CN101497808A - System and method for preparing high quality petrol - Google Patents
System and method for preparing high quality petrol Download PDFInfo
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- CN101497808A CN101497808A CN 200810005208 CN200810005208A CN101497808A CN 101497808 A CN101497808 A CN 101497808A CN 200810005208 CN200810005208 CN 200810005208 CN 200810005208 A CN200810005208 A CN 200810005208A CN 101497808 A CN101497808 A CN 101497808A
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Abstract
The invention discloses a system and a method for preparing high quality petrol. The system comprises a distillation device and is characterized in that the upper part of the distillation device is connected with a light petrol extraction system by a light petrol pipeline; the upper part of the light petrol extraction system directly extracts the product by a pipeline; the lower part of the light petrol extraction system is connected with a hydrogenation unit by a pipeline; the lower part of the distillation device is connected with a heavy petrol extraction system by a heavy petrol pipeline; the upper part of the heavy petrol extraction system directly extracts the product, and the lower part of the heavy petrol extraction system is connected with the hydrogenation unit by a pipeline. The system and the method can perform deolefination and remove mercaptans and diene and has small scale and low cost.
Description
Technical field
The present invention relates to a kind of system and method thereof for preparing premium-type gasoline.
Background technology
Catalytic cracking, catalytic pyrolysis and heavy oil catalytic pyrolysis technology are the core technologies of oil refining, and catalytic cracking is divided into wax catalysis cracking, heavy oil fluid catalytic cracking; Be referred to as catalytic hydrocarbon from the generation oil of these explained hereafter, the gained catalytic hydrocarbon is through processing treatment, generally be the separation column fractionation, can fractionate out products such as net gas, liquefaction vapour, gasoline, diesel oil, heavy oil, wherein gasoline, more than 70% of diesel oil total supply on gasoline, the diesel oil occuping market.
More and more strictness along with environmental requirement, the standard of gasoline, diesel oil improves constantly, existing catalytic hydrocarbon is showed following deficiency through the fractionated processing and treating method of separation column: one is that the gasoline produced of this treatment process and the quality of diesel oil have much room for improvement: the olefin(e) centent of gasoline is higher, (RON) is on the low side for octane value, diesel-fuel cetane number is on the low side, and stability is undesirable; The 2nd, above-mentioned treatment process can not be produced the gasoline of multiple label simultaneously, and range of product is single; The 3rd, the demand in the diesel oil of being produced, the ratio of gasoline and market does not match, and diesel oil can not satisfy the demands, and gasoline supply exceed demand.
In order to address the above problem, the patent No. is that the Chinese invention patent of 03148181.7 " catalytic hydrocarbon reorganization treatment process " provides a kind of catalytic hydrocarbon reorganization treatment process, and the patent No. is respectively 200310103541.9 and 200310103540.4 Chinese invention patent and discloses it and improve patent, relate to water wash system and solvent recuperation, but all do not relate to the problem of how to fall sulphur and falling alkene in these disclosed patents.
Present GB17930 gasoline standard requires sulphur content to be not more than 0.05% (wt), olefin(e) centent to be not more than 35% (v), benzene content is not more than 2.5% (v), most refinerys can guarantee quality of gasoline.But the national III gasoline standard that is about to implement in 2010 requires: sulphur content is not more than 0.015% (wt), olefin(e) centent and is not more than 30% (v), benzene content is not more than 1% (v).For most refinery, must require in the face of higher national IV gasoline standard: sulphur content is not more than 0.005% (wt), alkene and is not more than 25% (v) or lower.The quality of gasoline solution must be considered the transition from national III gasoline standard to national IV gasoline standard, and programme should be disposable according to national IV gasoline standard programme preferably.
Because ratio and developed country's difference of each blend component is very big in China's gasoline products, catalytically cracked gasoline occupies very high ratio, and reformed gasoline, gasoline alkylate proportion are less, and this situation is with long-term existence.Therefore, the quality of gasoline upgrading problem of falling sulphur and falling alkene to be solved relates generally to the problem of catalytic gasoline.
It is generally acknowledged, the 5-10% of total sulfur will enter gasoline fraction in the catalytically cracked material,, secondary processing catalytic cracking ability very little according to China's refinery fcc raw material hydrofining ability is big and the characteristics of residuum coking are arranged, the about 200ppm of refinery catalytic gasoline sulphur content of processing low-sulfur (sulfur-bearing 0.3%) crude oil, the crude oil of processing sulfur-bearing 0.8%, the about 900ppm of sulphur content in the catalytic gasoline, therefore, the difficult point of quality of gasoline upgrading changes the problem of sulphur into from alkene.The improvement of catalytic cracking process or catalyzer can not fundamentally solve the problem of sulphur, the catalytically cracked material hydrogenating desulfurization is because investment is big, working cost is high, existing refinery condition is limited and impossible large-scale application, and it is also inapplicable for the refinery of the low sulphur-bearing crude of processing, simultaneously, catalytic cracking unit excessively reduces the loss that alkene also can aggravate light-end products and gasoline octane rating (RON).
Can not deolefination with caustic wash desulfuration, but also can cause environmental pollution; By to the petroleum naphtha hydrotreatment, energy consumption height not only, expense is also high.
Therefore, provide the treatment system of the high blended gasoline of a kind of low cost, less energy-consumption, pollution-free preparation low sulfur content, low olefin-content and octane value (RON) and method thereof just to become the technical barrier that this technical field is badly in need of solution.
Summary of the invention
One of purpose of the present invention provides the system of the gasoline of a kind of low cost, less energy-consumption, pollution-free preparation low sulfur content, low olefin-content and boosting of octane rating (RON).
For achieving the above object, the present invention takes following technical scheme:
A kind of system for preparing premium-type gasoline comprises water distilling apparatus; It is characterized in that: described water distilling apparatus top is connected with the petroleum naphtha extraction system by pipeline; Described petroleum naphtha extraction system top is by the direct extraction product of pipeline, and described petroleum naphtha extraction system bottom is connected with hydrogenation unit by pipeline; Described water distilling apparatus bottom is connected with the heavy petrol extraction system by pipeline; Described heavy petrol extraction system top is by the direct extraction product of pipeline, and described heavy petrol extraction system bottom is connected with hydrogenation unit by pipeline.
A kind of optimal technical scheme is characterized in that: gasoline and be connected with described hydrogenation unit by pipeline in the described water distilling apparatus middle part cutting output.
Another object of the present invention provides the above-mentioned method for preparing premium-type gasoline.
A kind of method for preparing premium-type gasoline, its step is as follows: stable gasoline or stable gasoline are added water distilling apparatus with petroleum naphtha and hydrogenation coker gasoline carry out fractionation, cutting fractionates out petroleum naphtha and heavy petrol; Described petroleum naphtha enters the petroleum naphtha extraction system by water distilling apparatus top and carries out extracting and separating, isolates to extract oil out and raffinate oil; Described extraction oil uses described raffinating oil as the direct extraction of blended gasoline with described petroleum naphtha mediation after entering hydrogenation device for treatment by pipeline; Described heavy petrol carries out extracting and separating at the heavy petrol extraction system, isolates to extract oil out and raffinate oil; Described extraction oil obtains hydrogenation extraction oil after entering hydrogenation device for treatment by pipeline, is in harmonious proportion with described petroleum naphtha and uses described raffinating oil as chemical industry light oil.
A kind of preferred version is characterized in that: the middle part cutting of described water distilling apparatus fractionates out middle gasoline and enters hydrotreatment in the described hydrogenation unit.
A kind of preferred version is characterized in that: the tower top temperature of described water distilling apparatus is 77～86 ℃, and column bottom temperature is 190～192 ℃; The tower top pressure of described water distilling apparatus is 0.11～0.28MPa (cutting off), and tower bottom pressure is 0.12～0.30MPa (cutting off); The boiling range of described petroleum naphtha is controlled at 30 ℃～90 ℃; The boiling range of described heavy petrol is controlled at 90 ℃～205 ℃.
A kind of preferred version is characterized in that: the tower top temperature of described water distilling apparatus is 77～86 ℃, and column bottom temperature is 190～192 ℃; The tower top pressure of described water distilling apparatus is 0.11～0.28MPa (cutting off), and tower bottom pressure is 0.12～0.30MPa (cutting off); The boiling range of described petroleum naphtha is controlled at 30 ℃～65 ℃; The boiling range of gasoline is controlled at 65 ℃～90 ℃ in described; The boiling range of described heavy petrol is controlled at 90 ℃～205 ℃.
A kind of preferred version is characterized in that: the tower top temperature of described water distilling apparatus is 82 ℃, and column bottom temperature is 191 ℃; The tower top pressure of described water distilling apparatus is 0.2MPa (cutting off), and tower bottom pressure is 0.25MPa (cutting off).
A kind of preferred version is characterized in that: the catalyzer in the described hydrogenation unit is whole hydrogenation catalyst GHT-22; The volume space velocity of described hydrogenation unit is than being 2-3; Hydrogen/oil volume ratio is 200～300; Service temperature is 285～325 ℃, and working pressure is 1.5～2.5MPa (cutting off).
A kind of preferred version is characterized in that: the physico-chemical property of the whole hydrogenation catalyst GHT-22 in the described hydrogenation unit is as shown in the table.
Petroleum naphtha described in the present invention and heavy petrol extraction system can shared solvent recovering systems, also can use different solvent recovering systems respectively.
Petroleum naphtha of the present invention, stable gasoline and hydrogenation coker gasoline can be arbitrary proportions.
The cut point of petroleum naphtha of the present invention and heavy petrol (boiling range) can be adjusted.
The used water distilling apparatus of the present invention is that the patent No. is a disclosed Distallation systm in the Chinese invention patent of 03148181.7 " catalytic hydrocarbon reorganization treatment process ".Used extraction system is that the patent No. is a disclosed extraction system in 200310103541.9 and 200310103540.4, comprises solvent recuperation and water wash system.
The used hydrogenation unit of the present invention is existing hydrogenation unit, comprises process furnace, interchanger, high-pressure separator, atmospheric condenser, water condenser etc.
Beneficial effect:
The system of preparation low sulfur content of the present invention and gasoline with low olefine content and the advantage of method thereof are: compare with the alkali cleaning mode, system and method for the present invention can not only deolefination, can also mercaptan removal, and diene (diolefine); Compare with the petroleum naphtha hydrogenation, hydrogenation unit of the present invention is only oily at extracting out, small scale, and cost is low; At last, stable gasoline is not only handled in the raw material variation that the present invention handles, and can also handle the mixture of stable gasoline and petroleum naphtha and hydrogenation coker gasoline.Also contain in petroleum naphtha and the hydrogenation coker gasoline and extract oil out, chemical industry light oil is optimized, and the extraction oil in the blended gasoline increases, and octane value improves.
The present invention will be further described below by the drawings and specific embodiments, but and do not mean that limiting the scope of the invention.
Description of drawings
Fig. 1 is the schematic flow sheet of the embodiment of the invention 1.
Fig. 2 is the schematic flow sheet of the embodiment of the invention 2.
Fig. 3 is the schematic flow sheet of the embodiment of the invention 3.
Embodiment
Embodiment 1
As shown in Figure 1, be the schematic flow sheet of the embodiment of the invention 1.With boiling range is 30-205 ℃, and sulphur content is 2000ppm, and mercaptans content is 50ppm, and olefin(e) centent is 40%, and (v), diene content is 1.0% (v), aromaticity content is that 19% (v), octane value (RON) is 91, and density is 728 kilograms/meter
3Stable gasoline (catalytic gasoline) in distillation tower 1, cut fractionation with 100,000 tons/year flow, the tower top temperature of distillation tower 1 is 86 ℃, column bottom temperature is 192 ℃, tower top pressure is 0.2MPa (cutting off), and tower bottom pressure is 0.25MPa (cutting off), obtains petroleum naphtha and heavy petrol respectively, described petroleum naphtha (boiling range is 30-90 ℃) steams by distillation tower 1 top, its total amount of steaming is 4.3 ten thousand tons/year, enters extracting and separating among the petroleum naphtha extraction system 2-1 then, isolates to extract oil out and raffinate oil; Solvent for use is the N-formyl morpholine among the described extraction system 2-1, extraction temperature is 80 ℃, and solvent ratio (solvent/charging) is 2.5 (quality), and the washing of raffinating oil is than being 0.2 (quality), the solvent recuperation temperature is 149 ℃, and solvent recuperation pressure is 0.112MPa (cutting off); The oily flow with 1.08 ten thousand tons/year of described extraction is extracted oil and blended gasoline mediation extraction out as hydrogenation after entering hydrogenation unit 3 hydrotreatments, and the catalyzer in the described hydrogenation unit 3 is whole hydrogenation catalyst GHT-22; The volume space velocity of described hydrogenation unit 3 is than being 2h
-Hydrogen/oil volume ratio is 250; Service temperature is 295 ℃, and working pressure is 2.5MPa (cutting off); Described raffinating oil with 3.23 ten thousand tons/year flow as the blended gasoline extraction.Described heavy petrol (boiling range is 90-205 ℃) enters extracting and separating among the heavy petrol extraction system 2-2 with 5.7 ten thousand tons/year flows, isolates to extract oil out and raffinate oil; Solvent for use is the N-formyl morpholine among the described extraction system 2-2, extraction temperature is 115 ℃, and solvent ratio (solvent/charging) is 3.5 (quality), and the washing of raffinating oil is than being 0.2 (quality), the solvent recuperation temperature is 151 ℃, and solvent recuperation pressure is 0.112MPa (cutting off); The oily flow with 2.01 ten thousand tons/year of described extraction enters and carries out in the hydrogenation unit 3 extracting oil and blended gasoline mediation extraction out as hydrogenation after the hydrotreatment; Described raffinating oil with 3.6 ten thousand tons/year flow as the chemical industry light oil extraction.
The boiling range of gained blended gasoline is 30-205 ℃, and sulphur content is 28.4ppm, and mercaptans content is 1.0ppm, and olefin(e) centent is that 21.3% (v), diene content is not less than 0.01% (v) (trace can detect); Aromaticity content is that 32.15% (v), octane value (RON) is 93.1, and density is 721.4 kilograms/meter
3, produced quantity is 6.4 ten thousand tons/year.
The boiling range of gained chemical industry light oil is 90-205 ℃, sulphur content is 10.0ppm, mercaptans content is 1.0ppm, olefin(e) centent is 52.0% (v), (v) (trace can't be measured), aromaticity content are 3.0% (v) to diene content less than 0.01%, octane value (RON) is 82.0, and density is 740.0 kilograms/meter
3, produced quantity is 3.6 ten thousand tons/year.
The physico-chemical property of whole hydrogenation catalyst GHT-22 in the described hydrogenation unit is as shown in the table.
The used measuring method of the present invention is (down together):
1, boiling range: GB/T6536-1997 measured for petroleum product distillation method;
2, sulphur content: the total sulfur content assay method (ultraviolet fluorescence method) of SH/TO689-2000 light hydrocarbon and motor spirit and other oil products;
3, mercaptan sulfur: mercaptan sulfur assay method (potentiometric titration) in the GB/T1792-1988 distillate fuel oil;
4, alkene: GB/T11132-2002 liquid petroleum product hydro carbons assay method (fluorescent indicator adsorption method);
5, aromatic hydrocarbons: GB/T11132-2002 liquid petroleum product hydro carbons assay method (fluorescent indicator adsorption method);
6, octane value: GB/T5487 testing octane number of gasoline method (organon);
7, density: GB/T1884-2000 crude oil and liquid petroleum product density experiment chamber assay method (densimeter method);
8, the mensuration of diene (diolefine): volumetry.
9, hydrogenation catalyst analytical procedure:
| Chemical constitution | Analytical procedure | The petrochemical industry standard that adopts |
| NiO | Colorimetry | SH/TO346-1992 |
| CoO | Colorimetry | SH/TO345-1992 |
| WO 3 | Colorimetry | |
| Physical property | Analytical procedure | The instrument that uses |
| Surface-area | Low-temperature nitrogen adsorption method | 2400 types absorption instrument |
| Pore volume | Mercury penetration method | Auto?Pore?II?9200 |
| Intensity | The crush strength assay method | DL II type intelligence granule strength determinator |
| Bulk density | Weighing method |
Embodiment 2
As shown in Figure 2, be the schematic flow sheet of the embodiment of the invention 2.With boiling range is 30-205 ℃, and sulphur content is 100ppm, and mercaptans content is 5ppm, and olefin(e) centent is 30%, and (v), diene content is 0.1% (v), aromaticity content is that 15% (v), octane value (RON) is 89, and density is 728 kilograms/meter
3Stable gasoline (catalytic gasoline) in distillation tower 1, cut fractionation with 60,000 tons/year flow; Simultaneously, be 30-205 ℃ with boiling range, sulphur content is 200ppm, and mercaptans content is 1ppm, and the content of alkene is less than 0.1% (v) (trace can't detect); (v) (trace can't detect), aromaticity content are that 8% (v), octane value (RON) is 82, and density is 732 kilograms/meter to diene content less than 0.01%
3Petroleum naphtha in distillation tower 1, cut fractionation with 20,000 tons/year flow; Meanwhile, be 30-205 ℃ with boiling range, sulphur content is 150ppm, mercaptans content is 1ppm, olefin(e) centent is that 6% (v), diene content is less than 0.01% (v) (trace can't detect), aromaticity content is that 10% (v), octane value (RON) is 79, and density is 721 kilograms/meter
3The hydrogenation coker gasoline in distillation tower 1, cut fractionation with 20,000 tons/year flow; The tower top temperature of distillation tower 1 is 82 ℃, column bottom temperature is 190 ℃, tower top pressure is 0.2MPa (cutting off), tower bottom pressure is 0.25MPa (cutting off), obtain petroleum naphtha and heavy petrol respectively, described petroleum naphtha (boiling range is 30-90 ℃) steams by distillation tower 1 top, and its total amount of steaming is 4.0 ten thousand tons/year, enter extracting and separating among the petroleum naphtha extraction system 2-1 then, isolate and extract oil out and raffinate oil; Solvent for use is the N-formyl morpholine among the described extraction system 2-1, extraction temperature is 80 ℃, and solvent ratio (solvent/charging) is 2.5 (quality), and the washing of raffinating oil is than being 0.2 (quality), the solvent recuperation temperature is 149 ℃, and solvent recuperation pressure is 0.112MPa (cutting off); The oily flow with 0.8 ten thousand tons/year of described extraction is extracted oil and blended gasoline mediation extraction out as hydrogenation after entering hydrogenation unit 3 hydrotreatments, and the catalyzer in the described hydrogenation unit 3 is whole hydrogenation catalyst GHT-22; The volume space velocity of described hydrogenation unit 3 is than being 2.5h
-Hydrogen/oil volume ratio is 200; Service temperature is 285 ℃, and working pressure is 1.5MPa (cutting off); Described raffinating oil with 3.2 ten thousand tons/year flow as the blended gasoline extraction.Described heavy petrol (boiling range is 90-205 ℃) enters extracting and separating among the heavy petrol extraction system 2-2 with 6.0 ten thousand tons/year flows, isolates to extract oil out and raffinate oil; Solvent for use is the N-formyl morpholine among the described extraction system 2-2, extraction temperature is 115 ℃, and solvent ratio (solvent/charging) is 3.5 (quality), and the washing of raffinating oil is than being 0.2 (quality), the solvent recuperation temperature is 151 ℃, and solvent recuperation pressure is 0.112MPa (cutting off); The oily flow with 1.2 ten thousand tons/year of described extraction enters and carries out in the hydrogenation unit 3 extracting oil and blended gasoline mediation extraction out as hydrogenation after the hydrotreatment; Described raffinating oil with 4.8 ten thousand tons/year flow as the chemical industry light oil extraction.
The boiling range of gained blended gasoline is 30-205 ℃, and sulphur content is 7.9ppm, and mercaptans content＜1ppm (trace can not detect), olefin(e) centent are that 11.8% (v), diene content is not less than 0.01% (v) (trace can detect); Aromaticity content is that 22.1% (v), octane value (RON) is 92.12, and density is 717.76 kilograms/meter
3, produced quantity is 5.2 ten thousand tons/year.
The boiling range of gained chemical industry light oil is 90-205 ℃, sulphur content is 31.0ppm, mercaptans content is 1.0ppm, olefin(e) centent is 18.9% (v), (v) (trace can not detect), aromaticity content are 2.0% (v) to diene content less than 0.01%, octane value (RON) is 76.5, and density is 738.1 kilograms/meter
3, produced quantity is 4.8 ten thousand tons/year.
The physico-chemical property of whole hydrogenation catalyst GHT-22 in the described hydrogenation unit 3 is as shown in the table.
Embodiment 3
As shown in Figure 3, be the schematic flow sheet of the embodiment of the invention 3.With boiling range is 30-205 ℃, and sulphur content is 100ppm, and mercaptans content is 5ppm, and olefin(e) centent is 30%, and (v), diene content is 0.1% (v), aromaticity content is that 15% (v), octane value (RON) is 89, and density is 728 kilograms/meter
3Stable gasoline (catalytic gasoline) in distillation tower 1, cut fractionation with 60,000 tons/year flow; Simultaneously, with boiling range is 30-205 ℃, sulphur content is 200ppm, and mercaptans content is 1ppm, and olefin(e) centent is (v) (trace less than 0.1%, can't detect), (v) (trace can't detect), aromaticity content are 8% (v) to diene content less than 0.01%, octane value (RON) is 82, and density is 732 kilograms/meter
3Petroleum naphtha in distillation tower 1, cut fractionation with 20,000 tons/year flow; Meanwhile, be 30-205 ℃ with boiling range, sulphur content is 150ppm, mercaptans content is 1ppm, olefin(e) centent is that 6% (v), diene content is less than 0.01% (v) (trace can't detect), aromaticity content is that 10% (v), octane value (RON) is 79, and density is 721 kilograms/meter
3The hydrogenation coker gasoline in distillation tower 1, cut fractionation with 20,000 tons/year flow; The tower top temperature of distillation tower 1 is 77 ℃, and column bottom temperature is 192 ℃, and tower top pressure is 0.2MPa (cutting off), and tower bottom pressure is 0.25MPa (cutting off), obtains petroleum naphtha, middle gasoline and heavy petrol respectively; Described petroleum naphtha (boiling range is 30-65 ℃) steams by distillation tower 1 top, and its total amount of steaming is 3.0 ten thousand tons/year, enters extracting and separating among the petroleum naphtha extraction system 2-1 then, isolates to extract oil out and raffinate oil; Solvent for use is the N-formyl morpholine among the described extraction system 2-1, extraction temperature is 80 ℃, and solvent ratio (solvent/charging) is 2.5 (quality), and the washing of raffinating oil is than being 0.2 (quality), the solvent recuperation temperature is 149 ℃, and solvent recuperation pressure is 0.112MPa (cutting off); The oily flow with 0.4 ten thousand tons/year of described extraction is extracted oil and blended gasoline mediation extraction out as hydrogenation after entering hydrogenation unit 3 hydrotreatments, and the catalyzer in the described hydrogenation unit 3 is whole hydrogenation catalyst GHT-22; The volume space velocity of described hydrogenation unit 3 is than being 3h
-Hydrogen/oil volume ratio is 300; Service temperature is 325 ℃, and working pressure is 2.5MPa (cutting off); Described raffinating oil with 2.6 ten thousand tons/year flow as the blended gasoline extraction; Gasoline (boiling range is 65-90 ℃) enters after hydrogenation unit 3 hydrotreatments as gasoline in the hydrogenation and blended gasoline mediation extraction by pipeline with 1.0 ten thousand tons/year flows in described; Described heavy petrol (boiling range is 90-205 ℃) enters extracting and separating among the heavy petrol extraction system 2-2 with 6.0 ten thousand tons/year flows, isolates to extract oil out and raffinate oil; Solvent for use is the N-formyl morpholine among the described extraction system 2-2, extraction temperature is 115 ℃, and solvent ratio (solvent/charging) is 3.5 (quality), and the washing of raffinating oil is than being 0.2 (quality), the solvent recuperation temperature is 151 ℃, and solvent recuperation pressure is 0.112MPa (cutting off); The oily flow with 1.2 ten thousand tons/year of described extraction enters and carries out in the hydrogenation unit 3 extracting oil and blended gasoline mediation extraction out as hydrogenation after the hydrotreatment; Described raffinating oil with 4.8 ten thousand tons/year flow as the chemical industry light oil extraction.
The boiling range of gained blended gasoline is 30-205 ℃, and sulphur content is 6ppm, and mercaptans content＜1ppm (trace can not detect), olefin(e) centent are that 11.3% (v), diene content is not less than 0.01% (v) (trace can detect); Aromaticity content is that 22.1% (v), octane value (RON) is 92.1, and density is 717.8 kilograms/meter
3, produced quantity is 5.2 ten thousand tons/year.
The boiling range of gained chemical industry light oil is 90-205 ℃, sulphur content is 31.0ppm, mercaptans content is 1.0ppm, olefin(e) centent is 19.5% (v), (v) (trace can not detect), aromaticity content are 2.0% (v) to diene content less than 0.01%, octane value (RON) is 76.5, and density is 738.1 kilograms/meter
3, produced quantity is 4.8 ten thousand tons/year.
The physico-chemical property of whole hydrogenation catalyst GHT-22 in the described hydrogenation unit 3 is as shown in the table.
Claims (9)
1, a kind of system for preparing premium-type gasoline comprises water distilling apparatus; It is characterized in that: described water distilling apparatus top is connected with the petroleum naphtha extraction system by the petroleum naphtha pipeline; Described petroleum naphtha extraction system top is by the direct extraction product of pipeline, and described petroleum naphtha extraction system bottom is connected with hydrogenation unit by pipeline; Described water distilling apparatus bottom is connected with the heavy petrol extraction system by the heavy petrol pipeline; Described heavy petrol extraction system top is by the direct extraction product of pipeline, and described heavy petrol extraction system bottom is connected with hydrogenation unit by pipeline.
2, the system of preparation premium-type gasoline according to claim 1 is characterized in that: gasoline and be connected with described hydrogenation unit by pipeline in the described water distilling apparatus middle part cutting output.
3, a kind of method for preparing premium-type gasoline, its step is as follows: stable gasoline or stable gasoline are mixed the back add water distilling apparatus and carry out fractionation with petroleum naphtha and hydrogenation coker gasoline, cutting fractionates out petroleum naphtha and heavy petrol; Described petroleum naphtha enters the petroleum naphtha extraction system by water distilling apparatus top and carries out extracting and separating, isolates to extract oil out and raffinate oil; Described extraction oil uses described raffinating oil as the direct extraction of blended gasoline with described petroleum naphtha mediation after entering hydrogenation device for treatment by pipeline; Described heavy petrol carries out extracting and separating at the heavy petrol extraction system, isolates to extract oil out and raffinate oil; Described extraction oil obtains hydrogenation extraction oil after entering hydrogenation device for treatment by pipeline, is in harmonious proportion with described petroleum naphtha and uses described raffinating oil as chemical industry light oil.
4, the method for preparing premium-type gasoline according to claim 3 is characterized in that: the middle part cutting of described water distilling apparatus fractionates out middle gasoline and enters hydrotreatment in the described hydrogenation unit.
5, the method for preparing premium-type gasoline according to claim 3 is characterized in that: the tower top temperature of described water distilling apparatus is 77～86 ℃, and column bottom temperature is 190～192 ℃; The tower top pressure of described water distilling apparatus is 0.11～0.28MPa (cutting off), and tower bottom pressure is 0.12～0.30MPa (cutting off); The boiling range of described petroleum naphtha is controlled at 30 ℃～90 ℃; The boiling range of described heavy petrol is controlled at 90 ℃～205 ℃.
6, the method for preparing premium-type gasoline according to claim 4 is characterized in that: the tower top temperature of described water distilling apparatus is 77～86 ℃, and column bottom temperature is 190～192 ℃; The tower top pressure of described water distilling apparatus is 0.11～0.28MPa (cutting off), and tower bottom pressure is 0.12～0.30MPa (cutting off); The boiling range of described petroleum naphtha is controlled at 30 ℃～65 ℃; The boiling range of gasoline is controlled at 65 ℃～90 ℃ in described; The boiling range of described heavy petrol is controlled at 90 ℃～205 ℃.
7, according to claim 5 or the 6 described methods that prepare premium-type gasoline, it is characterized in that: the tower top temperature of described water distilling apparatus is 82 ℃, and column bottom temperature is 191 ℃; The tower top pressure of described water distilling apparatus is 0.2MPa (cutting off), and tower bottom pressure is 0.25MPa (cutting off).
8, the method for preparing premium-type gasoline according to claim 7 is characterized in that: the catalyzer in the described hydrogenation unit is whole hydrogenation catalyst GHT-22; The volume space velocity of described hydrogenation unit is than being 2-3; Hydrogen/oil volume ratio is 200～300; Service temperature is 285～325 ℃, and working pressure is 1.5～2.5MPa (cutting off).
9, the method for preparing premium-type gasoline according to claim 8 is characterized in that: the physico-chemical property of the whole hydrogenation catalyst GHT-22 in the described hydrogenation unit is as shown in the table.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200810005208 CN101497808B (en) | 2008-01-29 | 2008-01-29 | System and method for preparing high quality petrol |
| PCT/CN2009/070239 WO2009094934A1 (en) | 2008-01-29 | 2009-01-21 | A system and a process for producing high quality gasoline |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200810005208 CN101497808B (en) | 2008-01-29 | 2008-01-29 | System and method for preparing high quality petrol |
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| CN101497808A true CN101497808A (en) | 2009-08-05 |
| CN101497808B CN101497808B (en) | 2013-02-06 |
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| CN 200810005208 Expired - Fee Related CN101497808B (en) | 2008-01-29 | 2008-01-29 | System and method for preparing high quality petrol |
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| CN106833735A (en) * | 2017-01-20 | 2017-06-13 | 杨志强 | Petroleum fluids extraction desulfurization group technology |
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| CN1142258C (en) * | 2000-12-05 | 2004-03-17 | 中国石油化工股份有限公司 | Process for removing sulfide from gasoline fraction by solvent extraction |
| CN201186917Y (en) * | 2008-01-29 | 2009-01-28 | 丁冉峰 | System for preparing high-quality petrol |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106833735A (en) * | 2017-01-20 | 2017-06-13 | 杨志强 | Petroleum fluids extraction desulfurization group technology |
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