CN201144228Y - System for preparing high-quality petrol by recombination of catalytic hydrocarbon - Google Patents
System for preparing high-quality petrol by recombination of catalytic hydrocarbon Download PDFInfo
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- CN201144228Y CN201144228Y CNU2007203020939U CN200720302093U CN201144228Y CN 201144228 Y CN201144228 Y CN 201144228Y CN U2007203020939 U CNU2007203020939 U CN U2007203020939U CN 200720302093 U CN200720302093 U CN 200720302093U CN 201144228 Y CN201144228 Y CN 201144228Y
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Abstract
The utility model discloses a high-quality gasoline preparation system through recombination of catalytic hydrocarbon, which consists of a distillation unit and an extraction system, and is characterized in that the hydrogenation device is connected with the distillation unit; the upper and the lower parts of the distillation unit are respectively provided with a light gasoline pipeline and a heavy gasoline pipeline; the middle part of the distillation unit is provided with an intermediate gasoline pipeline; the intermediate and heavy gasoline is injected into the extraction system via the pipelines; the upper part of the extraction system directly extracts the high-quality ethylene material products or chemical light oil products; the heavy gasoline pipeline is directly connected with another extraction system or directly extracts the oil product as the low-freezing diesel oil. Compared with the prior art, the utility model has the advantages that hydrogen is fed first and then the gases are recombined, and the content of sulfur in the mixed gasoline is lower, the content of olefin is lower, and the cost is very low.
Description
Technical field
The utility model relates to a kind of catalytic hydrocarbon recombinant processing system, particularly 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.
The patent No. is the Chinese invention patent of 03148181.7 " catalytic hydrocarbon reorganization treatment process ", and the patent No. is respectively 200310103541.9 and 200310103540.4 and discloses it and improve patent, but all do not mention the problem of how to fall sulphur and falling alkene in these 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 state III gasoline standard requirement sulphur content that is about to implement in 2010 is not more than 0.015% (wt), alkene is not more than 30% (v), benzene content is not more than 1% (v), for most refinery, must be in the face of higher state IV standards requirement, promptly sulphur content ≯ 0.005% (wt), alkene ≯ 25% are (v) or lower.The quality of gasoline solution must be considered the transition from state III to state IV standards, and programme should be disposable according to state 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, upgrade sulphur to be solved and alkene of quality of gasoline mainly is the problem that solves catalytic gasoline.
It is generally acknowledged, the 5-10% of total sulfur will enter gasoline 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, how altogether, provide a kind of treatment system of blended gasoline of low-cost preparation low sulfur content, low olefin-content and high-octane rating (RON) and method thereof just to become this technical field and be badly in need of the technical barrier that solves hydrogenation and catalytic hydrocarbon recombination nodule.
Summary of the invention
The purpose of this utility model provides a kind of catalytic hydrocarbon recombination system of low-cost 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 system of catalyzing hydrocarbon for recombinant production of high-quality gasoline comprises water distilling apparatus and extraction system, it is characterized in that: hydrogenation unit is connected with described water distilling apparatus, and the top of described water distilling apparatus is provided with the petroleum naphtha pipeline; Described water distilling apparatus bottom is provided with the heavy petrol pipeline; The middle part of described water distilling apparatus is provided with middle medium gasoline pipeline; Medium gasoline pipeline is connected with an extraction system in described; The bottom of described extraction system is connected with the petroleum naphtha pipeline on water distilling apparatus top by pipeline; The top of described extraction system is by pipeline direct extraction product high-quality ethylene or chemical industry light oil; Described heavy petrol pipeline be connected with another extraction system or directly the extraction product as low-coagulation diesel oil; Described extraction system top is connected with the pipeline of raffinating oil after handling of described middle gasoline by pipeline, and the bottom of described extraction system is connected with the petroleum naphtha pipeline on water distilling apparatus top by pipeline.
A kind of method of catalyzing hydrocarbon for recombinant production of high-quality gasoline, its step is as follows: stable gasoline earlier by the hydrogenation unit hydrogenation, is entered water distilling apparatus then and carries out fractionation, and cutting fractionates out petroleum naphtha, middle gasoline and heavy petrol; Described petroleum naphtha steams by water distilling apparatus top; Described middle gasoline enters an extraction system by pipeline and carries out extracting and separating, isolates aromatic component and raffinates oil; The petroleum naphtha that described aromatic component steams by pipeline and water distilling apparatus top is in harmonious proportion and uses described raffinating oil as high-quality ethylene or chemical industry light oil; Described heavy petrol enters another extraction system by pipeline and carries out extracting and separating, isolates aromatic component and raffinates oil; The petroleum naphtha that described aromatic component steams by pipeline and water distilling apparatus top is in harmonious proportion and uses, and describedly raffinates oil or mixes with raffinating oil of middle gasoline afterwards as high-quality ethylene or chemical industry light oil by pipeline; Perhaps as the direct extraction of low-coagulation diesel oil.
A kind of preferred version is characterized in that: the tower top temperature of described water distilling apparatus is 80～90 ℃, and column bottom temperature is 218～238 ℃; 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 ℃～80 ℃; The boiling range of gasoline is controlled at 80 ℃～160 ℃ in described; The boiling range of described heavy petrol is controlled at 160 ℃～205 ℃.
A kind of preferred version is characterized in that: the tower top temperature of described water distilling apparatus is 80～90 ℃, and column bottom temperature is 218～238 ℃; 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 gasoline is controlled at 90 ℃～160 ℃ in described; The boiling range of described heavy petrol is controlled at 160 ℃～205 ℃.
A kind of preferred version is characterized in that: the catalyzer in the described hydrogenation unit is selective hydrogenation catalyst GHT-20; The volume space velocity of described hydrogenation unit is than being 2-4; Hydrogen/oil volume ratio is 250～350; Service temperature is 240～260 ℃, and working pressure is 0.6～1.5MPa (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 hydrogenation unit is as shown in table 1 below.
Table 1
| 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:
Compared with prior art, the advantage of the system of catalyzing hydrocarbon for recombinant production of high-quality gasoline of the present utility model is: first hydrogenation, and again through reorganization, the two combination, the sulphur content of gained blended gasoline is lower, and olefin(e) centent is also lower, and with low cost.
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.
Fig. 2 is the schematic flow sheet of the utility model embodiment 2.
Embodiment
Embodiment 1
As shown in Figure 1, be the schematic flow sheet of the utility model embodiment.With boiling range is 30-205 ℃, and sulphur content is 80ppm, and mercaptans content is 3ppm, and olefin(e) centent is 25%, and (v), diene content is 0.05% (v), aromaticity content is that 15% (v), octane value (RON) is 88, and density is 728,000 kilograms/meter
3Stable gasoline (catalytic gasoline) with 100,000 tons/year flow earlier through 3 hydrotreatments of front-end hydrogenation device, the catalyzer of adorning is selective hydrogenation catalyst GHT-20 in the described hydrogenation unit 3, the volume space velocity ratio of described hydrogenation unit 3 is 4; Hydrogen/oil volume ratio is 300; Service temperature is 250 ℃, and working pressure is 1.5MPa exhausted (selective hydrogenation); In distillation tower 1, cut fractionation then, the tower top temperature of distillation tower 1 is 85 ℃, column bottom temperature is 228 ℃, tower top pressure is 0.2MPa (cutting off), tower bottom pressure is 0.25MPa (cutting off), fractionation obtains petroleum naphtha, middle gasoline and heavy petrol respectively, and described petroleum naphtha (boiling range is 30-80 ℃) steams by distillation tower 1 top, and its amount of steaming is 40,000 tons/year; Carry out extracting and separating among the gasoline extraction system 2-1 during gasoline (boiling range is 80-160 ℃) enters by pipeline with 2.8 ten thousand tons/year flows in described, isolate aromatic component and raffinate oil; Solvent for use is a Tetraglycol 99 among the described extraction system 2-1, and extraction temperature is 125 ℃, and solvent ratio (solvent/charging) is 6.0 (quality), and the washing of raffinating oil is than being 0.2 (quality), and the solvent recuperation temperature is 172 ℃, and solvent recuperation pressure is 0.075MPa (cutting off); Described aromatic component is in harmonious proportion by the petroleum naphtha behind hydrogenation that pipeline and distillation tower 1 top steam with 0.6 ten thousand tons/year flow; Described raffinating oil with 2.2 ten thousand tons/year flow extraction, as high-quality ethylene; Described heavy petrol (boiling range is 160-205 ℃) enters extracting and separating among the heavy petrol extraction system 2-2 with 3.2 ten thousand tons/year flows by pipeline, isolates aromatic component and raffinates oil; Solvent for use is a Tetraglycol 99 among the described extraction system 2-2, and extraction temperature is 150 ℃, and solvent ratio (solvent/charging) is 8.0 (quality), and the washing of raffinating oil is than being 0.2 (quality), and the solvent recuperation temperature is 174 ℃, and solvent recuperation pressure is 0.075MPa (cutting off); Described aromatic component is in harmonious proportion with 0.8 ten thousand tons/year flow and described petroleum naphtha, described raffinate oil with 2.4 ten thousand tons/year flow with described in gasoline after raffinating oil after the extraction is mixed as high-quality ethylene.
The boiling range of gained blended gasoline is 30-205 ℃, and sulphur content is 49.56ppm, and mercaptans content is less than 1ppm, olefin(e) centent is 15.4%, and (v), diene content is that (v), aromaticity content is 26.5% (v) less than 0.01%, octane value (RON) is 95.8, and density is 703.1 thousand kilograms/meter
3, produced quantity is 5.4 ten thousand tons/year.
The boiling range of gained high-quality ethylene is 80-205 ℃, and sulphur content is 11.4ppm, and mercaptans content is less than 1ppm, olefin(e) centent is 22.8%, and (v), diene content is that (v), aromaticity content is 2.5% (v) less than 0.01%, octane value (RON) is 78.5, and density is 761.9 thousand kilograms/meter
3, produced quantity is 4.6 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 (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: 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 |
Embodiment 2
As shown in Figure 2, be the schematic flow sheet of the utility model embodiment.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 728,000 kilograms/meter
3Stable gasoline (catalytic gasoline) with 100,000 tons/year flow earlier through hydrogenation unit 3 hydrotreatments, the catalyzer of described hydrogenation unit 3 is selective hydrogenation catalyst GHT-20, the volume space velocity ratio of described hydrogenation unit 3 is 2; Hydrogen/oil volume ratio is 350; Service temperature is 260 ℃, and working pressure is 0.6MPa (cutting off) (selective hydrogenation); In distillation tower 1, cut fractionation then, the tower top temperature of distillation tower 1 is 86 ℃, column bottom temperature is 227 ℃, tower top pressure is that 0.2MPa is exhausted, tower bottom pressure is 0.25MPa (cutting off), fractionation obtains petroleum naphtha, middle gasoline and heavy petrol respectively, and described petroleum naphtha (boiling range is 30-90 ℃) steams by distillation tower 1 top, and its amount of steaming is 40,000 tons/year; Carry out extracting and separating among the gasoline extraction system 2-1 during gasoline (boiling range is 90-160 ℃) enters by pipeline with 2.7 ten thousand tons/year flows in described, isolate aromatic component and raffinate oil; Solvent for use is a N-Methyl pyrrolidone among the described extraction system 2-1, and extraction temperature is 75 ℃, and solvent ratio (solvent/charging) is 3.0 (quality), and the washing of raffinating oil is than being 0.2 (quality), and the solvent recuperation temperature is 161 ℃, and solvent recuperation pressure is that 0.086MPa is exhausted; Described aromatic component is in harmonious proportion by the petroleum naphtha behind hydrogenation that pipeline and distillation tower 1 top steam with 0.7 ten thousand tons/year flow; Described raffinating oil with 2.0 ten thousand tons/year flow extraction, as chemical industry light oil; Described heavy petrol (boiling range is 160-205 ℃) enters extracting and separating among the heavy petrol extraction system 2-2 with 3.3 ten thousand tons/year flows by pipeline, isolates aromatic component and raffinates oil; Solvent for use is a N-Methyl pyrrolidone among the described extraction system 2-2, and extraction temperature is 95 ℃, and solvent ratio (solvent/charging) is 4.0 (quality), and the washing of raffinating oil is than being 0.3 (quality), and the solvent recuperation temperature is 163 ℃, and solvent recuperation pressure is that 0.085MPa is exhausted; Described aromatic component is in harmonious proportion described raffinating oil with the direct extraction of 2.0 ten thousand tons/year flow as low-coagulation diesel oil with 1.3 ten thousand tons/year flow and described petroleum naphtha.
The boiling range of gained blended gasoline is 30-205 ℃, and sulphur content is 103.33ppm, and mercaptans content is less than 1ppm, olefin(e) centent is 14.8%, and (v), diene content is that (v), aromaticity content is 29.9% (v) less than 0.01%, octane value (RON) is 94.7, and density is 723.4 kilograms/meter
3, produced quantity is 6.0 ten thousand tons/year.
The boiling range of gained chemical industry light oil is 90-160 ℃, and sulphur content is 10.0ppm, and mercaptans content is less than 1ppm, olefin(e) centent is 22.5%, and (v), diene content is that (v), aromaticity content is 3.0% (v) less than 0.01%, octane value (RON) is 76.0, and density is 733.0 kilograms/meter
3, produced quantity is 2.0 ten thousand tons/year.
The boiling range of gained low-coagulation diesel oil is 160-205 ℃, and sulphur content is 80.0ppm, and mercaptans content is less than 1ppm, and olefin(e) centent is 23.0%, and (v), diene content is that (v), aromaticity content is that 3.0% (v), density is 747.5 kilograms/meter less than 0.01%
3, produced quantity is 2.0 ten thousand tons/year.
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: hydrogenation unit is connected with water distilling apparatus, and the top of described water distilling apparatus is provided with the petroleum naphtha pipeline; Described water distilling apparatus bottom is provided with the heavy petrol pipeline; The middle part of described water distilling apparatus is provided with middle medium gasoline pipeline; Medium gasoline pipeline is connected with an extraction system in described; The bottom of described extraction system is connected with the petroleum naphtha pipeline on water distilling apparatus top by pipeline; The top of described extraction system is by pipeline direct extraction product high-quality ethylene or chemical industry light oil; Described heavy petrol pipeline be connected with another extraction system or directly the extraction product as low-coagulation diesel oil; Described extraction system top is connected with the pipeline of raffinating oil after handling of described middle gasoline by pipeline, and the bottom of described extraction system is connected with the petroleum naphtha pipeline on water distilling apparatus top by pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007203020939U CN201144228Y (en) | 2007-11-09 | 2007-11-09 | System for preparing high-quality petrol by recombination of catalytic hydrocarbon |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007203020939U CN201144228Y (en) | 2007-11-09 | 2007-11-09 | System for preparing high-quality petrol by recombination of catalytic hydrocarbon |
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| CN201144228Y true CN201144228Y (en) | 2008-11-05 |
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| CNU2007203020939U Expired - Lifetime CN201144228Y (en) | 2007-11-09 | 2007-11-09 | System for preparing high-quality petrol by recombination of catalytic hydrocarbon |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101429443B (en) * | 2007-11-09 | 2012-08-22 | 丁冉峰 | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline |
| CN101798527B (en) * | 2009-12-11 | 2013-03-13 | 深圳市兖能环保科技有限公司 | Treatment method for liquid products in garbage microwave pyrolysis treatment system and distillation equipment used by same |
-
2007
- 2007-11-09 CN CNU2007203020939U patent/CN201144228Y/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101429443B (en) * | 2007-11-09 | 2012-08-22 | 丁冉峰 | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline |
| CN101798527B (en) * | 2009-12-11 | 2013-03-13 | 深圳市兖能环保科技有限公司 | Treatment method for liquid products in garbage microwave pyrolysis treatment system and distillation equipment used by same |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20081105 Effective date of abandoning: 20071109 |