CN101497807B - System and method for preparing high quality petrol - Google Patents
System and method for preparing high quality petrol Download PDFInfo
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- CN101497807B CN101497807B CN 200810005206 CN200810005206A CN101497807B CN 101497807 B CN101497807 B CN 101497807B CN 200810005206 CN200810005206 CN 200810005206 CN 200810005206 A CN200810005206 A CN 200810005206A CN 101497807 B CN101497807 B CN 101497807B
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Abstract
The invention discloses a device 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 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 the hydrogenation unit by a pipeline; the hydrogenation unit is connected with a heavy petrol extraction system by a pipeline; the upper part of the heavy petrol extraction directly extracts the product, and the lower part of the heavy petrol extraction system is connected with a pipeline at the upper part of the light petrol extraction system by a pipeline. The device 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 Apparatus for () and method therefor 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 the products such as net gas, liquefied gas tank, 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 stricter along with environmental requirement, the standard of gasoline, diesel oil improves constantly, existing catalytic hydrocarbon is showed following deficiency through the processing and treating method of separation column fractionation: 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 producing, the ratio of gasoline and market is not mated, 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 recombinant processing method " provides a kind of catalytic hydrocarbon recombinant processing method, 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 that 0.05% (wt), olefin(e) centent are not more than 35% (v), benzene content is not more than 2.5% (v), and 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 is not more than 30% (v), and 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 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 large 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 large and the characteristics of residuum coking are arranged, the refinery catalytic gasoline sulphur content of processing low-sulfur (sulfur-bearing 0.3%) crude oil is 200ppm approximately, 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 large, working cost is high, existing refinery condition is limited and impossible large-scale application, and 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, not only energy consumption is high, and expense is also high.
Therefore, provide the treatment facility 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 a kind of low cost, less energy-consumption, pollution-free preparation low sulfur content, low olefin-content and improves the equipment of the gasoline of octane value (RON).
For achieving the above object, the present invention takes following technical scheme:
A kind of equipment 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 described hydrogenation unit by pipeline; Described hydrogenation unit 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 by the pipeline of pipeline with described petroleum naphtha extraction system top.
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 hydrotreated 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 raffinating oil as the direct extraction of blended gasoline, described extraction oil enter by pipeline and enter the heavy petrol extraction system after the hydrogenation device for treatment again and carry out extracting and separating; Described heavy petrol also enters described heavy petrol extraction system after by hydrogenation device for treatment and carries out extracting and separating; Carry out isolating extraction oil and raffinating oil after the extracting and separating through described heavy petrol extraction system; Described extraction oil is raffinated oil by pipeline and described petroleum naphtha and is in harmonious proportion afterwards extraction, described raffinating oil as the high-quality ethylene extraction.
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 189～192 ℃; The tower top pressure of described water distilling apparatus is 0.11～0.28MPa (absolutely), and tower bottom pressure is 0.12～0.30MPa (absolutely); The boiling range of described petroleum naphtha is controlled at 30 ℃～100 ℃; The boiling range of described heavy petrol is controlled at 100 ℃～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 190 ℃; The tower top pressure of described water distilling apparatus is 0.2MPa (absolutely), and tower bottom pressure is 0.25MPa (absolutely).
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 ratio of described hydrogenation unit is 2.5; Hydrogen/oil volume ratio is 200; Service temperature is 285 ℃, and working pressure is 1.5MPa (absolutely).
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.
| 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 0O | m％ | 0.15 |
[0020]
| Na 2O | m％ | ＜0.09 |
| Fe 2O 3 | m％ | ＜0.06 |
| SiO 2 | m％ | ＜0.60 |
| Carrier | m％ | 82.4 |
Petroleum naphtha described in the present invention and heavy petrol extraction system can share a solvent recovering system, also can use respectively different solvent recovering systems.
Petroleum naphtha of the present invention, stable gasoline and hydrotreated 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 disclosed Distallation systm in the Chinese invention patent of 03148181.7 " catalytic hydrocarbon recombinant processing method ".Used extraction system is that the patent No. is 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 advantage of the Apparatus for () and method therefor of preparation low sulfur content of the present invention and gasoline with low olefine content is: compare with the alkali cleaning mode, Apparatus and method for of the present invention can not only deolefination, can also mercaptan removal, and diene; Compare with the petroleum naphtha hydrogenation, hydrogenation unit of the present invention is only oily for extracting out, small scale, and cost is low; At last, the diversification of feedstock that the present invention processes is not only processed stable gasoline, can also process the mixture of stable gasoline and petroleum naphtha and hydrotreated coker gasoline.Also contain in petroleum naphtha and the hydrotreated coker gasoline and extract oil out, high-quality ethylene 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.
Embodiment
As shown in Figure 1, be the schematic flow sheet of the embodiment of the invention 1.Be 30-205 ℃ with boiling range, sulphur content is 100ppm, and mercaptans content is 5ppm, and olefin(e) centent is 30% (v), and diene content is 0.1% (v), and aromaticity content is 15% (v), and octane value (RON) is 89, and density is 728 kg/ms
3Stable gasoline (catalytic gasoline) in distillation tower 1, cut fractionation with 60,000 ton/years flow, the tower top temperature of distillation tower 1 is 82 ℃, column bottom temperature is 190 ℃, tower top pressure is 0.2MPa (absolutely), tower bottom pressure is 0.25MPa (absolutely), obtain respectively petroleum naphtha and heavy petrol, described petroleum naphtha (boiling range is 30-100 ℃) steams by distillation tower 1 top, steaming that it is total is 2.4 ten thousand ton/years, then enter extracting and separating among the petroleum naphtha extraction system 2-1, isolate and extract oil out and raffinate oil; Solvent for use is tetramethylene sulfone among the described extraction system 2-1, extraction temperature is 70 ℃, and solvent ratio (solvent/charging) is 2.0 (quality), and the washing of raffinating oil is than being 0.2 (quality), the solvent recuperation temperature is 153 ℃, and solvent recuperation pressure is 0.112MPa (absolutely); Described petroleum naphtha is extracted out and is entered extracting and separating among the heavy petrol extraction system 2-2 after oily flow with 0.48 ten thousand ton/year enters 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 (absolutely); Described petroleum naphtha is raffinated oil with 1.92 ten thousand ton/years flow as the blended gasoline extraction.Described heavy petrol (boiling range is 100-205 ℃) enters extracting and separating among the heavy petrol extraction system 2-2 with 3.6 ten thousand ton/years flows, isolates heavy petrol extraction oil and heavy petrol and raffinates oil; Solvent for use is tetramethylene sulfone among the described extraction system 2-2, extraction temperature is 98 ℃, 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 157 ℃, and solvent recuperation pressure is 0.112MPa (absolutely); Described heavy petrol is raffinated oil with 2.78 ten thousand ton/years flow as the high-quality ethylene extraction; Described heavy petrol extraction oil is raffinated oil with described petroleum naphtha with 1.3 ten thousand ton/years flow and is mixed afterwards as the blended gasoline extraction.
The boiling range of gained blended gasoline is 30-205 ℃, and sulphur content is 14.5ppm, and mercaptans content is less than 1.0ppm (trace, inspection does not measure), and olefin(e) centent is 21.7% (v), and diene content is lower than 0.01% (v) (trace, inspection does not measure); Aromaticity content is 26.5% (v), and octane value (RON) is 95.7, and density is 735.0 kg/ms
3, produced quantity is 3.22 ten thousand ton/years.
The boiling range of gained high-quality ethylene is 100-205 ℃, sulphur content is 5.0ppm, mercaptans content is less than 1.0ppm (trace, inspection does not measure), olefin(e) centent is 1.2% (v), diene content is less than 0.01% (v) (trace, inspection does not measure), aromaticity content is 2.0% (v), and octane value (RON) is 73.8, and density is 720.0 kg/ms
3, produced quantity is 2.78 ten thousand ton/years.
The physico-chemical property of whole hydrogenation catalyst GHT-22 in the described hydrogenation unit is as shown in the table.
| 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 0O | 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 present invention is (lower same):
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 |
[0048]
| Surface-area | Low-temperature nitrogen adsorption method | 2400 type adsorption instruments |
| Pore volume | Mercury penetration method | Auto Pore II 9200 |
| Intensity | The crush strength assay method | DLII type intelligence detector for strength of particles |
| Bulk density | Weighing method |
Embodiment 2
As shown in Figure 2, be the schematic flow sheet of the embodiment of the invention 2.Be 30-205 ℃ with boiling range, sulphur content is 800ppm, and mercaptans content is 9ppm, and olefin(e) centent is 36% (v), and diene content is 0.9% (v), and aromaticity content is 17% (v), and octane value (RON) is 91, and density is 731 kg/ms
3Stable gasoline (catalytic gasoline) in distillation tower 1, cut fractionation with 60,000 ton/years flow; Simultaneously, it is 30-205 ℃ with boiling range, sulphur content is 200ppm, and mercaptans content is 1ppm, and olefin(e) centent is less than 0.1% (v) (trace, inspection does not measure), diene content is less than 0.01% (v) (trace, inspection does not measure), and aromaticity content is 8% (v), octane value (RON) is 82, and density is 732 kg/ms
3Petroleum naphtha in distillation tower 1, cut fractionation with 20,000 ton/years flow; Meanwhile, it is 30-205 ℃ with boiling range, sulphur content is 150ppm, mercaptans content is 1ppm, and olefin(e) centent is 6% (v), and diene content is less than 0.01% (v) (trace, inspection does not measure), aromaticity content is 10% (v), and octane value (RON) is 79, and density is 721 kg/ms
3Hydrotreated coker gasoline in distillation tower 1, cut fractionation with 20,000 ton/years flow; The tower top temperature of distillation tower 1 is 82 ℃, column bottom temperature is 190 ℃, tower top pressure is 0.2MPa (absolutely), tower bottom pressure is 0.25MPa (absolutely), obtain respectively petroleum naphtha and heavy petrol, described petroleum naphtha (boiling range is 30-100 ℃) steams by distillation tower 1 top, and its total amount of steaming is 4.5 ten thousand ton/years, then enter extracting and separating among the petroleum naphtha extraction system 2-1, isolate and extract oil out and raffinate oil; Solvent for use is tetramethylene sulfone among the described extraction system 2-1, extraction temperature is 70 ℃, and solvent ratio (solvent/charging) is 2.0 (quality), and the washing of raffinating oil is than being 0.2 (quality), the solvent recuperation temperature is 153 ℃, and solvent recuperation pressure is 0.112MPa (absolutely); Described petroleum naphtha is extracted out and is entered extracting and separating among the heavy petrol extraction system 2-2 after oily flow with 1.26 ten thousand ton/years enters 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 (absolutely); Described petroleum naphtha is raffinated oil with 3.24 ten thousand ton/years flow as the blended gasoline extraction.Described heavy petrol (boiling range is 100-205 ℃) enters extracting and separating among the heavy petrol extraction system 2-2 with 5.5 ten thousand ton/years flows, isolates heavy petrol extraction oil and heavy petrol and raffinates oil; Solvent for use is tetramethylene sulfone among the described extraction system 2-2, extraction temperature is 98 ℃, 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 157 ℃, and solvent recuperation pressure is 0.112MPa (absolutely); Described heavy petrol is raffinated oil with 4.87 ten thousand ton/years flow as the high-quality ethylene extraction; Described heavy petrol extraction oil is raffinated oil with described petroleum naphtha with 1.89 ten thousand ton/years flow and is mixed afterwards as the blended gasoline extraction.
The boiling range of gained blended gasoline is 30-205 ℃, and sulphur content is 36.5ppm, and mercaptans content 1.26ppm, olefin(e) centent are 13.4% (v), and diene content is lower than 0.01% (v) (trace detects not out); Aromaticity content is 23.2% (v), and octane value (RON) is 95.8, and density is 701.4 kg/ms
3, produced quantity is 5.13 ten thousand ton/years.
The boiling range of gained high-quality ethylene is 100-205 ℃, sulphur content is 6.0ppm, mercaptans content is less than 1.0ppm (trace, inspection does not measure), olefin(e) centent is 1.2% (v), diene content is less than 0.01% (v) (trace, inspection does not measure), aromaticity content is 3.0% (v), and octane value (RON) is 70.5, and density is 761.0 kg/ms
3, produced quantity is 4.87 ten thousand ton/years.
The physico-chemical property of whole hydrogenation catalyst GHT-22 in the described hydrogenation unit 3 is as shown in the table.
| 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 0O | m％ | 0.15 |
| Na 2O | m％ | ＜0.09 |
| Fe 2O 3 | m％ | ＜0.06 |
| SiO 2 | m％ | ＜0.60 |
| Carrier | m％ | 82.4 |
Claims (5)
1. an equipment 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 described hydrogenation unit by pipeline; Described hydrogenation unit 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 by the pipeline of pipeline with described petroleum naphtha extraction system top.
2. 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 hydrotreated 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 raffinating oil as the direct extraction of blended gasoline, described extraction oil enter by pipeline and enter the heavy petrol extraction system after the hydrogenation device for treatment again and carry out extracting and separating; Described heavy petrol also enters described heavy petrol extraction system after by hydrogenation device for treatment and carries out extracting and separating; Carry out isolating after the extracting and separating that heavy petrol is extracted oil out and heavy petrol is raffinated oil through described heavy petrol extraction system; Described heavy petrol is extracted oil out and is raffinated oil by pipeline and described petroleum naphtha and mix afterwards as the blended gasoline extraction, and described heavy petrol is raffinated oil as the high-quality ethylene extraction.
3. the method for preparing premium-type gasoline according to claim 2, it is characterized in that: the tower top temperature of described water distilling apparatus is 77～86 ℃, column bottom temperature is 189～192 ℃; The tower top pressure of described water distilling apparatus is 0.11～0.28MPa bar absolute pressure, and tower bottom pressure is 0.12～0.30MPa bar absolute pressure; The boiling range of described petroleum naphtha is controlled at 30 ℃～100 ℃; The boiling range of described heavy petrol is controlled at 100 ℃～205 ℃.
4. the method for preparing premium-type gasoline according to claim 3, it is characterized in that: the tower top temperature of described water distilling apparatus is 82 ℃, column bottom temperature is 190 ℃; The tower top pressure of described water distilling apparatus is the 0.2MPa bar absolute pressure, and tower bottom pressure is the 0.25MPa bar absolute pressure.
5. the method for preparing premium-type gasoline according to claim 4, it 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 2.5h
-Hydrogen/oil volume ratio is 200; Service temperature is 285 ℃, and working pressure is the 1.5MPa bar absolute pressure; The physico-chemical property of whole hydrogenation catalyst GHT-22 in the described hydrogenation unit is as shown in the table
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200810005206 CN101497807B (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 200810005206 CN101497807B (en) | 2008-01-29 | 2008-01-29 | System and method for preparing high quality petrol |
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| CN101497807A CN101497807A (en) | 2009-08-05 |
| CN101497807B true CN101497807B (en) | 2013-04-10 |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1470607A (en) * | 2003-07-04 | 2004-01-28 | 北京金伟晖工程技术有限公司 | Catalytic hydrocarbon reforming treatment method |
| CN1511925A (en) * | 2002-12-31 | 2004-07-14 | 中国石油化工股份有限公司齐鲁分公司 | Method for reoving mercaptan from gasoline |
| DE69827657T2 (en) * | 1997-09-03 | 2005-03-31 | GTC Technology, Inc., Houston | METHOD FOR DISCONNECTING FLAVORS |
-
2008
- 2008-01-29 CN CN 200810005206 patent/CN101497807B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE69827657T2 (en) * | 1997-09-03 | 2005-03-31 | GTC Technology, Inc., Houston | METHOD FOR DISCONNECTING FLAVORS |
| CN1511925A (en) * | 2002-12-31 | 2004-07-14 | 中国石油化工股份有限公司齐鲁分公司 | Method for reoving mercaptan from gasoline |
| CN1470607A (en) * | 2003-07-04 | 2004-01-28 | 北京金伟晖工程技术有限公司 | Catalytic hydrocarbon reforming treatment method |
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| CN101497807A (en) | 2009-08-05 |
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