CN101497806B - System and method for preparing high quality petrol - Google Patents
System and method for preparing high quality petrol Download PDFInfo
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- CN101497806B CN101497806B CN 200810005205 CN200810005205A CN101497806B CN 101497806 B CN101497806 B CN 101497806B CN 200810005205 CN200810005205 CN 200810005205 CN 200810005205 A CN200810005205 A CN 200810005205A CN 101497806 B CN101497806 B CN 101497806B
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- 238000000034 method Methods 0.000 title claims abstract description 33
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 69
- 238000000605 extraction Methods 0.000 claims abstract description 59
- 239000000284 extract Substances 0.000 claims abstract description 4
- 239000003502 gasoline Substances 0.000 claims description 122
- 239000003208 petroleum Substances 0.000 claims description 51
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 24
- 238000009835 boiling Methods 0.000 claims description 23
- 239000002283 diesel fuel Substances 0.000 claims description 17
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 9
- 239000005977 Ethylene Substances 0.000 claims description 9
- 239000003054 catalyst Substances 0.000 claims description 9
- 238000005194 fractionation Methods 0.000 claims description 9
- 239000000126 substance Substances 0.000 claims description 6
- 238000005345 coagulation Methods 0.000 claims description 4
- 239000001257 hydrogen Substances 0.000 claims description 4
- 229910052739 hydrogen Inorganic materials 0.000 claims description 4
- 238000002360 preparation method Methods 0.000 claims description 4
- 238000005520 cutting process Methods 0.000 claims description 2
- 238000002156 mixing Methods 0.000 claims 2
- 150000001336 alkenes Chemical class 0.000 abstract description 20
- 238000004821 distillation Methods 0.000 abstract description 13
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 abstract description 13
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical class S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 abstract description 10
- 150000001993 dienes Chemical class 0.000 abstract description 8
- 239000003921 oil Substances 0.000 description 48
- 239000002904 solvent Substances 0.000 description 34
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 29
- 239000005864 Sulphur Substances 0.000 description 20
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 16
- 230000003197 catalytic effect Effects 0.000 description 12
- 238000007689 inspection Methods 0.000 description 11
- 229930195733 hydrocarbon Natural products 0.000 description 10
- 150000002430 hydrocarbons Chemical class 0.000 description 10
- 229910052717 sulfur Inorganic materials 0.000 description 10
- 239000011593 sulfur Substances 0.000 description 10
- 239000004215 Carbon black (E152) Substances 0.000 description 8
- 230000008569 process Effects 0.000 description 8
- 239000000047 product Substances 0.000 description 7
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 6
- 238000003556 assay Methods 0.000 description 6
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical group O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 0.000 description 6
- 238000005406 washing Methods 0.000 description 6
- 238000004523 catalytic cracking Methods 0.000 description 5
- 239000003209 petroleum derivative Substances 0.000 description 4
- 238000001179 sorption measurement Methods 0.000 description 4
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 description 3
- 238000004458 analytical method Methods 0.000 description 3
- 238000004737 colorimetric analysis Methods 0.000 description 3
- 239000010779 crude oil Substances 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000000295 fuel oil Substances 0.000 description 3
- 230000006872 improvement Effects 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 238000003672 processing method Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 238000007233 catalytic pyrolysis Methods 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000003269 fluorescent indicator Substances 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000010025 steaming Methods 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 229910004298 SiO 2 Inorganic materials 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003518 caustics Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 239000010771 distillate fuel oil Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000004231 fluid catalytic cracking Methods 0.000 description 1
- 238000002795 fluorescence method Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000035515 penetration Effects 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 238000003918 potentiometric titration Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 238000000207 volumetry Methods 0.000 description 1
- 238000005303 weighing Methods 0.000 description 1
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Abstract
The invention discloses a device and a method for preparing high quality petrol. The device comprises a distillation device and is characterized in that the upper part of the distillation device is connected with a light petrol extraction device by a pipeline, the lower part of the distillation device is connected with a heavy petrol extraction device by a pipeline, the upper part of the heavy petrol extraction device is connected with the other hydrogenation unit by a pipeline or directly extracts the product; the lower part of the heavy petrol extraction device is connected with a hydrogenation unit by a pipeline, the middle part of the distillation device is connected with an immediate petrol extraction device by a pipeline, the upper part of the immediate petrol extraction device is connected with the other hydrogenation unit by a pipeline, and the lower part of the immediate petrol extraction device is connected with the hydrogenation unit by a pipeline. The device and the method can remove olefin, 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.
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 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 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 extractor by pipeline; Described petroleum naphtha extractor top is by the direct extraction product of pipeline, and described petroleum naphtha extractor bottom is connected with hydrogenation unit by pipeline; Described water distilling apparatus bottom is connected with the heavy petrol extractor by pipeline; Described heavy petrol extractor top is connected with another hydrogenation unit by pipeline or direct extraction product; Described heavy petrol extractor bottom is connected with hydrogenation unit by pipeline; Described water distilling apparatus middle part is connected with middle gasoline extractor by pipeline; Described middle gasoline extractor top is connected with another hydrogenation unit by pipeline, and described middle gasoline extractor bottom is connected with hydrogenation unit by pipeline.
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, middle gasoline and heavy petrol; Described petroleum naphtha enters the petroleum naphtha extractor by water distilling apparatus top and carries out extracting and separating, isolates petroleum naphtha extraction oil and petroleum naphtha and raffinates oil; Described petroleum naphtha is raffinated oil as the direct extraction of blended gasoline, and described petroleum naphtha is extracted oil out and entered after the hydrogenation device for treatment to raffinate oil to be in harmonious proportion with described petroleum naphtha by pipeline and use; Described middle gasoline carries out extracting and separating in middle gasoline extractor, isolates middle gasoline extraction oil and middle gasoline and raffinates oil; Described middle gasoline is extracted oil out and is entered by pipeline and obtain hydrogenation after the hydrogenation device for treatment and extract oil out, is in harmonious proportion with described petroleum naphtha and uses, and described middle gasoline is raffinated oil and entered after the hydrogenation device for treatment as the high-quality ethylene extraction by pipeline; Described heavy petrol carries out extracting and separating in the heavy petrol extractor, isolates heavy petrol extraction oil and heavy petrol and raffinates oil; Described heavy petrol is extracted out and is obtained hydrogenation extraction oil after oil enters hydrogenation device for treatment by pipeline, mix again rear as the blended gasoline extraction with described petroleum naphtha, described heavy petrol is raffinated oil or as the direct extraction of low-coagulation diesel oil, perhaps after hydrogenation device for treatment 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 190～192 ℃; The tower top pressure of described water distilling apparatus is 0.11～0.28MPa absolute pressure, and tower bottom pressure is 0.12～0.30MPa absolute pressure; The boiling range of described petroleum naphtha is controlled at 30 ℃～80 ℃; The boiling range of described middle gasoline is controlled at 80 ℃～160 ℃; 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 82 ℃, and column bottom temperature is 190 ℃; The tower top pressure of described water distilling apparatus is the 0.2MPa absolute pressure, and tower bottom pressure is the 0.25MPa absolute pressure.
A kind of preferred version is characterized in that: the catalyzer in the described hydrogenation unit is whole hydrogenation catalyst GHT-22; The volume space velocity of described hydrogenation unit is 2-3; Hydrogen/oil volume ratio is 200～300; Service temperature is 285～325 ℃, and working pressure is 1.5～2.5MPa absolute pressure.
A kind of preferred version is characterized in that: the physico-chemical property of the whole hydrogenation catalyst GHT-22 in the described hydrogenation unit is as shown in the table.
Petroleum naphtha described in the present invention, middle gasoline and heavy petrol extractor 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 (boiling range) of petroleum naphtha of the present invention, middle gasoline and heavy petrol 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 extractor 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 (diolefine); 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, chemical industry light oil is optimized, and the extraction oil in the blended gasoline increases, and octane value improves.
The present invention will be further described below by the drawings and specific embodiments, but and do not mean that limiting the scope of the invention.
Fig. 1 is the schematic flow sheet of the embodiment of the invention 1.
Description of drawings
Fig. 2 is the schematic flow sheet of the embodiment of the invention 2.
Embodiment 1
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 100,000 ton/years flow, the tower top temperature of distillation tower 1 is 82 ℃, column bottom temperature is 190 ℃, tower top pressure is the 0.2MPa absolute pressure, tower bottom pressure is the 0.25MPa absolute pressure, obtains respectively petroleum naphtha, middle gasoline and heavy petrol; Described petroleum naphtha (boiling range is 30-80 ℃) steams by distillation tower 1 top, and its total amount of steaming is 3.8 ten thousand ton/years, then enters extracting and separating among the petroleum naphtha extractor 2-1, isolates petroleum naphtha extraction oil and petroleum naphtha and raffinates oil; Solvent for use is tetramethylene sulfone among the described extractor 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 the 0.112MPa absolute pressure; The described extraction out extracted the oily rear extraction that mixes with blended gasoline out as hydrogenation after oily flow with 1.50 ten thousand ton/years enters hydrogenation unit 3-1 hydrotreatment, and the catalyzer among the described hydrogenation unit 3-1 is whole hydrogenation catalyst GHT-22; The volume space velocity of described hydrogenation unit 3-1 is 2.5h
-1Hydrogen/oil volume ratio is 200; Service temperature is 285 ℃, and working pressure is the 1.5MPa absolute pressure; Described petroleum naphtha is raffinated oil with 2.3 ten thousand ton/years flow as the blended gasoline extraction.Described heavy petrol (boiling range is 160-205 ℃) enters extracting and separating among the heavy petrol extractor 2-2 with 2.0 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 extractor 2-2, extraction temperature is 115 ℃, and solvent ratio (solvent/charging) is 3.5 (quality), and the washing of raffinating oil is than being 0.2 (quality), the solvent recuperation temperature is 157 ℃, and solvent recuperation pressure is the 0.112MPa absolute pressure; The oily flow with 0.8 ten thousand ton/years of described heavy petrol extraction enters and carries out among the hydrogenation unit 3-1 extracting the oily rear extraction that mixes with blended gasoline out as hydrogenation after the hydrotreatment; Described heavy petrol is raffinated oil to enter with 1.2 ten thousand ton/years flow and is carried out among the hydrogenation unit 3-2 after the hydrotreatment as the high-quality ethylene extraction.Described middle gasoline (boiling range is 80-160 ℃) enters extracting and separating among the middle gasoline extractor 2-3 with 4.2 ten thousand ton/years flows, isolates middle gasoline extraction oil and middle gasoline and raffinates oil; Solvent for use is tetramethylene sulfone among the described extractor 2-3, extraction temperature is 95 ℃, and solvent ratio (solvent/charging) is 2.5 (quality), and the washing of raffinating oil is than being 0.2 (quality), the solvent recuperation temperature is 155 ℃, and solvent recuperation pressure is the 0.13MPa absolute pressure; The oily flow with 1.30 ten thousand ton/years of described middle gasoline extraction enters and carries out among the hydrogenation unit 3-1 extracting the oily rear extraction that mixes with blended gasoline out as hydrogenation after the hydrotreatment; Described middle gasoline is raffinated oil to enter with 2.9 ten thousand ton/years flow and is carried out among the hydrogenation unit 3-2 after the hydrotreatment as the high-quality ethylene extraction.
The boiling range of gained blended gasoline is 30-205 ℃, sulphur content is 23.14ppm, mercaptans content is 0.8ppm, olefin(e) centent is 18.8% (v), diolefine＜0.01% (v) (trace, inspection does not measure), aromaticity content is 22.9% (v), octane value (RON) is 94.6, and density is 724.3 kg/ms
3, produced quantity is 5.9 ten thousand ton/years.
The boiling range of gained high-quality ethylene is 160-205 ℃, sulphur content is 2.0ppm, mercaptans content＜1ppm (trace, inspection does not measure), olefin(e) centent is 1.0% (v), diolefine＜0.01% (v) (trace, inspection does not measure), aromaticity content is 3.6% (v), and octane value (RON) is 70.2, and density is 733.4 kg/ms
3, produced quantity is 4.1 ten thousand ton/years.
The physico-chemical property of whole hydrogenation catalyst GHT-22 among described hydrogenation unit 3-1 and the 3-2 is as shown in the table.
The used measuring method of the present invention is (together lower):
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 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.It is 30-205 ℃ with boiling range, sulphur content is 100ppm, mercaptans content is 5ppm, olefin(e) centent is 30% (v), diene content is 0.1% (v), aromaticity content is 15% (v), octane value (RON) is 89, and density is that 728 kg/m 3 stable gasoline (catalytic gasoline) cuts fractionation with 60,000 ton/years flow in distillation tower 1, simultaneously, it is 30-205 ℃ with boiling range, sulphur content is 200ppm, and mercaptans content is 1ppm, olefin(e) centent＜0.1% (v) (trace, inspection does not measure), diene content＜0.01% (v) (trace, inspection does not measure), 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), diene content＜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 the 0.2MPa absolute pressure, tower bottom pressure is the 0.25MPa absolute pressure, obtain respectively petroleum naphtha, middle gasoline and heavy petrol, described petroleum naphtha (boiling range is 30-80 ℃) steams by distillation tower 1 top, and its total amount of steaming is 3.7 ten thousand ton/years, then enter extracting and separating among the petroleum naphtha extractor 2-1, isolate petroleum naphtha extraction oil and petroleum naphtha and raffinate oil; Solvent for use is tetramethylene sulfone among the described extractor 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 the 0.112MPa absolute pressure; Described petroleum naphtha is extracted out and is extracted the oily rear extraction that mixes with blended gasoline out as hydrogenation after oily flow with 1.40 ten thousand ton/years enters hydrogenation unit 3-1 hydrotreatment, and the catalyzer among the described hydrogenation unit 3-1 is whole hydrogenation catalyst GHT-22; The volume space velocity of described hydrogenation unit 3-1 is 2.5h
-1Hydrogen/oil volume ratio is 200; Service temperature is 285 ℃, and working pressure is the 1.5MPa absolute pressure; Described petroleum naphtha is raffinated oil with 2.3 ten thousand ton/years flow as the blended gasoline extraction.Described heavy petrol (boiling range is 160-205 ℃) enters extracting and separating among the heavy petrol extractor 2-2 with 2.1 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 extractor 2-2, extraction temperature is 115 ℃, and solvent ratio (solvent/charging) is 3.5 (quality), and the washing of raffinating oil is than being 0.2 (quality), the solvent recuperation temperature is 157 ℃, and solvent recuperation pressure is the 0.112MPa absolute pressure; The oily flow with 0.8 ten thousand ton/years of described heavy petrol extraction enters and carries out among the hydrogenation unit 3-1 extracting the oily rear extraction that mixes with blended gasoline out as hydrogenation after the hydrotreatment; Described heavy petrol is raffinated oil to enter with 1.3 ten thousand ton/years flow and is carried out among the hydrogenation unit 3-2 after the hydrotreatment as the low-coagulation diesel oil extraction.Described middle gasoline (boiling range is 80-160 ℃) enters extracting and separating among the middle gasoline extractor 2-3 with 4.2 ten thousand ton/years flows, isolates middle gasoline extraction oil and middle gasoline and raffinates oil; Solvent for use is tetramethylene sulfone among the described extractor 2-3, extraction temperature is 95 ℃, and solvent ratio (solvent/charging) is 2.5 (quality), and middle gasoline is raffinated oil washing than being 0.2 (quality), the solvent recuperation temperature is 155 ℃, and solvent recuperation pressure is the 0.13MPa absolute pressure; The oily flow with 0.95 ten thousand ton/year of described middle gasoline extraction enters and carries out among the hydrogenation unit 3-1 extracting the oily rear extraction that mixes with blended gasoline out as hydrogenation after the hydrotreatment; Described middle gasoline is raffinated oil to enter with 3.25 ten thousand ton/years flow and is carried out among the hydrogenation unit 3-2 after the hydrotreatment as high-quality ethylene or as the reformer feed extraction.
The boiling range of gained blended gasoline is 30-205 ℃, and sulphur content is 23.7ppm, and mercaptans content is 0.4ppm, and olefin(e) centent is 15.0% (v), diene content＜0.01% (v) (trace, inspection does not measure); Aromaticity content is 20.3% (v), and octane value (RON) is 92.8, and density is 720.5 kg/ms
3, produced quantity is 5.45 ten thousand ton/years.
The boiling range of gained reformer feed (or high-quality ethylene) is 160-205 ℃, sulphur content is 0.50ppm, mercaptans content＜1ppm (trace, inspection does not measure), alkene＜0.1% (v) (trace, inspection does not measure), diolefine＜0.01% (v) (trace, inspection does not measure), aromaticity content is 3.0% (v), octane value (RON) is 74.1, and density is 727.0 kg/ms
3, produced quantity is 3.25 ten thousand ton/years.
The boiling range of gained low-coagulation diesel oil is 160-205 ℃, and sulphur content is 32.0ppm, and mercaptans content is 1.0ppm, olefin(e) centent is 28.2% (v), diolefine＜0.01% (v) (trace, inspection does not measure), aromaticity content is 3.5% (v), and density is 759.0 kg/ms
3, produced quantity is 1.3 ten thousand ton/years.
The physico-chemical property of whole hydrogenation catalyst GHT-22 among described hydrogenation unit 3-1 and the 3-2 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 |
| 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 extractor by pipeline; Described petroleum naphtha extractor top is by the direct extraction product of pipeline, and described petroleum naphtha extractor bottom is connected with hydrogenation unit by pipeline; Described water distilling apparatus bottom is connected with the heavy petrol extractor by pipeline; Described heavy petrol extractor top is connected with another hydrogenation unit by pipeline or direct extraction product; Described heavy petrol extractor bottom is connected with hydrogenation unit by pipeline; Described water distilling apparatus middle part is connected with middle gasoline extractor by pipeline; Described middle gasoline extractor top is connected with another hydrogenation unit by pipeline, and described middle gasoline extractor bottom is connected with hydrogenation unit by pipeline.
2. the equipment of described preparation premium-type gasoline prepares the method for premium-type gasoline according to claim 1, 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, middle gasoline and heavy petrol; Described petroleum naphtha enters the petroleum naphtha extractor by water distilling apparatus top and carries out extracting and separating, isolates petroleum naphtha extraction oil and petroleum naphtha and raffinates oil; Described petroleum naphtha is raffinated oil as the direct extraction of blended gasoline, and described petroleum naphtha is extracted oil out and entered after the hydrogenation device for treatment to raffinate oil to mix afterwards with described petroleum naphtha by pipeline and use as blended gasoline; Described middle gasoline carries out extracting and separating in middle gasoline extractor, isolates middle gasoline extraction oil and middle gasoline and raffinates oil; Described middle gasoline is extracted oil out and is entered by pipeline and obtain hydrogenation after the hydrogenation device for treatment and extract oil out, and as the blended gasoline use, described middle gasoline is raffinated oil and entered after the hydrogenation device for treatment as the high-quality ethylene extraction by pipeline after mixing with described petroleum naphtha again; Described heavy petrol carries out extracting and separating in the heavy petrol extractor, isolates heavy petrol extraction oil and heavy petrol and raffinates oil; Described heavy petrol is extracted out and is obtained hydrogenation extraction oil after oil enters hydrogenation device for treatment by pipeline, use as blended gasoline after mixing with described petroleum naphtha again, described heavy petrol is raffinated oil or as the direct extraction of low-coagulation diesel oil, perhaps enters after the hydrogenation device for treatment as the high-quality ethylene extraction by pipeline.
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 190～192 ℃; The tower top pressure of described water distilling apparatus is 0.11～0.28MPa absolute pressure, and tower bottom pressure is 0.12～0.30MPa absolute pressure; The boiling range of described petroleum naphtha is controlled at 30 ℃～80 ℃; The boiling range of described middle gasoline is controlled at 80 ℃～160 ℃; The boiling range of described heavy petrol is controlled at 160 ℃～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 absolute pressure, and tower bottom pressure is the 0.25MPa 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 2-3h
-1Hydrogen/oil volume ratio is 200～300; Service temperature is 285～325 ℃, and working pressure is 1.5～2.5MPa 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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| CN 200810005205 CN101497806B (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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| CN111778068A (en) * | 2020-07-10 | 2020-10-16 | 盘锦浩业化工有限公司 | Coking gasoline processing technology |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1994022980A1 (en) * | 1993-04-02 | 1994-10-13 | Mobil Oil Corporation | Gasoline upgrading process |
| US20010027936A1 (en) * | 2000-01-11 | 2001-10-11 | Frederic Morel | Process for converting petroleum fractions, comprising an ebullated bed hydroconversion step, a separation step, a hydrodesulphurisation step and a cracking step |
| CN1621497A (en) * | 2003-11-24 | 2005-06-01 | 北京金伟晖工程技术有限公司 | Recombinant processing method for naphtha |
| CN1912062A (en) * | 2005-08-09 | 2007-02-14 | 中国石油化工股份有限公司 | Hydrogenation method for producing catalytic reforming raw material |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1994022980A1 (en) * | 1993-04-02 | 1994-10-13 | Mobil Oil Corporation | Gasoline upgrading process |
| US20010027936A1 (en) * | 2000-01-11 | 2001-10-11 | Frederic Morel | Process for converting petroleum fractions, comprising an ebullated bed hydroconversion step, a separation step, a hydrodesulphurisation step and a cracking step |
| CN1621497A (en) * | 2003-11-24 | 2005-06-01 | 北京金伟晖工程技术有限公司 | Recombinant processing method for naphtha |
| CN1912062A (en) * | 2005-08-09 | 2007-02-14 | 中国石油化工股份有限公司 | Hydrogenation method for producing catalytic reforming raw material |
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