2. it is the schematic flow sheet of this embodiment. The gasoline is fractionated at fractionator 1 with the flow rate of 100,000 ton/year in the tractionator 1 to the stabilized gasoline(catalytic gasoline) wherein low sulfur content whose distillinng range is 30-205oC, the sulfur content is 100ppm, the mercaptan content is. 5ppm, the olefin content is 30%(v), the diolcfin content is 0.1%(v), the aromatic hydrocarbon content is 15%(v), the octane number(RON) is 89, density is 728 kg/m3, the fractionator overhead temperature of fraclionalor 1 is 82oC, the fraelionalor bottom temperature is 186oC. fractionator overhead pressure is 0.2MPa(absolute pressure), fraction ator bottom pressure is 0.25MPa(absolute

pressure), light petrol and heavy petrol can be separately obtained. The above light pctrol(distilling range 30-80oC) is vaporized through the upper of fraetionator 1, the total vaporization volume is 40,000 tons/year, then it enters the light petrol hydrogenation apparatus 3-1 to carry out hydrogenation treatment The catalyst of the above light petrol hydrogenation apparatus 3-1 is selective hydrogenation catalyst GHT-20.The volume airspeed ratio of the ahove light petrol hydrogenation unit 3 1 is 2, hydrogen/oil volume ratio is 150, the operation temperature is 220oC, the operation pressure is 0.6MPa (absolute pressure). The above heavy petrol(distilling range is 80 205oC) enters the heavy petrol hydrogenation unit 3-2 to carry out hydrogenation treatment with the flow rate of 60000 Lons/year Lhe catalyst of the above heavy petrol hydrogenation apparatus .3 2 is full hydrogenation catalyst GHT 22. The volume airspeed ratio of the above heavy petrol hydrogenation unit 3-2 is 2, hydrogen/oil volume ratio is 250, the operation temperature is 290oC the operation pressure is l.2MPa (absolute pressure). Then it passes through the pipeline into the heavy petrol extraetor 2 LO carry out Lhe extraction separation and the aromatic hydrocarbon & raffinate oil can be separated, The solvent used in extractor 2 is N-pyrrolidone, the extraclion temperature is 115 oC the solvent ratio(solvent/feed material) is 3.5 (mass), the rinsing ratio of the raffinate oil is 0,2(mass), the solvent recovered temperalture is 151 oC the recovery pressure of the solveut is 0.112MPA (absolute pressure). The above aromatic hydrocarbon is blended with the above-hydrogenated light petrol with the flow rate of 15000 tons/year, the above raffimale oil is extracted out with the flow rate of 45000 tons/year as the fine quality ethylene material. The distilling range of the ohtained blended gasoline is 30-205oC. the sulfur content is 5.27ppm, the mereaplan content is lower than lppm, olefin content is 17.8%(v), the diolefin content is 0.01 %(v), the aromatic hydrocarbon content is 25.6%(v), the octane number(RON) is 94.1, the density is 703.8 kg/m3, the extraction volume is 55000 tons/year. The distilling range of the obtained fine quality ethylene material is 80-205oC, the sulfur content is 2.0ppm. the merecaptan content is lower than lppm. olefin content is 0.1%(v), the dioJcfin content is 0.01%(v), the aromatic hydrocarbon content is 3.0%(v), the octane

number (RON) is 81 0. the density is 760.0 kg/m3 the extraction volume is 45000 tons/year. The physical and chemical characteristics of the se leetive hydrogenalinn calnlyst GHT-20 are as shown in the- following table:

Name of the index Unit GHT-20
Appearance Grey three-leaf type
Specification mm 01,7
Intensity N/cm 170
Bulk density g/ml 0.70
Specific suffice m2/g 180
Pore volume ml/g 0.55
WO3
NIO m% m% 6.6
2.1
C0O m% 0.16
The physical and chemical characteristics of the full hydrogenation talalyst GHT-22 are as shown in the following table:

Name of the index Unit GHT-22
Appearance Grey three-leat type
Specification mm ф1.7
In tensity N/cm 180
Bulk density g/ml 0.7.1
Specific surface m/g 180
Pore volume ml/g 0.57
WO3 m% 15
NiO m% 1.7
CoO m% 0.15

Na2O Fe2O3 m% SiO2 m% Carrier m% 82.4
The measuring methods used in this invention are as follows (same below):
1. Distilling range: GB/T6536-1997 petroleum products -determination of distillation
2. Sulfur content: SH/T0689-2000 light hydrocarbon & engine fuel and other petroleum products-deierminadon of total sulfur contenlfultra-luminescence method)
3. Mercaptan sulfur: GB/T1792-1985 Distillate fuels--Determination of mercaptan sulphur Potentiantptric titration method
4. Olefin: GB/T111.32-2002 Liquid patroleum products-Determination of hydrocarbon types-Fluoresceni indicator absorption method
5. Aramaic hydrocarbon: GB/T11 132-2002 Liquid petroleum products-Determination of hydrocarbon types-Fluorescent indicator absorption method
6. Octane number: GB/T5487 gasoline- testing methods for octane number -research method
7. Density: GB/T1884-2000, method for laboratory measurement of crude oil and liquid
petroleum products (densitometer method ) 8. Measurement of the diolefin: titration method 9. Hydrogenation catalyst analysis method:

Chemical component. Analytical procedure Applied petrochemical industry standar d
NiO Colorimetric analysis SH/T034G-1992
CoO Colorimetric analysis SH/T034-1992
WO3 Colorimetric analysis
Physical characteristics Analytical procedure Applied instrument

Surface area Low temperature nitrogen adsorption 2400 model sorption analyzer
Pore volume Mercury intrusion method Auto Pore II 9200
Intensity Cold Crushing Strength DL II type intelligent granular intensity
measurement method measuring gauge
Bulk density Weighing method
Embodiment 3
As shown in figure 2, it is the schematic flow sheet of this embodiment, The gasoline is fractionated at fractionator 1 with the flow rate of 100.000 ton/year to the stabilized gaiolinc(catalytic gasoline) with high sulfur content whose distilling range is 30-205oC. the sulfur content is 2000ppm, the mercaptan content is 50ppm, the olefin content is 40%(v), the diolefin content is l.0%(v), the aromatic hydrocarbon content is 19%(v), the octane number (RON) is 91 density is 728 kg/m3, the fractionator overhead temperature of fractionator 1 is 86oC, the fractionator bottom temperature is 192oC, fractionator overhead pressure is 0.2MPa(absolute pressure), fractionator bottom pressure is 0.25MPa(absolute pressure), light petrol and heavy petrol can be separately obtained. The above light petrol(distilling range 30-80oC) is vaporized through the upper of fractionalor 1, the total vaporization volume is 43,000 tons/year, then it enters lhe light petrol hydrogenation apparatus 3-1 to tarry out hydrogenation treatment, The catalyst of the above light petrol hydrogenation apparatus 3-1 is selective hydrogenation catalyst GHT-20. The volume airspeed ratio of the above light patrol hydrogenation unit 3-1 is 4, hydrogen/oil volume ratio is 300, the operation temperature is 280°C. the operation pressure is 2.0MPa (absolute pressure). The above heavy petrol(distilling range 90-203 °C) enters heavy petrol hydrogenation unit 3-2 TO carry out hydrogenation treatment with the flow rate of 57000 tons/year, The catalyst of lhe light petrol hydrogenation apparatus 3-2 is selective hydrogenation catalyst GHT-20, lhe

volume airspeed ratio af the above light petrol hydrogenation unit 3-2 is 4, hydrogen/oil volume ratio is 350, the operation temperature is 330oC, the operation pressure is 3.0V1Pa (absolute pressure). Then it passcs through the pipeline into the heavy petrol extractor 2 to carry out the extraction separation and the aromatic hydrocarbon & raffinate oil can be separated/The solvent used in extractor 2 is N- pyrrolidine, the extraction temperature is 115 °C, the solvent ratio(solvent/feed material) is 3,5(mass), the rinsing ratio of the raffinate oil is 0.2(mass) the solvent recovered temperature is 151 oC, The recovery pressure of the solvent is 0.112MPa (absolute pressure). The above aromatic hydrocarbon is blended with the above hydrogenated light petrol with the flow rate of 19000 tons/year, the above raffinate oil is extracted out with the flow rate of 38000 as The fine quality ethylene: material. The distilling range of the obtained blended gasoline is 30-205oC the sulfur content is 7.52ppm. the mercaptan content is lower than 1ppm, olefin content is 17.99%(v), the diolefin content is 0.01%(v), the aromatic hydrocarbon content is 29-1 %(v), the octane number(RON) is 95.2, the density is 720.1 kg/m3. the extraction volume is 62000 Lous/year. The distilling range ol the obtained fine quality ethylene material is 00-205oC. the sulfur content is 2.0ppm, the mercaptan content is lower than 1ppm, olefin content is 6%(v), the diolefin content is lower than 0.01%(v), the aromatic hydrocarbon content is 3.0%(v), the octanc number(RON) is 81.5. the density is 740.0 kg/m3, the extraction volume is 38000 tons/year.
Embodiment 4
As shown in figure 3, it is the schematic flow sheet of this embodiment.
The gasoline is fractionated at fractionator I with the flow rale of 100,000 ton/year lo the stabilized gasolinc(catalytic gasoline) with low sulfur content whose distilling range is 30-205 oC the sulfur content is 100ppm, the mcrcaptan content is 5ppm, the olefin content is 30%(v), the diolefin conlent is 0.1%(v), lhe womatic hydroearbon content is 15%(v). the octane number(RON) is 89, density is 728 kg/m3. the fraelionator overhead temperature of

fractionator 1 is 86oC, the fractionator bottorm temperature is 192oC, fractionator overhead pressure is 0.2MPa(absolute pressure), fractionator bottom pressure is 0.25MPa(absolute pressure), light petrol and heavy petrel can be separately obtained, The above light petrol(distilling range 30-80oC) vaporized through the upper of fraetronator 1, then it enters tlte light petrol hydrogenation apparatus 3-1 to carry out hydrogention treatment, the total vaporization volume after the hydrogcnation is 40.000 tons/year. The catalyst of the above light petrol hydrogenation apparatus 3-1 is selective hydrogenation catalyst GHT-20. tlte volume airspeed ratio of the above light petrol hydrogenation unit 3-1 is 2, hydrogen/oil volume ratio is 150, the operation temperature is 230oC, the operation pressure is l.0MPa (absolute pressure). Then the above heavy pelrol (distilling range 80~205oC) passes through the pipeline into the heavy pelrol extractor 2 with the flow rate of 60000 tons/years to carry out the extraction separation and the aromatic hydrocarbon & raffmate oil can be separated.The solvent used in extractor 2 is N-formyl-morpholine, the extraction temperature is 115oC the solvent ratio(solvent/feed material) is 3-5(mass), the rinsing ratio of the raffinate oil is 0.2(mass)„ the solvent recovered temperature is 151oC, the recovery pressure of tlte solvent is 0.112MPa [absolute pressure).The above aromatic hydrocarbon enters the aromatic hydrocarbon hydrogenation unit 3-2 with the flow rale of 15000 tons/year to carry out the aromatic hydrocarbon hydrogenation. The catalyst of the above aromatic hydrocarbon hydrogenation unit 3-2 is full hydrogenation catalysl GHT-22.The volume airspeed ratio of the above light petrol hydrogenation and 3-2 is 2, hydrogen/oil volume ratio is 250, the operation temperature is 295oC. the operation pressure it 2.0MPa (absolute pressure). Then it will be blended with Ihe above hydrogenaled light petrel, the above raffmate oil will be extracted out as the chemical light petrol with tlte flow rate of 15000 tons/year. The distilling range of the obtai ncd blended gasoli nc is 30-205oC, the sulfur content is 4.2ppm. tlte mercaptan content is lower than 1ppm olefin content is l7.8%(v), the diolefin content is lower than 0.01 %(v), the aromatic hydrocarbon content is 25.6%(v) the octane numher(RON) is 94.1. the density is 703.8 kg/m3, the extraction volume is 55000 tons/year.

The distilling range of the oblained chemical light petrol is 80-205oC, the sulfur content is l0.0ppm, the mercaplan content is l.0ppm. olefin content ii 35.5%(v), the diolefin content is 0.01 %(v), the aromatic hydrocarbon content is 3.0%(v), the octane number(RON) is S 1.0, the density is 760.0 kg/m3, the extraction volume is 45000 urns/year.
The physical and chemical characteristics of Lhe selective hydrogenation catalyst GHT-20 are as shown in the following table:

Name of lhe index Lnil. GHT-20
Appearance Grey three-leal' type
Spue ifi cation mm 1.7
Intensity NVcm 170
Tiulk denshy g/rri 1 0.70
Specific surface inVg ISO
Pore volume ml/& 0.55
WO; m% 6.6
NiO m'ft 2.1
OP mfl 0.1S
hmbodimem 5
AH shown in figure 3, it is Lhe schematic How shucLof this embodiment.
The gasoline is fractionaLed ML fracLionaLor 1 with Lhe How rate of 100,000 ton/year in Lhe to
ihe stabilized gas olintifcii Inly tic gasoline) with high sulfur content whose distilling range is
30-205 T. Lhe sulfur content is 2O00ppm, lhe mere apian content ii 50ppni, the olefin eonLenl
is 40%(v). the dioletin content is l.0%(v). the aromatic hydrocarbon content is I9%(v), the
octane mimbcn(RO\) is 91, density is 7'2S kp/m , Hie fraction ator overhead temperature of
fractionator I is 86 °C. the fractionator bottom temperature is 1921, fractionator overhead
pressure is 0.2\TPa(absoluije pressure), fracLionaloT hoLLom pressure is 0.2.H1Pa[ahsoluLe
pressure), li^ht petrol and heavy petrol can be separately obtained. The above light

petrol (distilling range 30-90oC) is vaporized through the upper of fractionator 1, then it enters the light peirol hydrogenation apparatus 3-1 to carry out hydrogenation treatment, the total vaporization volume after the hydrogenation is 43,000 cons/year. The catalyst of the above light petrol hydrogenation apparatus 3-1 is selective hydrogenation catalyst GHT-20, the volume airspeed ratio of the above light petrol hydrogenation unit 3-1 is 4. hydrogen/oil volume ratio is. 300, the operation temperature is 250oC, the operation pressure is 1.0MPa (absolute pressure).Then the ahove heavy petrol (distilling range 90-205oC) passes through the pipeline into the heavy petrol extractor 2 with the flow rate of 57000 tons/years to carry out the extraction separation and the aromatic hydrocarbon &. raffinate oil can be separated. The solvent used in extractor 2 is N -formyl-morphline, the extraction temperature is 115oC. the solvent ratio(solvent/feed material) is 3.5(mass), the rinsing ratio of the raffinate od is 0.2(mass), the solvent recovered temperalure is 151oC, the recovery pressure of the solvent is 0.112MPa (absolute pressine).The above aromatic hydrocarbon enters the aromatic hydrocarbon hydrogenation unit 3-2 with the flow rate of 15000 tons/year to carry out the aromatic hydrocarbon hydro venation, The catalyst of the above aromatic hydrocarbon
■■ ■■ 4.- p- p
hydrogenation unit 3-2 is full hydrogen at ion catalyst GHT-22.The volume airspeed ralio of the above aromatic hydrocarbon hydrogenation unil 3-2 is 3. hydrogen/oil volume ratio is 300. the operation temperature is 325oC, the operation pressure is 2.5MPa (absolute pressure), Then it will be blended with the above-hydrogcnated light petrol, the above raffinate oil will be extrated out as the chemical light petrol with the flow rate of 15000 tons/year. The distilling, range of the obtained blended gasoline is 30-205oC, the sulfur content is l0.0ppm, the mercaptan content is lower than 1ppm. olefin content is 17.84%(v). the dioletin content is lower than 0.01%(v), the aromatic hydrocarbon content is- 28.2%(v), the octane number(RON) is 04.05, the density is 721.4 kg/m3 the extraction volume is 64000 tons/year. The distilling range of the obtained chemical light petrol is 90-205oC, the sulfur content is 10.0ppm, the mercaptan content is l.0ppm, olefin content is 58.3%(v), the diolefin content is 0.01%(v), the aromatic hydrocarbon content is 3.0%(v), the octane number(ROM) is 82.0. the

density is 740.0 kg/m3 the extraction volume is 36000 tons/year.
Industrial applicability
The advantage of this invention is as the following:
Compared with the pre-hydrogenation (hydrogenation before the stabilized gasoline enters the distilling unit, it must use great volume of catalyst, in addition, it can only reduce the volume of diolefin and mercapalan), the advantage of the catalytic hydrocarbon recombination system and method is as follows: first, because it is specially used for light petrol and/or heavy petrol, and/or aromatic hydrocarbon to carry out the hydrogenalion treatment, the volume of used catalyst is greatly reduced. Secondly, regarding light petrol, and/or heavy petrol, and/or aromatic hydrocarbon, the volume of used catalyst is greatly reduced. Tn addition, the content of olefin and diolefin can be reduced, we can not only reduce the content of the mercaptan, but can also reduce the general sulfur content. Finally, as for the selective hydrogenation. specific catalysts and parameters are used, mainly through removal of mercaptan, we can solve the olefin and diolefin problem, the effect is remarkable,

I Claim:
1. A system for preparation of a high quality gasoline through recombination of catalytic hydrocarbon, comprising a fractionator, wherein an upper part of the fractionator is connected with a light petrol hydrogenation equipment through a light petrol pipeline; a lower part of the fractionator is cotinected with an extractor through a heavy petrol pipeline: the upper part of the extractor directly extracts the produce through a pipeline and rhe lower part of the extractor is connected to a light perrol pipeline behind a light petrol hydrogenation unit.
2. A system according to claim 1, wherein a lower part of a distilling unit is first connected to a heavy petrol hydrogenation unit through the heavy petrol pipeline, then the heavy petrol hydroge nation unit is connected to the extractor through a pipeline.
3. A system according to claim 1, wherein the lower part of the extractor is first connected to an aromatic hydrocarbon hydroge nation unit through the heavy petrol pipeline, then the aromatic hydrocarbon hydragenation unit is connected to the light petrol pipeline behind the light petrol hydroge nation unit.
4. A process for preparation of a high quality gasoline through recombination of catalytic hydrocarbon comprising: putting stabilized gasoline into a fractionator to carry out distilling and fractionizing into light petrol and heavy petrol; the light petrol enters a light petrol hydroge nation unit through an upper part of a distilling unit to carry out hydrogenation; the heavy petrol is extracted in an extractor and separated into aromatic hydrocarbon and raffinate oil; the aromatic hydrocarbon is blended and used with the light petrol after the hydrogenatecl light petrol, the raffinate oil is directly extracted as chemical

light oil.
5. A process according to claim 4, wherein hydrogeiiation is first carried out in the heavy petrol hydrogenation unit before the heavy petrol enters the extractor to carry out the extraction separation.
6. A process according to claim 4, wherein first the aromatic hydrocarbon is hydrogenated through an aromatic hydrocarbon hydrogenation unit and then it is blended and used with the hydrogenated light petrol.
7. A process according to any claims 4-6. wherein a temperature at overhead at overhead of the fractionator is 100-110oC, a termperature at bottom the fractionator is 206-225oC, a pressure at overhead of thefractionator is 0.11-028MPa(absolute pressure), a pressure a bottom of the fractionator is 0.12-030MPa(absolute pressure). a distillation range of the light petrol is controlled to 30oC-100oC and a distillation range of the heavy gasoline is controlled to 100oC-205oC
8. A process according to any claims 4-6. wherein a temperature at overhead of the fractionator is 105oC a temperature at bottom of the fractionator is 216oC. a pressure at overhead of the fraction ator is 0.11-0.28MPa(absolute pressure), a pressure at bottom of the fractionator is 0. 12-0.30MPa(absolate pressure), a distillation range of the light petrol is controlled to 30oC-100oC and a distillation range of the heavy gasoline is controlled lo 100oC-205oC,
9. A process according to claim 4 wherein a catalyst of the light petrol hydrogenation unit is selective hydrogenation catalyst GHT-20. volume airspeed ratio of the light petrol hydrogenation unit is 2-4, hydrogen/oil volume ratio is 250-350, operation temperature is

240-260oC, operation pressure is 1.4~1.6MPa (absolute pressure).
10. A process according to claim 9 wherein physical and chemical characteristics of the catalyst of the light petrol hydrogenation unit, i.e., selective hydrogenation catalyst GHT-20 are is shown in the following table:

Name of the index Unit CHT-20
Appearance Grey three-leaf type
Specification mm ф1.5-2.0
Intensity N/cm 170
Bulk density
g/ml 0.70
Speufk surface m% 180
Pore volume ml/g 0. 5-0.6
wo3 m% 6.6
NiO m% 2.1
CoO m% 0.16
11. A process according to claim 5, wherein a catalys of the heavy petrol hydrogenation unit is lull hydrogenation catalys GHT-22, volume airspeed ratio of the heavy petrol hydrogenation unit is 2-4, hydrogen/oil volume ratio is 250-350, operation temperature is 290-330oC, operation pressure is 1.2~3MPa (absolute pressure).
12. A process according to claim 11, wherein physical and chemical characteristics of the catalyst of the heavy petrol hydrogenation unit, i.e., full hydro genation catalyst GHT-22 are as shown in the follow ins table:

Name of the index Unit GHT-22

Appearance Grey three-leaf type
Specification m m ф1.5-2.0
Intensity N/cm 180
Bulk density g/ml 0.73
Specific surface m2/g 180
Pore volume ml/a
■_ 0.5-0.6
WO3 m% 15
NiO m% 1.7
CoO m% 0.15
Na2O m% Fe2O3 m% SiO2 m% Carrier m% 82.4
13. A process according to claim 6. wherein the catalyst of the heavy petrol hydrogenation unit is fullhydrogenation catalyst GHT-22, volume airspeed ratio of the heavy petrol hydrogenation unit is 2-3, hydrogen/oil volume ratio is 250-300, operation lempeiaiure is 285-325oC, operation pressure is 1.5-2.5MPa (absolute pressure).
14. A process according to claim 13, wherein physical and chemical characteristics of the catalyst of the heavy petrol hydro genation unit. i.e.. full hydrogenaation catalyst GHT-22 arc as shown in the following table:

Name of the index Unit GHT-22
Appearance Grey three-leaf type
Specification m m ф 1.5-2.0
Intensity N/cm 180

Bulk density g/ml 0.73
Specific surface m2/g 180
Pore volume ml/g 0.5-0.6
WO3 m% 15
NiO m% 1.7
CoO m% 0.15
Na2O m% Fe2O3 m% SiO2 m% Carrier m% 82.4

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Patent Number

277993

Indian Patent Application Number

744/MUMNP/2010

PG Journal Number

51/2016

Publication Date

09-Dec-2016

Grant Date

07-Dec-2016

Date of Filing

13-Apr-2010

Name of Patentee

DING Ranfeng

Applicant Address

B-1805 Jinma Building No.38 Xueqing Road Haidian District Beijing China.

Inventors:

#	Inventor's Name	Inventor's Address
1	DING Ranfeng	B-1805 Jinma Building No.38 Xueqing Road Haidian District Beijing China.

PCT International Classification Number

C10G 7/00,C10G 21/00

PCT International Application Number

PCT/CN2008/072943

PCT International Filing date

2008-11-05

PCT Conventions:

#	PCT Application Number	Date of Convention	Priority Country
1	200710169947.5	2007-11-09	China
2	200710169942.2	2007-11-09	China
3	200710169949.4	2007-11-09	China