CN201334459Y - System for preparing high-quality gasoline by component oil refining, hydrocarbon recombination and post-hydrogenation - Google Patents
System for preparing high-quality gasoline by component oil refining, hydrocarbon recombination and post-hydrogenation Download PDFInfo
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- CN201334459Y CN201334459Y CNU2009201054060U CN200920105406U CN201334459Y CN 201334459 Y CN201334459 Y CN 201334459Y CN U2009201054060 U CNU2009201054060 U CN U2009201054060U CN 200920105406 U CN200920105406 U CN 200920105406U CN 201334459 Y CN201334459 Y CN 201334459Y
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Abstract
The utility model relates to a system for preparing the high-quality gasoline by component oil refining, hydrocarbon recombination and post-hydrogenation. The system comprises an extraction system, a distillation system and hydrogenation units, wherein, the upper part of the distillation system is connected with a light gasoline hydrogenation unit through a pipeline; the lower part of the distillation system is connected with the extraction system through a pipeline; the upper part of the extraction system is connected with a raffinate oil hydrogenation unit through a pipeline, and the lower part of the extraction system is connected with an extract oil hydrogenation unit through a pipeline; and the extract oil hydrogenation unit is connected with a pipeline at the tail end of the light gasoline hydrogenation unit. The system for preparing the high-quality gasoline by post-hydrogenation not only can perform alkene removal, but also can perform mercaptan removal and diolefine removal.
Description
Technical field
The utility model relates to a kind of system for preparing premium-type gasoline, relates in particular to a kind of system of preparing high quality petrol by hydrogenation after, and particularly a kind of hydrogenation after component oil refining hydrocarbon recombination prepares the system of 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 dry gas, liquefied gas, 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 falling sulphur into from falling 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) just to become the technical barrier that this technical field is needed solution badly.
Summary of the invention
The purpose of this utility model provides the system of a kind of low cost, less energy-consumption, pollution-free preparation low sulfur content, low olefin-content and boosting of octane rating (RON) gasoline.
For achieving the above object, the utility model is taked following technical scheme:
A kind of hydrogenation after component oil refining hydrocarbon recombination prepares the system of premium-type gasoline, it is characterized in that: comprise Distallation systm, and extraction system and hydrogenation unit, described Distallation systm top is connected with the petroleum naphtha hydrogenation unit by pipeline; Described Distallation systm bottom is connected with described extraction system by pipeline; Described extraction system top is connected with the hydrogenation unit of raffinating oil by pipeline, and described extraction system bottom is connected with the oily hydrogenation unit of extraction by pipeline; The oily hydrogenation unit of described extraction is connected by the tip line of pipeline with described petroleum naphtha hydrogenation unit.
A kind of hydrogenation after component oil refining hydrocarbon recombination prepares the method for premium-type gasoline, its step is as follows: raw material cuts fractionation in Distallation systm, obtain petroleum naphtha and heavy petrol respectively, described petroleum naphtha steams by Distallation systm top, enter then and carry out hydrotreatment in the petroleum naphtha hydrogenation unit, the petroleum naphtha after the hydrotreatment is as the blended gasoline extraction; Described heavy petrol enters extracting and separating in the extraction system, isolates heavy petrol and raffinates oil and heavy petrol extraction oil; Described heavy petrol is raffinated oil and is entered the hydrogenation unit of raffinating oil and carry out hydrotreatment, after the hydrotreatment as the high-quality ethylene or the material extraction of reforming; Described heavy petrol is extracted oil out and is entered and extract oily hydrogenation unit out and carry out hydrotreatment, mixes afterwards as the blended gasoline extraction with petroleum naphtha after the described hydrotreatment after the hydrotreatment.
A kind of preferred version is characterized in that: described Distallation systm is a distillation tower, and tower top temperature is 78～97 ℃, and column bottom temperature is 167～187 ℃; Tower top pressure is 0.15～0.25MPa (cutting off), and tower bottom pressure is 0.20～0.30MPa (cutting off); The boiling range of described petroleum naphtha is controlled at 30 ℃～110 ℃; The boiling range of described heavy petrol is controlled at 110 ℃～185 ℃.
A kind of preferred version is characterized in that: the tower top temperature of described distillation tower is 88 ℃, and column bottom temperature is 178 ℃; The tower top pressure of described distillation tower is 0.20MPa (cutting off), and tower bottom pressure is 0.25MPa (cutting off).
A kind of preferred version is characterized in that: solvent for use is a tetramethylene sulfone in the described extraction system, and extraction temperature is 120 ℃, solvent ratio (solvent/charging) is 3.5 (quality), raffinate oil washing than being 0.2 (quality), and the solvent recuperation temperature is 165 ℃, and solvent recuperation pressure is 0.1MPa (cutting off).
A kind of preferred version, it is characterized in that: solvent for use is a N-Methyl pyrrolidone in the described extraction system, extraction temperature is 130 ℃, solvent ratio (solvent/charging) is 2.5 (quality), raffinate oil washing than being 0.25 (quality), the solvent recuperation temperature is 177 ℃, and solvent recuperation pressure is 0.15MPa (cutting off).
A kind of preferred version; it is characterized in that: solvent for use is the N-formyl morpholine in the described extraction system; extraction temperature is 150 ℃; solvent ratio (solvent/charging) is 6.0 (quality); raffinate oil washing than being 0.3 (quality); the solvent recuperation temperature is 185 ℃, and solvent recuperation pressure is 0.2MPa (cutting off).
The utility model solvent for use also can other common solvent, the perhaps mixing of the arbitrary proportion of two or more in these solvents.
Petroleum naphtha of the present utility model, stable gasoline and hydrogenation coker gasoline can be arbitrary proportions.
The cut point of petroleum naphtha of the present utility model and heavy petrol (boiling range) can be adjusted.The boiling range of petroleum naphtha is controlled at 30 ℃～70 ℃ as described; The boiling range of described heavy petrol is controlled at 70 ℃～185 ℃; Perhaps, the boiling range of described petroleum naphtha is controlled at 30 ℃～90 ℃; The boiling range of described heavy petrol is controlled at 90 ℃～185 ℃.
The used Distallation systm of the utility model (distillation tower) is disclosed Distallation systm in the Chinese invention patent of 03148181.7 " catalytic hydrocarbon reorganization treatment process " for the patent No..Used extraction system (extraction tower) comprises solvent recuperation and water wash system for the patent No. is a disclosed extraction system in 200310103541.9 and 200310103540.4 Chinese invention patents.
The used hydrogenation unit of the utility model is existing hydrogenation unit, comprises process furnace, interchanger, high-pressure separator, atmospheric condenser, water condenser etc.
Beneficial effect:
The advantage of the system of preparation low sulfur content of the present utility model and gasoline with low olefine content is: compare with the alkali cleaning mode, system of the present utility model is for raw material distillation cutting earlier, and extracting separates again, according to circumstances carry out hydrotreatment then respectively, can not only deolefination, can also mercaptan removal, diene; And stable gasoline is not only handled in the raw material variation that the utility model is handled, 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, high-quality ethylene is optimized, and the extraction oil in the blended gasoline increases, and octane value improves.
Below by the drawings and specific embodiments the utility model is described further, but and does not mean that restriction the utility model protection domain.
Description of drawings
Fig. 1 is the system architecture synoptic diagram of the utility model embodiment 1.
Fig. 2 is the system architecture synoptic diagram of the utility model embodiment 2 and 3.
Embodiment
Embodiment 1
As shown in Figure 1, be the system architecture synoptic diagram of the utility model embodiment 1.With boiling range is 30-185 ℃, 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, the tower top temperature of distillation tower 1 is 78 ℃, column bottom temperature is 167 ℃, tower top pressure is 0.15MPa (cutting off), tower bottom pressure is 0.20MPa (cutting off), obtain petroleum naphtha and heavy petrol respectively, described petroleum naphtha (boiling range is 30-110 ℃) steams by distillation tower 1 top, steaming that it is total is 2.95 ten thousand tons/year, enter then among the petroleum naphtha hydrogenation unit 3-1 and carry out hydrotreatment, the catalyzer among the described hydrogenation unit 3-1 is selective hydrogenation catalyst GHT-20; The volume space velocity of described hydrogenation unit 3-1 is than being 4.0h
-1Hydrogen/oil volume ratio is 300; Service temperature is 150 ℃, and working pressure is 1.0MPa (cutting off); Petroleum naphtha behind the described hydrogenation with 2.95 ten thousand tons/year flow as the blended gasoline extraction.Described heavy petrol (boiling range is 110-185 ℃) enters extracting and separating in the heavy petrol extraction tower 2 with 3.05 ten thousand tons/year flows, isolates heavy petrol extraction oil and heavy petrol and raffinates oil; Solvent for use is a tetramethylene sulfone in the described extraction tower 2, and extraction temperature is 120 ℃, and solvent ratio (solvent/charging) is 3.5 (quality), and the washing of raffinating oil is than being 0.2 (quality), and the solvent recuperation temperature is 165 ℃, and solvent recuperation pressure is 0.1MPa (cutting off); Described heavy petrol is raffinated oil and is entered hydrogenation unit 3-2 with 1.95 ten thousand tons/year flow and carry out hydrotreatment, and the catalyzer among the described hydrogenation unit 3-2 is whole hydrogenation catalyst GHT-22; The volume space velocity of described hydrogenation unit 3-2 is than being 4.0h
-1Hydrogen/oil volume ratio is 500; Service temperature is 320 ℃, and working pressure is 4.0MPa (cutting off); The oily flow with 1.1 ten thousand tons/year of described heavy petrol extraction enters hydrogenation unit 3-3 and carries out hydrotreatment, and the catalyzer among the described hydrogenation unit 3-3 is whole hydrogenation catalyst GHT-22; The volume space velocity of described hydrogenation unit 3-3 is than being 4.0h
-1Hydrogen/oil volume ratio is 500; Service temperature is 290 ℃, and working pressure is 4.0MPa (cutting off); Described heavy petrol is raffinated oil behind the hydrogenation with 1.95 ten thousand tons/year flow as the high-quality ethylene or the material extraction of reforming; Described heavy petrol is extracted out behind the oily hydrogenation with 1.10 ten thousand tons/year flow and is mixed the back as the blended gasoline extraction with petroleum naphtha behind the described hydrogenation.
The boiling range of gained blended gasoline is 30-185 ℃, and sulphur content is 11.5ppm, and mercaptans content is less than 1.0ppm (trace can detect), and olefin(e) centent is that 22.5% (v), diene content 0.01% (v); Aromaticity content is that 20.8% (v), octane value (RON) is 94.9, and density is 716.6 kilograms/meter
3, produced quantity is 4.05 ten thousand tons/year.
The boiling range of the gained high-quality ethylene or the material of reforming is 110-185 ℃, sulphur content is a trace, can not detect, mercaptans content is not less than 1.0ppm (trace can detect), olefin(e) centent is a trace, can not detect, bromine index (bromine valency) 39 (0.039), aromaticity content are 2.0% (v), octane value (RON) is 72.8, and density is 753.0 kilograms/meter
3, produced quantity is 1.95 ten thousand tons/year.
The physico-chemical property of selective hydrogenation catalyst GHT-20 among the described petroleum naphtha hydrogenation unit 3-1 is as shown in table 1 below, and the physico-chemical property of the whole hydrogenation catalyst GHT-22 among described hydrogenation unit 3-2 and the 3-3 is as shown in table 2 below.
Table 1
| Index name | Unit | GHT-20 |
| Outward appearance | - | The grey trilobal cross |
| Specification | mm | Φ1.5-2.0 |
| Intensity | N/cm | 170 |
| Bulk density | g/ml | 0.70 |
| Specific surface | m 2/g | 180 |
| Pore volume | ml/g | 0.5-0.6 |
| WO 3 | m％ | 6.6 |
| NiO | m％ | 2.1 |
| C oO | m％ | 0.16 |
Table 2
| Index name | Unit | GHT-22 |
| Outward appearance | - | The grey trilobal cross |
| Specification | mm | Φ1.5-2.0 |
| Intensity | N/cm | 180 |
| Bulk density | g/ml | 0.73 |
| Specific surface area | m 2/g | 180 |
| Pore volume | ml/g | 0.5-0.6 |
| WO 3 | m％ | 15 |
| NiO | m％ | 1.7 |
| C oO | m％ | 0.15 |
| Na 2O | m％ | ＜0.09 |
| Fe 2O 3 | m％ | ＜0.06 |
| SiO 2 | m％ | ＜0.60 |
| Carrier | m％ | 82.4 |
The used measuring method of the utility model 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/T0689-2000 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/T0346-1992 |
| CoO | Colorimetry | SH/T0345-1992 |
| 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 |
10, bromine index (bromine valency) detects: GB/T-11136-1989.
As shown in Figure 2, be the system architecture synoptic diagram of the utility model embodiment 2.With boiling range is 30-185 ℃, 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 30-185 ℃, sulphur content is 200ppm, and mercaptans content is 1ppm, and olefin(e) centent is (v) (trace less than 0.1%, can not detect), (v) (trace can not 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 30-185 ℃ with boiling range, sulphur content is 150ppm, mercaptans content is 1ppm, olefin(e) centent is that 6% (v), diene content is not less than 0.01% (v) (trace can 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 88 ℃, column bottom temperature is 178 ℃, tower top pressure is 0.20MPa (cutting off), tower bottom pressure is 0.25MPa (cutting off), obtain petroleum naphtha and heavy petrol respectively, described petroleum naphtha (boiling range is 30-110 ℃) steams by distillation tower 1 top, and steaming that it is total is 4.5 ten thousand tons/year, enter then among the petroleum naphtha hydrogenation unit 3-1 and carry out hydrotreatment, the catalyzer among the described hydrogenation unit 3-1 is selective hydrogenation catalyst GHT-20; The volume space velocity of described hydrogenation unit 3-1 is than being 1.0h
-1Hydrogen/oil volume ratio is 100; Service temperature is 220 ℃, and working pressure is 4.0MPa (cutting off); Described petroleum naphtha is raffinated oil with 4.5 ten thousand tons/year flow as the blended gasoline extraction.Described heavy petrol (boiling range is 110-185 ℃) enters extracting and separating in the heavy petrol extraction tower 2 with 5.5 ten thousand tons/year flows, isolates heavy petrol extraction oil and heavy petrol and raffinates oil; Solvent for use is a N-Methyl pyrrolidone in the described extraction tower 2, and extraction temperature is 130 ℃, and solvent ratio (solvent/charging) is 2.5 (quality), and the washing of raffinating oil is than being 0.25 (quality), and the solvent recuperation temperature is 177 ℃, and solvent recuperation pressure is 0.15MPa (cutting off); Described heavy petrol is raffinated oil and is entered hydrogenation unit 3-2 with 4.0 ten thousand tons/year flow and carry out hydrotreatment, and the catalyzer among the described hydrogenation unit 3-2 is whole hydrogenation catalyst GHT-22; The volume space velocity of described hydrogenation unit 3-2 is than being 1.0h
-1Hydrogen/oil volume ratio is 250; Service temperature is 250 ℃, and working pressure is 1.0MPa (cutting off); The oily flow with 1.5 ten thousand tons/year of described heavy petrol extraction enters hydrogenation unit 3-3 and carries out hydrotreatment, and the catalyzer among the described hydrogenation unit 3-3 is whole hydrogenation catalyst GHT-22; The volume space velocity of described hydrogenation unit 3-3 is than being 1.0h
-1Hydrogen/oil volume ratio is 250; Service temperature is 250 ℃, and working pressure is 1.0MPa (cutting off); Described heavy petrol hydrogenation is raffinated oil and is expected extraction with 4.0 ten thousand tons/year flow as high-quality ethylene or reformation; Described heavy petrol hydrogenation is extracted oily flow with 1.5 ten thousand tons/year out and is mixed the back with described hydrogenation petroleum naphtha (4.5 ten thousand tons/year flows) as the blended gasoline extraction.
The boiling range of gained blended gasoline is 30-185 ℃, and sulphur content is 23.5ppm, and mercaptans content is less than 1.0ppm (trace can detect), and olefin(e) centent is that 15.6% (v), diene content is a trace, can not detect; Aromaticity content is that 19.5% (v), octane value (RON) is 94.1, and density is 716.4 kilograms/meter
3, produced quantity is 6.0 ten thousand tons/year.
The boiling range of the gained high-quality ethylene or the material of reforming is 110-185 ℃, sulphur content is a trace, can not detect, and mercaptans content is less than 1.0ppm (trace, can not detect), olefin(e) centent is a trace, can not detect bromine index (bromine valency) 32 (0.032), aromaticity content is 2.1% (v), octane value (RON) is 71.4, and density is 744.5 kilograms/meter 3, and produced quantity is 4.0 ten thousand tons/year.
Selective hydrogenation catalyst GHT-20 among the described hydrogenation unit 3-1, and the physico-chemical property of the whole hydrogenation catalyst GHT-22 in other hydrogenation unit and measuring method are identical with embodiment 1.
Embodiment 3
System architecture is identical with embodiment 2.With boiling range is 30-185 ℃, and sulphur content is 800ppm, and mercaptans content is 9ppm, and olefin(e) centent is 36%, and (v), diene content is 0.9% (v), aromaticity content is that 17% (v), octane value (RON) is 91, and density is 731 kilograms/meter
3Stable gasoline (catalytic gasoline) in distillation tower 1, cut fractionation with 60,000 tons/year flow; Simultaneously, with boiling range is 30-185 ℃, sulphur content is 200ppm, and mercaptans content is 1ppm, and olefin(e) centent is (v) (trace less than 0.1%, can not detect), (v) (trace can not 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 30-185 ℃ with boiling range, sulphur content is 150ppm, mercaptans content is 1ppm, olefin(e) centent is that 6% (v), diene content is not less than 0.01% (v) (trace can 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 97 ℃, column bottom temperature is 187 ℃, tower top pressure is 0.25MPa (cutting off), tower bottom pressure is 0.30MPa (cutting off), obtain petroleum naphtha and heavy petrol respectively, described petroleum naphtha (boiling range is 30-110 ℃) steams by distillation tower 1 top, and steaming that it is total is 4.5 ten thousand tons/year, enter then among the petroleum naphtha hydrogenation system 3-1 and carry out hydrotreatment, the catalyzer among the described hydrogenation unit 3-1 is selective hydrogenation catalyst GHT-20; The volume space velocity of described hydrogenation unit 3-1 is than being 2.5h
-1Hydrogen/oil volume ratio is 150; Service temperature is 180 ℃, and working pressure is 2.0MPa (cutting off); Described petroleum naphtha is raffinated oil with 4.5 ten thousand tons/year flow as the blended gasoline extraction.Described heavy petrol (boiling range is 110-185 ℃) enters extracting and separating in the heavy petrol extraction tower 2 with 5.5 ten thousand tons/year flows, isolates heavy petrol extraction oil and heavy petrol and raffinates oil; Solvent for use is the N-formyl morpholine in the described extraction tower 2, and extraction temperature is 150 ℃, and solvent ratio (solvent/charging) is 6.0 (quality), and the washing of raffinating oil is than being 0.3 (quality), and the solvent recuperation temperature is 185 ℃, and solvent recuperation pressure is 0.2MPa (cutting off); Described heavy petrol is raffinated oil and is entered hydrogenation unit 3-2 with 3.9 ten thousand tons/year flow and carry out hydrotreatment, and the catalyzer among the described hydrogenation unit 3-2 is whole hydrogenation catalyst GHT-22; The volume space velocity of described hydrogenation unit 3-2 is than being 2.5h
-1Hydrogen/oil volume ratio is 300; Service temperature is 285 ℃, and working pressure is 2.5MPa (cutting off); The oily flow with 1.6 ten thousand tons/year of described heavy petrol extraction enters hydrogenation unit 3-3 and carries out hydrotreatment, and the catalyzer among the described hydrogenation unit 3-3 is whole hydrogenation catalyst GHT-22; The volume space velocity of described hydrogenation unit 3-3 is than being 2.5h
-1Hydrogen/oil volume ratio is 300; Service temperature is 270 ℃, and working pressure is 2.5MPa (cutting off); Described heavy petrol hydrogenation is raffinated oil and is expected extraction with 3.9 ten thousand tons/year flow as high-quality ethylene or reformation; Described heavy petrol hydrogenation is extracted oily flow with 1.6 ten thousand tons/year out and is mixed the back with described hydrogenation petroleum naphtha as the blended gasoline extraction.
The boiling range of gained blended gasoline is 30-185 ℃, and sulphur content is 25.2ppm, and mercaptans content is less than 1.0ppm (trace can detect), and olefin(e) centent is that 19.4% (v), the diolefine trace can not detect; Aromaticity content is that 20.9% (v), octane value (RON) is 94.3, and density is 718.1 kilograms/meter
3, produced quantity is 6.1 ten thousand tons/year.
The boiling range of the gained high-quality ethylene or the material of reforming is 110-185 ℃, containing sulphur content is trace, can not detect, mercaptans content is not less than 1.0ppm (trace can detect), olefin(e) centent is a trace, can not detect, bromine index (bromine valency) 25 (0.025), aromaticity content are 2.4% (v), octane value (RON) is 74.1, and density is 749.3 kilograms/meter
3, produced quantity is 3.9 ten thousand tons/year.
Selective hydrogenation catalyst GHT-20 among the described hydrogenation unit 3-1, and the physico-chemical property of the whole hydrogenation catalyst GHT-22 in other hydrogenation unit and measuring method are identical with embodiment 1.
Claims (1)
1, a kind of hydrogenation after component oil refining hydrocarbon recombination prepares the system of premium-type gasoline, it is characterized in that: comprise Distallation systm, and extraction system and hydrogenation unit, described Distallation systm top is connected with the petroleum naphtha hydrogenation unit by pipeline; Described Distallation systm bottom is connected with described extraction system by pipeline; Described extraction system top is connected with the hydrogenation unit of raffinating oil by pipeline, and described extraction system bottom is connected with the oily hydrogenation unit of extraction by pipeline; The oily hydrogenation unit of described extraction is connected by the tip line of pipeline with described petroleum naphtha hydrogenation unit.
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| CN (1) | CN201334459Y (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101475835B (en) * | 2009-01-22 | 2012-09-05 | 北京金伟晖工程技术有限公司 | System and method for preparing high quality petrol by hydrogenation after component oil refining hydrocarbon recombination |
-
2009
- 2009-01-22 CN CNU2009201054060U patent/CN201334459Y/en not_active Expired - Lifetime
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101475835B (en) * | 2009-01-22 | 2012-09-05 | 北京金伟晖工程技术有限公司 | System and method for preparing high quality petrol by hydrogenation after component oil refining hydrocarbon recombination |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20091028 Effective date of abandoning: 20090122 |