CN101429447B - System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline - Google Patents
System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline Download PDFInfo
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- CN101429447B CN101429447B CN2007101699475A CN200710169947A CN101429447B CN 101429447 B CN101429447 B CN 101429447B CN 2007101699475 A CN2007101699475 A CN 2007101699475A CN 200710169947 A CN200710169947 A CN 200710169947A CN 101429447 B CN101429447 B CN 101429447B
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- 239000003502 gasoline Substances 0.000 title claims abstract description 62
- 238000000034 method Methods 0.000 title claims abstract description 31
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 25
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 25
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 23
- 238000004519 manufacturing process Methods 0.000 title claims description 14
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 60
- 238000000605 extraction Methods 0.000 claims abstract description 31
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims abstract description 13
- 239000003208 petroleum Substances 0.000 claims description 36
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 33
- 238000009835 boiling Methods 0.000 claims description 28
- 239000000126 substance Substances 0.000 claims description 15
- 125000003118 aryl group Chemical group 0.000 claims description 10
- 238000005194 fractionation Methods 0.000 claims description 9
- 230000008569 process Effects 0.000 claims description 8
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 30
- 239000005864 Sulphur Substances 0.000 abstract description 22
- 230000003197 catalytic effect Effects 0.000 abstract description 15
- 239000003054 catalyst Substances 0.000 abstract description 13
- 238000004821 distillation Methods 0.000 abstract description 13
- 238000005215 recombination Methods 0.000 abstract description 2
- 230000006798 recombination Effects 0.000 abstract description 2
- 239000003921 oil Substances 0.000 description 29
- 238000005520 cutting process Methods 0.000 description 22
- 150000001336 alkenes Chemical class 0.000 description 19
- 239000002904 solvent Substances 0.000 description 17
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 15
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 13
- 150000001993 dienes Chemical class 0.000 description 10
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical class S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 9
- 229910052717 sulfur Inorganic materials 0.000 description 9
- 239000011593 sulfur Substances 0.000 description 9
- 239000002283 diesel fuel Substances 0.000 description 8
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 7
- 239000001257 hydrogen Substances 0.000 description 7
- 229910052739 hydrogen Inorganic materials 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
- LCEDQNDDFOCWGG-UHFFFAOYSA-N morpholine-4-carbaldehyde Chemical compound O=CN1CCOCC1 LCEDQNDDFOCWGG-UHFFFAOYSA-N 0.000 description 6
- 239000011148 porous material Substances 0.000 description 6
- 238000004523 catalytic cracking Methods 0.000 description 4
- 239000003209 petroleum derivative Substances 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 230000008521 reorganization Effects 0.000 description 4
- 238000004458 analytical method Methods 0.000 description 3
- 238000004737 colorimetric analysis Methods 0.000 description 3
- 239000010779 crude oil Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 230000006872 improvement Effects 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 238000001179 sorption measurement Methods 0.000 description 3
- 238000010025 steaming Methods 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 description 2
- 229910004298 SiO 2 Inorganic materials 0.000 description 2
- 238000007233 catalytic pyrolysis Methods 0.000 description 2
- 239000003269 fluorescent indicator Substances 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 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
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 239000010771 distillate fuel oil Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000002795 fluorescence method Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- -1 liquefaction vapour Substances 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
- 239000000203 mixture Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 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 system and a method for preparing high-quality gasoline by recombination of catalyzed hydrocarbon. The system comprises a distillation apparatus, and is characterized in that the upper part of the distillation apparatus is connected with a light gasoline hydrogenation device; the lower part of the distillation apparatus is connected with an extraction system through a heavy gasoline pipeline; the lower part of the extraction system is connected with a hydrogenation device through a pipeline; and the hydrogenation device is connected with the light gasoline pipeline on the upper part of a catalytic unit through a pipeline. Catalysts and parameters of the hydrogenation device aim at aromatic hydrocarbon; and the sulphur content of the obtained blended gasoline are lower, and the olefinic content is lower (below 1 percent), which meet the requirements of national standard 4.
Description
Technical field
The present invention relates to a kind of system and method thereof 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, RFCC; 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, and 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 and discloses its improvement 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).As far as 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 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, quality of gasoline upgrading is to be solved falls the problem that sulphur and the problem of falling alkene relate generally to catalytic gasoline.
It is generally acknowledged; The 5-10% of total sulfur will get into gasoline in the catalytically cracked material, and, secondary processing catalytic cracking ability very little according to China's refinery fcc raw material unifining ability is big and the characteristics of residuum coking, the about 200ppm of refinery catalytic gasoline sulphur content of processing low-sulfur (sulfur-bearing 0.3%) crude oil are arranged; 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, CCU excessively reduces the loss that alkene also can aggravate light-end products and gasoline octane rating (RON).
Therefore, provide the treatment system and the method thereof 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
One of the object of the invention 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 realizing above-mentioned purpose, the present invention takes 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: said water distilling apparatus top is provided with the petroleum naphtha pipeline; Said water distilling apparatus bottom is connected with said extraction system through the heavy petrol pipeline; The bottom of said extraction system is connected with hydrogenation unit through pipeline, and said hydrogenation unit is connected through the petroleum naphtha pipeline of pipeline with said catalytic unit top again; The top of said extraction system is through pipeline extraction chemical industry light oil.
A kind of preferred version is characterized in that: the top of said water distilling apparatus is connected with hydrogenation unit through the petroleum naphtha pipeline.
Another object of the present invention provides the method for catalyzing hydrocarbon for recombinant production of high-quality gasoline.
A kind of method of catalyzing hydrocarbon for recombinant production of high-quality gasoline, its step is following: stable gasoline is added water distilling apparatus carry out fractionation, fractionate out petroleum naphtha and heavy petrol; Said petroleum naphtha steams through water distilling apparatus top; Said heavy petrol gets in the extraction system and carries out extracting and separating, isolates aromatic hydrocarbons and raffinates oil; Said aromatic hydrogenation is handled the back and is used with the petroleum naphtha mediation that said water distilling apparatus top steams, and the said direct extraction of raffinating oil is as chemical industry light oil.
A kind of preferred version is characterized in that: the petroleum naphtha pipeline of said water distilling apparatus through after the hydrogenation device for treatment again with hydrogenation after aromatic hydrocarbons be in harmonious proportion.
A kind of preferred version is characterized in that: the tower top temperature of said water distilling apparatus is 82～86 ℃, and column bottom temperature is 190～192 ℃; The tower top pressure of said 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 said petroleum naphtha is controlled at 30 ℃～80 ℃; The boiling range of said heavy petrol is controlled at 80 ℃～205 ℃.
A kind of preferred version is characterized in that: the tower top temperature of said water distilling apparatus is 82～86 ℃, and column bottom temperature is 190～192 ℃; The tower top pressure of said water distilling apparatus is 0.2MPa (cutting off), and tower bottom pressure is 0.25MPa (cutting off); The boiling range of said petroleum naphtha is controlled at 30 ℃～80 ℃; The boiling range of said heavy petrol is controlled at 80 ℃～205 ℃.
A kind of preferred version is characterized in that: the tower top temperature of said water distilling apparatus is 82～86 ℃, and column bottom temperature is 190～192 ℃; The tower top pressure of said water distilling apparatus is 0.2MPa (cutting off), and tower bottom pressure is 0.25MPa (cutting off); The boiling range of said petroleum naphtha is controlled at 30 ℃～90 ℃; The boiling range of said heavy petrol is controlled at 90 ℃～205 ℃.
A kind of preferred version is characterized in that: the selective hydrogenation catalyst GHT-20 in the said petroleum naphtha hydrogenation unit; The volume space velocity ratio of said petroleum naphtha hydrogenation unit is 2～4; Hydrogen/oil volume ratio is 150～300; Service temperature is 230～250 ℃, and working pressure is 1.0MPa (cutting off).
A kind of preferred version is characterized in that: the physico-chemical property of the selective hydrogenation catalyst GHT-20 in the said petroleum naphtha 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 |
[0023]A kind of preferred version is characterized in that: the catalyzer in the said aromatic hydrogenation device is whole hydrogenation catalyst GHT-22; The volume space velocity ratio of said aromatic hydrogenation device is 2～3; Hydrogen/oil volume ratio is 250～300; Service temperature is 285～325 ℃, and working pressure is 1.5～2.5MPa (cutting off).
A kind of preferred version is characterized in that: the physico-chemical property of the whole hydrogenation catalyst GHT-22 in the said aromatic hydrogenation device is as shown in table 2 below.
Table 2
| Index name | Unit | GHT-22 |
| Outward appearance | - | The grey trilobal cross |
| Specification | mm | Φ1.5-2.0 |
| Intensity | N/cm | 180 |
| Bulk density | g/ml | 0.73 |
| Specific surface area | m 2/g | 180 |
| Pore volume | ml/g | 0.5-0.6 |
| WO 3 | m％ | 15 |
| NiO | m％ | 1.7 |
| C 0O | m％ | 0.15 |
| Na 2O | m％ | ＜0.09 |
| Fe 2O 3 | m％ | ＜0.06 |
| SiO 2 | m％ | ＜0.60 |
| Carrier | m％ | 82.4 |
The used water distilling apparatus of the present invention 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 said extraction system uses the patent No., comprises solvent recuperation and water wash system.
The used hydrogenation unit of the present invention is existing hydrogenation unit, comprises process furnace, interchanger, HP separator, atmospheric condenser, water condenser etc.
Beneficial effect:
Compared with prior art; The system of catalyzing hydrocarbon for recombinant production of high-quality gasoline of the present invention and the advantage of method thereof are: earlier through after the reorganization; Repeated hydrogenation, catalyzer and parameter in the used hydrogenation unit have more specific aim, and the sulphur content of gained blended gasoline is lower; Olefin(e) centent is also lower, and with low cost.
Through accompanying drawing and embodiment the present invention is further specified below, but and do not mean that restriction protection domain of the present invention.
Description of drawings
Fig. 1 is the schematic flow sheet of the embodiment of the invention 1.
Fig. 2-1 is the schematic flow sheet of the embodiment of the invention 2.
Fig. 2-2 is the schematic flow sheet of the embodiment of the invention 3.
Embodiment
Embodiment 1
As shown in Figure 1, be the schematic flow sheet of one of embodiment of the invention, be 30-205 ℃ with boiling range, sulphur content is 100ppm; Mercaptans content is 5ppm, and olefin(e) centent is 30%, and (v), diene content is 0.1% (v); Aromaticity content is that 15% (v), octane value (RON) is 89, and density is 728 kilograms/meter
3Stable gasoline (catalytic gasoline) in distillation tower 1, cut fractionation with 100,000 tons/year flow; The tower top temperature of distillation tower 1 is 82 ℃, and column bottom temperature is 190 ℃, and tower top pressure is 0.2MPa (cutting off); Tower bottom pressure is 0.25MPa (cutting off); Fractionation obtains petroleum naphtha and heavy petrol respectively, and said petroleum naphtha (boiling range is 30-80 ℃) steams through distillation tower 1 top, and its total amount of steaming is 40,000 tons/year; Said heavy petrol (boiling range is 80-205 ℃) gets into extracting and separating in the heavy petrol extraction system 2 with 60,000 tons/year flows through pipeline, isolates aromatic hydrocarbons and raffinates oil; The extraction solvent for use is the N-formyl morpholine in the said extraction system 2, and 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), and the solvent recuperation temperature is 151 ℃, and solvent recuperation pressure is 0.112MPa (cutting off); Said aromatic hydrocarbons gets into aromatic hydrogenation device 3 hydrogenation with 1.5 ten thousand tons/year flow, and the catalyzer in the said hydrogenation unit 3 is whole hydrogenation catalyst GHT-22; The volume space velocity ratio of said hydrogenation unit 3 is 2; Hydrogen/oil volume ratio is 250; Service temperature is 285 ℃, and working pressure is 1.5MPa (cutting off); And then be in harmonious proportion said raffinating oil with 1.5 ten thousand tons/year flow with said petroleum naphtha as the chemical industry light oil extraction.
The boiling range of gained blended gasoline is 30-205 ℃, and sulphur content is 13.6ppm, and mercaptans content is 4.4ppm, and olefin(e) centent is 23.9%, and (v), diene content is 0.1% (v), aromaticity content is that 25.6% (v), octane value (RON) is 95.6, and density is 703.8 kilograms/meter
3, produced quantity is 5.5 ten thousand tons/year.
The boiling range of gained chemical industry light oil is 80-205 ℃, and sulphur content is 10.0ppm, and mercaptans content is 1.0ppm, and olefin(e) centent is 35.5%, and (v), diene content is 0.01% (v), aromaticity content is that 3.0% (v), octane value (RON) is 81.0, and density is 760.0 kilograms/meter
3, produced quantity is 4.5 ten thousand tons/year.
The physico-chemical property of said whole hydrogenation catalyst GHT-22 is as shown in table 3 below.
Table 3
| Index name | Unit | GHT-22 |
| Outward appearance | - | The grey trilobal cross |
| Specification | mm | Φ1.7 |
| Intensity | N/cm | 180 |
| Bulk density | g/ml | 0.73 |
| Specific surface area | m 2/g | 180 |
| Pore volume | ml/g | 0.57 |
| WO 3 | m％ | 15 |
| NiO | m％ | 1.7 |
| C 0O | m％ | 0.15 |
| Na 2O | m％ | ＜0.09 |
| Fe 2O 3 | m％ | ＜0.06 |
| SiO 2 | m％ | ＜0.60 |
| Carrier | m％ | 82.4 |
The used measuring method of the present invention is (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 | Colourimetry | SH/T0346-1992 |
| CoO | Colourimetry | SH/T0345-1992 |
[0053]
| WO 3 | Colourimetry | |
| Physical property | Analytical procedure | The instrument that uses |
| Surface-area | Low-temperature nitrogen adsorption method | 2400 types absorption appearance |
| 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 |
Shown in Fig. 2-1, be two schematic flow sheet of the embodiment of the invention.With boiling range is 30-205 ℃, and sulphur content is 100ppm, and mercaptans content is 5ppm, and olefin(e) centent is 30%, and (v), diene content is 0.1% (v), aromaticity content is that 15% (v), octane value (RON) is 89, and density is 728 kilograms/meter
3Stable gasoline (catalytic gasoline) in distillation tower 1, cut fractionation with 100,000 tons/year flow; The tower top temperature of distillation tower 1 is 86 ℃, and column bottom temperature is 192 ℃, and tower top pressure is 0.2MPa (cutting off); Tower bottom pressure is 0.25MPa (cutting off); Fractionation obtains petroleum naphtha and heavy petrol respectively, and said petroleum naphtha (boiling range is 30-80 ℃) steams back hydrotreatment in hydrogenation unit 3-1 through distillation tower 1 top, and the total amount of steaming of the petroleum naphtha behind the hydrogenation is 40,000 tons/year; Catalyzer among the said hydrogenation unit 3-1 is selective hydrogenation catalyst GHT-20; The volume space velocity ratio of said hydrogenation unit 3-1 is 2; Hydrogen/oil volume ratio is 150; Service temperature is 230 ℃, and working pressure is 1.0MPa (cutting off); Said heavy petrol (boiling range is 80-205 ℃) gets into extracting and separating in the heavy petrol extraction system 2 with 60,000 tons/year flows through pipeline, isolates aromatic hydrocarbons and raffinates oil; Solvent for use is the N-formyl morpholine in the said extraction system 2, and 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), and the solvent recuperation temperature is 151 ℃, and solvent recuperation pressure is 0.112MPa (cutting off); Said aromatic hydrocarbons gets into aromatic hydrogenation device 3-2 hydrogenation with 1.5 ten thousand tons/year flow, and the catalyzer among the said hydrogenation unit 3-2 is whole hydrogenation catalyst GHT-22; The volume space velocity ratio of said hydrogenation unit 3-2 is 2; Hydrogen/oil volume ratio is 250; Service temperature is 295 ℃, and working pressure is 2.0MPa (cutting off); And then be in harmonious proportion said raffinating oil with 1.5 ten thousand tons/year flow with petroleum naphtha behind the said hydrogenation as the chemical industry light oil extraction.
The boiling range of gained blended gasoline is 30-205 ℃, and sulphur content is 4.2ppm, and mercaptans content is less than 1ppm; Olefin(e) centent is 17.8%, and (v), diene content is that (v), aromaticity content is 25.6% (v) less than 0.01%; Octane value (RON) is 94.1, and density is 703.8 kilograms/meter
3, produced quantity is 5.5 ten thousand tons/year.
The boiling range of gained chemical industry light oil is 80-205 ℃, and sulphur content is 10.0ppm, and mercaptans content is 1.0ppm, and olefin(e) centent is 35.5%, and (v), diene content is 0.01% (v), aromaticity content is that 3.0% (v), octane value (RON) is 81.0, and density is 760.0 kilograms/meter
3, produced quantity is 4.5 ten thousand tons/year.
The physico-chemical property of said selective hydrogenation catalyst GHT-20 is as shown in table 4 below.
Table 4
| 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 |
Shown in Fig. 2-2, be three schematic flow sheet of the embodiment of the invention.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 kilograms/meter
3Stable gasoline (catalytic gasoline) in distillation tower 1, cut fractionation with 100,000 tons/year flow; The tower top temperature of distillation tower 1 is 86 ℃, and column bottom temperature is 192 ℃, and tower top pressure is 0.2MPa (cutting off); Tower bottom pressure is 0.25MPa (cutting off); Fractionation obtains petroleum naphtha and heavy petrol respectively, and said petroleum naphtha (boiling range is 30-90 ℃) steams back hydrotreatment in hydrogenation unit 3-1 through distillation tower 1 top, and the total amount of steaming of the petroleum naphtha behind the hydrogenation is 4.3 ten thousand tons/year; Catalyzer among the said hydrogenation unit 3-1 is selective hydrogenation catalyst GHT-20; The volume space velocity ratio of said hydrogenation unit 3-1 is 4; Hydrogen/oil volume ratio is 300; Service temperature is 250 ℃, and working pressure is 1.0MPa (cutting off); Said heavy petrol (boiling range is 90-205 ℃) gets into extracting and separating in the heavy petrol extraction system 2 with 5.7 ten thousand tons/year flows through pipeline, isolates aromatic hydrocarbons and raffinates oil; Solvent for use is the N-formyl morpholine in the said extraction system 2, and extraction temperature is 5 ℃ of youngsters, and solvent ratio (solvent/charging) is 3.5 (quality), and the washing of raffinating oil is than being 0.2 (quality), and the solvent recuperation temperature is 151 ℃, and solvent recuperation pressure is 0.112MPa (cutting off); Said aromatic hydrocarbons gets into aromatic hydrogenation device 3-2 hydrogenation with 1.5 ten thousand tons/year flow, and the catalyzer among the said hydrogenation unit 3-2 is whole hydrogenation catalyst GHT-22; The volume space velocity ratio of said hydrogenation unit 3-2 is 3; Hydrogen/oil volume ratio is 300; Service temperature is 325 ℃, and working pressure is 2.5MPa (cutting off); And then be in harmonious proportion said raffinating oil with 1.5 ten thousand tons/year flow with petroleum naphtha behind the said hydrogenation as the chemical industry light oil extraction.
The boiling range of gained blended gasoline is 30-205 ℃, and sulphur content is 10.0ppm, and mercaptans content is less than 1ppm; Olefin(e) centent is 17.84%, and (v), diene content is that (v), aromaticity content is 28.2% (v) less than 0.01%; Octane value (RON) is 94.05, and density is 721.4 kilograms/meter
3, produced quantity is 6.4 ten thousand tons/year.
The boiling range of gained chemical industry light oil is 90-205 ℃, and sulphur content is 10.0ppm, and mercaptans content is 1.0ppm, and olefin(e) centent is 58.3%, and (v), diene content is 0.01% (v), aromaticity content is that 3.0% (v), octane value (RON) is 82.0, and density is 740.0 kilograms/meter
3, produced quantity is 3.6 ten thousand tons/year.
Claims (7)
1. the device of a catalyzing hydrocarbon for recombinant production of high-quality gasoline comprises water distilling apparatus and extraction system; It is characterized in that: said water distilling apparatus top is provided with the petroleum naphtha pipeline; Said water distilling apparatus bottom is connected with extraction system through the heavy petrol pipeline; The bottom of said extraction system is connected with the aromatic hydrogenation device through pipeline, and said aromatic hydrogenation device is connected through the petroleum naphtha pipeline of pipeline with said water distilling apparatus top again; The top of said extraction system is through pipeline extraction chemical industry light oil.
2. the device of catalyzing hydrocarbon for recombinant production of high-quality gasoline according to claim 1, it is characterized in that: the top of said water distilling apparatus is connected with the petroleum naphtha hydrogenation unit through the petroleum naphtha pipeline.
3. the method for a catalyzing hydrocarbon for recombinant production of high-quality gasoline, its step is following: stable gasoline is added water distilling apparatus carry out fractionation, fractionate out petroleum naphtha and heavy petrol; Said petroleum naphtha steams through water distilling apparatus top; Said heavy petrol gets in the extraction system and carries out extracting and separating, isolates aromatic hydrocarbons and raffinates oil; The petroleum naphtha that steams with said water distilling apparatus top after the hydrotreatment of said aromatic hydrocarbons process aromatic hydrogenation device is in harmonious proportion and uses, and the said direct extraction of raffinating oil is as chemical industry light oil.
4. the method for catalyzing hydrocarbon for recombinant production of high-quality gasoline according to claim 3 is characterized in that: the petroleum naphtha of said water distilling apparatus through the petroleum naphtha hydrogenation device for treatment after again with hydrogenation after aromatic hydrocarbons be in harmonious proportion and become blended gasoline.
5. the method for catalyzing hydrocarbon for recombinant production of high-quality gasoline according to claim 4, it is characterized in that: the tower top temperature of said water distilling apparatus is 82～86 ℃, column bottom temperature is 190～192 ℃; The tower top pressure of said 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 said petroleum naphtha is controlled at 30 ℃～80 ℃; The boiling range of said heavy petrol is controlled at greater than 80 ℃ smaller or equal to 205 ℃.
6. the method for catalyzing hydrocarbon for recombinant production of high-quality gasoline according to claim 4, it is characterized in that: the tower top temperature of said water distilling apparatus is 82～86 ℃, column bottom temperature is 190～192 ℃; The tower top pressure of said water distilling apparatus is the 0.2MPa absolute pressure, and tower bottom pressure is the 0.25MPa absolute pressure; The boiling range of said petroleum naphtha is controlled at 30 ℃～80 ℃; The boiling range of said heavy petrol is controlled at greater than 80 ℃ smaller or equal to 205 ℃.
7. the method for catalyzing hydrocarbon for recombinant production of high-quality gasoline according to claim 4, it is characterized in that: the tower top temperature of said water distilling apparatus is 82～86 ℃, column bottom temperature is 190～192 ℃; The tower top pressure of said water distilling apparatus is the 0.2MPa absolute pressure, and tower bottom pressure is the 0.25MPa absolute pressure; The boiling range of said petroleum naphtha is controlled at 30 ℃～90 ℃; The boiling range of said heavy petrol is controlled at greater than 90 ℃ smaller or equal to 205 ℃.
Priority Applications (7)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2007101699475A CN101429447B (en) | 2007-11-09 | 2007-11-09 | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline |
| EP08855052A EP2236583A4 (en) | 2007-11-09 | 2008-11-05 | A system and process for producing high quality gasoline by catalytic hydrocarbon recombination |
| US12/682,034 US8524043B2 (en) | 2007-11-09 | 2008-11-05 | System for producing high quality gasoline by catalytic hydrocarbon recombination |
| JP2010532411A JP2011503264A (en) | 2007-11-09 | 2008-11-05 | System and method for producing high quality gasoline by recombining hydrocarbons by catalytic action |
| CA2705034A CA2705034C (en) | 2007-11-09 | 2008-11-05 | System and process for producing high quality gasoline by catalytic hydrocarbon recombination |
| EA201070499A EA201070499A1 (en) | 2007-11-09 | 2008-11-05 | SYSTEM AND METHOD FOR OBTAINING HIGH-QUALITY GASOLINE AS A RESULT OF CATALYTIC HYDROCARBON RECOMBINATION |
| PCT/CN2008/072943 WO2009067885A1 (en) | 2007-11-09 | 2008-11-05 | A system and process for producing high quality gasoline by catalytic hydrocarbon recombination |
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| CN2007101699475A CN101429447B (en) | 2007-11-09 | 2007-11-09 | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline |
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| CA1206908A (en) * | 1982-04-08 | 1986-07-02 | Alfons Jankowski | Carburetion fuel |
| CN1144259A (en) * | 1995-08-29 | 1997-03-05 | 巴陵石化长岭炼油化工总厂 | Method for producing extraction solvent naphtha by catalytic reforming device |
| CN1253993A (en) * | 1998-11-18 | 2000-05-24 | 法国石油公司 | Production method of low-sulfur gasoline |
| CN1470607A (en) * | 2003-07-04 | 2004-01-28 | 北京金伟晖工程技术有限公司 | Catalytic hydrocarbon reforming treatment method |
| CN1613976A (en) * | 2003-11-07 | 2005-05-11 | 丁冉峰 | Catalytic hydrocarbon recombinant treating method |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA1206908A (en) * | 1982-04-08 | 1986-07-02 | Alfons Jankowski | Carburetion fuel |
| CN1144259A (en) * | 1995-08-29 | 1997-03-05 | 巴陵石化长岭炼油化工总厂 | Method for producing extraction solvent naphtha by catalytic reforming device |
| CN1253993A (en) * | 1998-11-18 | 2000-05-24 | 法国石油公司 | Production method of low-sulfur gasoline |
| CN1470607A (en) * | 2003-07-04 | 2004-01-28 | 北京金伟晖工程技术有限公司 | Catalytic hydrocarbon reforming treatment method |
| CN1613976A (en) * | 2003-11-07 | 2005-05-11 | 丁冉峰 | Catalytic hydrocarbon recombinant treating method |
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