CN201154953Y - System for preparing high quality gasoline by catalytic hydrocarbon recombination - Google Patents
System for preparing high quality gasoline by catalytic hydrocarbon recombination Download PDFInfo
- Publication number
- CN201154953Y CN201154953Y CNU2007203020924U CN200720302092U CN201154953Y CN 201154953 Y CN201154953 Y CN 201154953Y CN U2007203020924 U CNU2007203020924 U CN U2007203020924U CN 200720302092 U CN200720302092 U CN 200720302092U CN 201154953 Y CN201154953 Y CN 201154953Y
- Authority
- CN
- China
- Prior art keywords
- gasoline
- pipeline
- content
- extraction
- extraction system
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model discloses a processing system for preparing high-quality gasoline by catalyzing hydrocarbon recombination, which comprises a distillation device and an extraction system and is characterized in that the upper part of the distillation device is connected with a hydrogenation unit by a light gasoline pipeline; the lower part of the distillation device is connected with the extraction system by a heavy gasoline pipeline; the upper part of the extraction unit produces products by pipelines directly, and the lower part of the extraction system is connected with the light gasoline pipeline after hydrotreating by the pipelines. Compared with the prior art, the processing system for preparing high-quality gasoline by catalyzing hydrocarbon recombination has the advantages of reducing the amount of a catalyst greatly and having an obvious effects of sulfur reduction and alkene reduction by adopting specific catalyst and parameter for light gasoline.
Description
Technical field
The utility model relates to a kind of system of catalyzing hydrocarbon for recombinant production of high-quality 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).
Therefore, provide the treatment system of the high blended gasoline of a kind of low-cost preparation low sulfur content, low olefin-content and octane value (RON) just to become the technical barrier that this technical field is badly in need of solution.
Summary of the invention
The purpose of this utility model provides a kind of catalytic hydrocarbon recombination system of gasoline of low-cost preparation low sulfur content, low olefin-content and boosting of octane rating (RON).
For achieving the above object, the utility model is taked following technical scheme:
A kind of system of catalyzing hydrocarbon for recombinant production of high-quality gasoline comprises water distilling apparatus; It is characterized in that: described water distilling apparatus top is connected with hydrogenation unit by the petroleum naphtha pipeline; Described water distilling apparatus bottom is connected with extraction system by the heavy petrol pipeline; Described extraction system top is by the direct extraction product of pipeline, described extraction system bottom by pipeline with pass through hydrotreatment after the petroleum naphtha pipeline be connected.
A kind of method of catalyzing hydrocarbon for recombinant production of high-quality gasoline, its step is as follows: stable gasoline is added water distilling apparatus carry out fractionation, cutting fractionates out petroleum naphtha and heavy petrol; Described petroleum naphtha enters hydrogenation unit by water distilling apparatus top and carries out hydrogenation; Described heavy petrol carries out extracting and separating at extraction system, isolates aromatic hydrocarbons and raffinates oil; Described aromatic hydrocarbons uses described raffinating oil as the direct extraction of chemical industry light oil by pipeline and the petroleum naphtha mediation through hydrotreatment.
A kind of preferred version is characterized in that: the tower top temperature of described water distilling apparatus is 100～110 ℃, and column bottom temperature is 206～226 ℃; 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 ℃～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 105 ℃, and column bottom temperature is 216 ℃; 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 ℃～100 ℃; The boiling range of described heavy petrol is controlled at 100 ℃～205 ℃.
A kind of preferred version is characterized in that: the catalyzer in the described petroleum naphtha hydrogenation unit is selective hydrogenation catalyst GHT-20; The volume space velocity of described petroleum naphtha hydrogenation unit is than being 2-4; Hydrogen/oil volume ratio is 250～350; Service temperature is 240～260 ℃, and working pressure is 1.4～1.6MPa (cutting off).
A kind of preferred version is characterized in that: the physico-chemical property of the selective hydrogenation catalyst GHT-20 in the described petroleum naphtha hydrogenation unit is as shown in the table:
| Index name | Unit | Index |
| 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 0O | m％ | 0.16 |
The used water distilling apparatus of the utility model is that the patent No. is a disclosed Distallation systm in the Chinese invention patent of 03148181.7 " catalytic hydrocarbon reorganization treatment process ".It is disclosed extraction system in 200310103541.9 and 200310103540.4 that described extraction system uses the patent No., comprises solvent recuperation and water wash system.
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 amount of the catalyzer of front-end hydrogenation (carrying out hydrotreatment before stable gasoline enters water distilling apparatus) usefulness is big, and can only reduce the amount of diene and mercaptan; The advantage of the catalytic hydrocarbon recombinant processing system of preparation low sulfur content of the present utility model and gasoline with low olefine content is: at first, owing to carry out hydrotreatment at petroleum naphtha specially, the amount of catalyst system therefor significantly reduces; Secondly, at petroleum naphtha, the amount of catalyst system therefor is much smaller, in addition, can reduce the content of monoene and diene, not only reduces the content of mercaptan, can also reduce total sulphur content; At last, specific catalyst and parameter are adopted in selective hydrogenation, mainly are mercaptan removal, solve alkene and diene problem, and effect is obvious.
The utility model is specially adapted to the processing of the stable gasoline of the high diene of low-sulfur.
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 schematic flow sheet of the utility model embodiment 1.
Embodiment
Embodiment 1
As shown in Figure 1, be the schematic flow sheet of the utility model embodiment.With boiling range is 30-205 ℃, sulphur content is 85ppm, mercaptans content is 15ppm, olefin(e) centent is 25% (v), diene content is 0.1% (v), aromaticity content is 13% (v), octane value (RON) is 87, density is that 728 kilograms/meter 3 stable gasoline (catalytic gasoline) cuts fractionation with 100,000 tons/year flow in distillation tower 1, the tower top temperature of distillation tower 1 is 105 ℃, column bottom temperature is 216 ℃, and tower top pressure is 0.2MPa (cutting off), and tower bottom pressure is 0.25MPa (cutting off), obtain petroleum naphtha and heavy petrol respectively, described petroleum naphtha (boiling range is 30-100 ℃) steams by distillation tower 1 top, and its total amount of steaming is 50,000 tons/year, enters hydrogenation unit 3 hydrotreatments then; Catalyzer in the described hydrogenation unit 3 is selective hydrogenation catalyst GHT-20, and the volume space velocity ratio of described petroleum naphtha hydrogenation unit is 4; Hydrogen/oil volume ratio is 300; Service temperature is 250 ℃, and working pressure is 1.5MPa (cutting off) (selective hydrogenation); Described heavy petrol (the gold-plating journey is 100-205 ℃) enters extracting and separating in the heavy petrol extraction system 2 with 50,000 tons/year flows, isolates aromatic hydrocarbons and raffinates oil; Solvent for use is a tetramethylene sulfone in the described extraction system 2, and extraction temperature is 120 ℃, and solvent ratio (solvent/charging) is 4.0 (quality), and the washing of raffinating oil is than being 0.2 (quality), and the solvent recuperation temperature is 175 ℃, and solvent recuperation pressure is 0.065MPa (cutting off); Described aromatic hydrocarbons is in harmonious proportion with 1.1 ten thousand tons/year flow and the petroleum naphtha behind the described hydrogenation, described raffinating oil with 3.9 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 102.8ppm, and mercaptans content is 4.3ppm, olefin(e) centent is 17.9%, and (v), diene content is 0.05% (v), aromaticity content is 20.0% (v), octane value (RON) is 91.8, and density is 700.6 kilograms/meter
3, produced quantity is 6.1 ten thousand tons/year.
The boiling range of gained chemical industry light oil is 100-205 ℃, and sulphur content is 29.0ppm, and mercaptans content is 1.0ppm, olefin(e) centent is 28.2%, and (v), diene content is that (v), aromaticity content is 3.0% (v) less than 0.01%, octane value (RON) is 78.5, and density is 775.5 kilograms/meter
3, produced quantity is 3.9 ten thousand tons/year.
The physico-chemical property of described selective hydrogenation catalyst GHT-20 is as shown in table 1 below:
Table 1
| Index name | Unit | Index |
| Outward appearance | The grey trilobal cross | |
| Specification | mm | Φ1.7 |
| Intensity | N/cm | 170 |
| Bulk density | g/ml | 0.70 |
| Specific surface | m 2/g | 180 |
| Pore volume | ml/g | 0.55 |
| WO 3 | m％ | 6.6 |
| NiO | m％ | 2.1 |
| C 0O | m％ | 0.16 |
The used measuring method of the utility model is:
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: 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 |
Claims (1)
1, a kind of system of catalyzing hydrocarbon for recombinant production of high-quality gasoline comprises water distilling apparatus and extraction system; It is characterized in that: described water distilling apparatus top is connected with hydrogenation unit by the petroleum naphtha pipeline; Described water distilling apparatus bottom is connected with extraction system by the heavy petrol pipeline; Described extraction plant top is by the direct extraction product of pipeline, described extraction system bottom by pipeline with pass through hydrotreatment after the petroleum naphtha pipeline be connected.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007203020924U CN201154953Y (en) | 2007-11-09 | 2007-11-09 | System for preparing high quality gasoline by catalytic hydrocarbon recombination |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007203020924U CN201154953Y (en) | 2007-11-09 | 2007-11-09 | System for preparing high quality gasoline by catalytic hydrocarbon recombination |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201154953Y true CN201154953Y (en) | 2008-11-26 |
Family
ID=40102739
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNU2007203020924U Expired - Lifetime CN201154953Y (en) | 2007-11-09 | 2007-11-09 | System for preparing high quality gasoline by catalytic hydrocarbon recombination |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201154953Y (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101429442A (en) * | 2007-11-09 | 2009-05-13 | 丁冉峰 | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline |
| WO2009067885A1 (en) * | 2007-11-09 | 2009-06-04 | Ranfeng Ding | A system and process for producing high quality gasoline by catalytic hydrocarbon recombination |
| WO2009094934A1 (en) * | 2008-01-29 | 2009-08-06 | Beijing Grand Golden-Bright Engineering & Technologies Co., Ltd | A system and a process for producing high quality gasoline |
| WO2010083642A1 (en) * | 2009-01-21 | 2010-07-29 | 北京金伟晖工程技术有限公司 | System and process for producing high quality gasoline by recombination and subsequent hydrogenation of catalytic hydrocarbons |
-
2007
- 2007-11-09 CN CNU2007203020924U patent/CN201154953Y/en not_active Expired - Lifetime
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101429442A (en) * | 2007-11-09 | 2009-05-13 | 丁冉峰 | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline |
| WO2009067885A1 (en) * | 2007-11-09 | 2009-06-04 | Ranfeng Ding | A system and process for producing high quality gasoline by catalytic hydrocarbon recombination |
| US8524043B2 (en) | 2007-11-09 | 2013-09-03 | Ranfeng Ding | System for producing high quality gasoline by catalytic hydrocarbon recombination |
| WO2009094934A1 (en) * | 2008-01-29 | 2009-08-06 | Beijing Grand Golden-Bright Engineering & Technologies Co., Ltd | A system and a process for producing high quality gasoline |
| WO2010083642A1 (en) * | 2009-01-21 | 2010-07-29 | 北京金伟晖工程技术有限公司 | System and process for producing high quality gasoline by recombination and subsequent hydrogenation of catalytic hydrocarbons |
| US8419930B2 (en) | 2009-01-21 | 2013-04-16 | Beijing Grand Golden-Bright Engineering & Technologies Co., Ltd. | System for preparing high-quality gasoline through component oil refining hydrocarbon recombination hydrogenation and method thereof |
| EA019489B1 (en) * | 2009-01-21 | 2014-04-30 | Бейджин Гранд Голден-Брайт Инджиниринг Энд Текнолоджиз Ко., Лтд. | System and process for producing high quality gasoline by hydrogenation and recombination of oil refining hydrocarbon component |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN201186917Y (en) | System for preparing high-quality petrol | |
| CN201158633Y (en) | System for producing high quality gasoline by catalyzing hydrocarbon regrouping | |
| CN201154953Y (en) | System for preparing high quality gasoline by catalytic hydrocarbon recombination | |
| CN101429442B (en) | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline | |
| CN201144231Y (en) | System for preparing high-quality petrol by recombination of catalytic hydrocarbon | |
| CN201144229Y (en) | System for preparing high-quality petrol by recombination of catalytic hydrocarbon | |
| CN201154954Y (en) | System for preparing high quality gasoline by catalytic hydrocarbon recombination | |
| US8419930B2 (en) | System for preparing high-quality gasoline through component oil refining hydrocarbon recombination hydrogenation and method thereof | |
| CN201144228Y (en) | System for preparing high-quality petrol by recombination of catalytic hydrocarbon | |
| CN101429443B (en) | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline | |
| CN101497806B (en) | System and method for preparing high quality petrol | |
| CN101475833B (en) | Method for preparing high quality petrol by hydrogenation after component oil refining hydrocarbon recombination | |
| CN201144230Y (en) | System for preparing high-quality petrol by recombination of catalytic hydrocarbon | |
| CN201334457Y (en) | System for preparing high-quality gasoline by component oil refining, hydrocarbon recombination and post-hydrogenation | |
| CN201334459Y (en) | System for preparing high-quality gasoline by component oil refining, hydrocarbon recombination and post-hydrogenation | |
| CN201334458Y (en) | System for preparing high-quality petrol and diesel oil by component oil refining, hydrocarbon recombination and post-hydrogenation | |
| CN101475835B (en) | System and method for preparing high quality petrol by hydrogenation after component oil refining hydrocarbon recombination | |
| CN101497808B (en) | System and method for preparing high quality petrol | |
| CN101475834B (en) | System and method for preparing high quality gasoline and diesel by hydrogenation after component oil refining hydrocarbon recombination | |
| CA2853924A1 (en) | Pretreatment of fcc naphthas and selective hydrotreating | |
| CN101429447B (en) | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline | |
| CN201186916Y (en) | System for preparing high-quality petrol by recombination of catalytic hydrocarbon | |
| CN101429448B (en) | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline | |
| CN101429446B (en) | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline | |
| CN101497809B (en) | Method for preparing high quality petrol |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Assignee: Tianjin Jin Weihui biological Petrochemical Co., Ltd. Assignor: Ding Ranfeng Contract record no.: 2011120000270 Denomination of utility model: System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline Granted publication date: 20081126 License type: Exclusive License Record date: 20111114 |
|
| AV01 | Patent right actively abandoned |
Granted publication date: 20081126 Effective date of abandoning: 20071109 |
|
| RGAV | Abandon patent right to avoid regrant |