CN201144229Y - 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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- CN201144229Y CN201144229Y CNU2007203020943U CN200720302094U CN201144229Y CN 201144229 Y CN201144229 Y CN 201144229Y CN U2007203020943 U CNU2007203020943 U CN U2007203020943U CN 200720302094 U CN200720302094 U CN 200720302094U CN 201144229 Y CN201144229 Y CN 201144229Y
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- hydrogenation unit
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- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 19
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 19
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 17
- 230000003197 catalytic effect Effects 0.000 title abstract description 15
- 238000005215 recombination Methods 0.000 title abstract description 3
- 230000006798 recombination Effects 0.000 title abstract description 3
- 239000003502 gasoline Substances 0.000 claims abstract description 57
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 48
- 238000000605 extraction Methods 0.000 claims abstract description 31
- 239000003208 petroleum Substances 0.000 claims description 25
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 24
- 238000004519 manufacturing process Methods 0.000 claims description 7
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 30
- 150000001336 alkenes Chemical class 0.000 abstract description 20
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 abstract description 16
- 238000004821 distillation Methods 0.000 abstract description 14
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 abstract description 14
- 229910052717 sulfur Inorganic materials 0.000 abstract description 10
- 239000011593 sulfur Substances 0.000 abstract description 10
- 238000002360 preparation method Methods 0.000 abstract description 3
- 230000008901 benefit Effects 0.000 abstract description 2
- 239000000284 extract Substances 0.000 abstract 1
- 238000009835 boiling Methods 0.000 description 22
- 238000005520 cutting process Methods 0.000 description 22
- 239000005864 Sulphur Substances 0.000 description 21
- 239000003921 oil Substances 0.000 description 21
- 238000000034 method Methods 0.000 description 18
- 239000002904 solvent Substances 0.000 description 17
- 239000003054 catalyst Substances 0.000 description 12
- 150000001993 dienes Chemical class 0.000 description 10
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical class S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 9
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 9
- 239000002283 diesel fuel Substances 0.000 description 8
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 7
- 239000005977 Ethylene Substances 0.000 description 7
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 7
- 238000005194 fractionation Methods 0.000 description 7
- 239000001257 hydrogen Substances 0.000 description 7
- 229910052739 hydrogen Inorganic materials 0.000 description 7
- 230000008569 process Effects 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
- 238000004523 catalytic cracking Methods 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 239000003209 petroleum derivative Substances 0.000 description 4
- 239000011148 porous material Substances 0.000 description 4
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical compound CN1CCCC1=O SECXISVLQFMRJM-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
- 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
- 230000008521 reorganization Effects 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
- 238000007233 catalytic pyrolysis Methods 0.000 description 2
- 239000003269 fluorescent indicator Substances 0.000 description 2
- 239000000463 material Substances 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
- 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
- 238000004231 fluid catalytic cracking 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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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
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, the upper part of the distillation unit is provided with a light gasoline pipeline; the lower part of the distillation unit is connected with a heavy gasoline hydrogenation device via a heavy gasoline pipeline; the heavy gasoline hydrogenation device is connected with the extraction system via a pipeline; the lower part of the extraction system is connected with the light gasoline pipeline at the upper part of the distillation unit via a pipeline; the upper part of the extraction system directly extracts the products through the system. The utility model has the advantages that the cost of the system is low, the content of sulfur in the mixed gasoline is lower, the content of olefin is lower, and the octane rating in the gasoline is high.
Description
Technical field
The utility model relates to a kind of system of catalyzing hydrocarbon for recombinant production of high-quality gasoline.
Background technology
Catalytic cracking, catalytic pyrolysis and heavy oil catalytic pyrolysis technology are the core technologies of oil refining, and catalytic cracking is divided into wax catalysis cracking, heavy oil fluid catalytic cracking; Be referred to as catalytic hydrocarbon from the generation oil of these explained hereafter, the gained catalytic hydrocarbon is through processing treatment, generally be the separation column fractionation, can fractionate out products such as net gas, liquefaction vapour, gasoline, diesel oil, heavy oil, wherein gasoline, more than 70% of diesel oil total supply on gasoline, the diesel oil occuping market.
More and more strictness along with environmental requirement, the standard of gasoline, diesel oil improves constantly, existing catalytic hydrocarbon is showed following deficiency through the fractionated processing and treating method of separation column: one is that the gasoline produced of this treatment process and the quality of diesel oil have much room for improvement: the olefin(e) centent of gasoline is higher, (RON) is on the low side for octane value, diesel-fuel cetane number is on the low side, and stability is undesirable; The 2nd, above-mentioned treatment process can not be produced the gasoline of multiple label simultaneously, and range of product is single; The 3rd, the demand in the diesel oil of being produced, the ratio of gasoline and market does not match, and diesel oil can not satisfy the demands, and gasoline supply exceed demand.
In order to address the above problem, the patent No. is that the Chinese invention patent of 03148181.7 " catalytic hydrocarbon reorganization treatment process " provides a kind of catalytic hydrocarbon reorganization treatment process, and the patent No. is respectively 200310103541.9 and 200310103540.4 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).For most refinery, must require in the face of higher national IV gasoline standard: sulphur content is not more than 0.005% (wt), alkene and is not more than 25% (v) or lower.The quality of gasoline solution must be considered the transition from national III gasoline standard to national IV gasoline standard, and programme should be disposable according to national IV gasoline standard programme preferably.
Because ratio and developed country's difference of each blend component is very big in China's gasoline products, catalytically cracked gasoline occupies very high ratio, and reformed gasoline, gasoline alkylate proportion are less, and this situation is with long-term existence.Therefore, the quality of gasoline upgrading problem of falling sulphur and falling alkene to be solved relates generally to the problem of catalytic gasoline.
It is generally acknowledged, the 5-10% of total sulfur will enter gasoline in the catalytically cracked material,, secondary processing catalytic cracking ability very little according to China's refinery fcc raw material hydrofining ability is big and the characteristics of residuum coking are arranged, the about 200ppm of refinery catalytic gasoline sulphur content of processing low-sulfur (sulfur-bearing 0.3%) crude oil, the crude oil of processing sulfur-bearing 0.8%, the about 900ppm of sulphur content in the catalytic gasoline, therefore, the difficult point of quality of gasoline upgrading changes the problem of sulphur into from alkene.The improvement of catalytic cracking process or catalyzer can not fundamentally solve the problem of sulphur, the catalytically cracked material hydrogenating desulfurization is because investment is big, working cost is high, existing refinery condition is limited and impossible large-scale application, and it is also inapplicable for the refinery of the low sulphur-bearing crude of processing, simultaneously, catalytic cracking unit excessively reduces the loss that alkene also can aggravate light-end products and gasoline octane rating (RON).
Therefore, provide the treatment system of the high blended gasoline of a kind of low-cost preparation low sulfur content, low olefin-content and octane value (RON) just to become the technical barrier that this technical field is badly in need of solution.
Summary of the invention
The purpose of this utility model provides a kind of catalytic hydrocarbon recombination system of gasoline of low-cost preparation low sulfur content, low olefin-content and boosting of octane rating (RON).
For achieving the above object, the utility model is taked following technical scheme:
A kind of system of catalyzing hydrocarbon for recombinant production of high-quality gasoline comprises water distilling apparatus and extraction system, it is characterized in that: described water distilling apparatus top is provided with the petroleum naphtha pipeline; Described water distilling apparatus bottom is connected with the heavy petrol hydrogenation unit by the heavy petrol pipeline; Described heavy petrol hydrogenation unit is connected with extraction system by pipeline; The bottom of described extraction system is connected by the petroleum naphtha pipeline of pipeline with described water distilling apparatus top; The top of described extraction system is by the direct extraction product of pipeline.
A kind of preferred version is characterized in that: the top of described water distilling apparatus is connected with hydrogenation unit by the petroleum naphtha pipeline.
A kind of method of catalyzing hydrocarbon for recombinant production of high-quality gasoline, its step is as follows: stable gasoline is added water distilling apparatus carry out fractionation, fractionate out petroleum naphtha and heavy petrol; Described petroleum naphtha steams by water distilling apparatus top; The hydrotreatment in hydrogenation unit of described heavy petrol enters then and carries out extracting and separating in the extraction system, isolates aromatic hydrocarbons and raffinates oil; The petroleum naphtha that described aromatic hydrocarbons steams by pipeline and water distilling apparatus top is in harmonious proportion and uses, and the described direct extraction of raffinating oil is as feed ethylene.
A kind of preferred version is characterized in that: the petroleum naphtha that described water distilling apparatus top steams is by hydrotreatment.
A kind of preferred version is characterized in that: the tower top temperature of described water distilling apparatus is 82～86 ℃, and column bottom temperature is 186～192 ℃; 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 ℃～65 ℃; The boiling range of described heavy petrol is controlled at 65 ℃～205 ℃.
A kind of preferred version is characterized in that: the tower top temperature of described water distilling apparatus is 82～86 ℃, and column bottom temperature is 186～192 ℃; 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 described heavy petrol is controlled at 90 ℃～205 ℃.
A kind of preferred version is characterized in that: the tower top temperature of described water distilling apparatus is 82～86 ℃, and column bottom temperature is 186～192 ℃; 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 described heavy petrol is controlled at 80 ℃～205 ℃.
A kind of preferred version is characterized in that: the catalyzer in the described petroleum naphtha hydrogenation unit is selective hydrogenation catalyst GHT-20; The volume space velocity ratio of described petroleum naphtha hydrogenation unit is 2～4; Hydrogen/oil volume ratio is 150～300; Service temperature is 220～280 ℃, and working pressure is 0.6～2MPa (cutting off).
A kind of preferred version is characterized in that: the physico-chemical property of the selective hydrogenation catalyst GHT-20 in the described petroleum naphtha hydrogenation unit is as shown in 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 |
A kind of preferred version is characterized in that: the catalyzer in the described heavy petrol hydrogenation unit is whole hydrogenation catalyst GHT-22; The volume space velocity ratio of described heavy petrol hydrogenation unit is 2～4; Hydrogen/oil volume ratio is 250～350; Service temperature is 290～330 ℃, and working pressure is 1.2～3MPa (cutting off).
A kind of preferred version is characterized in that: the physico-chemical property of the whole hydrogenation catalyst GHT-22 in the described heavy petrol hydrogenation unit is as shown in the table.
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: the catalyzer of used light, heavy petrol hydrogenation unit is respectively at light, heavy petrol, the parameter of described hydrogenation unit has more specific aim, the sulphur content of gained blended gasoline is lower, olefin(e) centent also lower (below 1%).
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. 1-1 is the schematic flow sheet of the utility model embodiment 1.
Fig. 1-2 is the schematic flow sheet of the utility model embodiment 2.
Fig. 2 is the schematic flow sheet of the utility model embodiment 3.
Embodiment
Embodiment 1
As Figure 1-1, be the schematic flow sheet of present embodiment.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 (RON), 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 ℃, column bottom temperature is 186 ℃, tower top pressure is 0.2MPa (cutting off), tower bottom pressure is 0.25MPa (cutting off), obtains petroleum naphtha and heavy petrol respectively, and described petroleum naphtha (boiling range is 30-80 ℃) steams by distillation tower 1 top, its total amount of steaming is 40,000 tons/year, enters hydrogenation unit 3-1 hydrotreatment then; The catalyzer of described hydrogenation unit 3-1 is selective hydrogenation catalyst GHT-20; The volume space velocity ratio of described hydrogenation unit 3-1 is 2; Hydrogen/oil volume ratio is 150; Service temperature is 220 ℃, and working pressure is 0.6MPa (cutting off); Described heavy petrol (boiling range is 80-205 ℃) enters hydrogenation unit 3-2 hydrotreatment with 60,000 tons/year flows; Catalyzer among the described heavy petrol hydrogenation unit 3-2 is whole hydrogenation catalyst GHT-22; The volume space velocity ratio of described hydrogenation unit 3-2 is 2; Hydrogen/oil volume ratio is 250; Service temperature is 290 ℃, and working pressure is 1.2MPa (cutting off); Enter extracting and separating in the heavy petrol extraction system 2 by pipeline then, isolate aromatic hydrocarbons and raffinate oil; Solvent for use is a N-Methyl pyrrolidone in the described extraction system 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 151 ℃, and solvent recuperation pressure is 0.112MPa (cutting off); Described aromatic hydrocarbons is in harmonious proportion with 1.5 ten thousand tons/year flow and the petroleum naphtha behind the described hydrogenation, described raffinating oil with 4.5 ten thousand tons/year flow as the high-quality ethylene extraction.
The boiling range of gained blended gasoline is 30-205 ℃, and sulphur content is 5.27ppm, 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 high-quality ethylene is 80-205 ℃, and sulphur content is 2.0ppm, and mercaptans content is less than 1ppm, olefin(e) centent is that (v), diene content is that (v), aromaticity content is 3.0% (v) less than 0.01% less than 0.1%, 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 described selective hydrogenation catalyst GHT-20 is as shown in the table.
| 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 physico-chemical property of described whole hydrogenation catalyst GHT-22 is as shown in the table.
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
Shown in Fig. 1-2, be the schematic flow sheet of present 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 (RON), 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 ℃, column bottom temperature is 192 ℃, tower top pressure is 0.2MPa (cutting off), tower bottom pressure is 0.25MPa (cutting off), and fractionation obtains petroleum naphtha and heavy petrol respectively, and described petroleum naphtha (boiling range is 30-90 ℃) steams by distillation tower 1 top, its total amount of steaming is 4.3 ten thousand tons/year, enters hydrogenation unit 3-1 hydrotreatment then; The catalyzer of described hydrogenation unit 3-1 is selective hydrogenation catalyst GHT-20; The volume space velocity ratio of described hydrogenation unit 3-1 is 4; Hydrogen/oil volume ratio is 300; Service temperature is 280 ℃, and working pressure is 2.0MPa (cutting off); Described heavy petrol (boiling range is 90-205 ℃) enters hydrogenation unit 3-2 hydrotreatment with 5.7 ten thousand tons/year flows; Catalyzer among the described heavy petrol hydrogenation unit 3-2 is selective hydrogenation catalyst GHT-20; The volume space velocity ratio of described hydrogenation unit 3-2 is 4; Hydrogen/oil volume ratio is 350; Service temperature is 330 ℃, and working pressure is 3.0MPa (cutting off); Enter extracting and separating in the heavy petrol extraction system 2 by pipeline then, isolate aromatic hydrocarbons and raffinate oil; Solvent for use is a N-Methyl pyrrolidone in the described extraction system 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 151 ℃, and solvent recuperation pressure is 0.112MPa (cutting off); Described aromatic hydrocarbons is in harmonious proportion with 1.9 ten thousand tons/year flow and the petroleum naphtha behind the described hydrogenation, described raffinating oil with 3.8 ten thousand tons/year flow as the high-quality ethylene extraction.
The boiling range of gained blended gasoline is 30-205 ℃, and sulphur content is 7.52ppm, and mercaptans content is less than 1ppm, olefin(e) centent is 17.99%, and (v), diene content is that (v), aromaticity content is 29.1% (v) less than 0.01%, octane value (RON) is 95.2, and density is 720.1 kilograms/meter
3, produced quantity is 6.2 ten thousand tons/year.
The boiling range of gained high-quality ethylene is 90-205 ℃, and sulphur content is 2.0ppm, and mercaptans content is less than 1ppm, olefin(e) centent is 6%, and (v), diene content is that (v), aromaticity content is 3.0% (v) less than 0.01%, octane value (RON) is 81.5, and density is 740.0 kilograms/meter
3, produced quantity is 3.8 ten thousand tons/year.
Embodiment 3
As shown in Figure 2, be the schematic flow sheet of present 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 (RON), 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 ℃, column bottom temperature is 186 ℃, 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 described petroleum naphtha (boiling range is 30-80 ℃) steams by distillation tower 1 top, and its total amount of steaming is 40,000 tons/year; Described heavy petrol (boiling range is 80-205 ℃) enters hydrogenation unit 3 hydrotreatments with 60,000 tons/year flows; Catalyzer in the described heavy petrol hydrogenation unit 3 is whole hydrogenation catalyst GHT-22; The volume space velocity ratio of described hydrogenation unit 3 is 3; Hydrogen/oil volume ratio is 250; Service temperature is 290 ℃, and working pressure is 1.2MPa (cutting off); Enter extracting and separating in the heavy petrol extraction system 2 by pipeline then, isolate aromatic hydrocarbons and raffinate oil; The extraction solvent for use is a N-Methyl pyrrolidone in the described extraction system 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 151 ℃, and solvent recuperation pressure is 0.112MPa (cutting off); Described aromatic hydrocarbons is in harmonious proportion with 1.6 ten thousand tons/year flow and described petroleum naphtha, described raffinating oil with 4.4 ten thousand tons/year flow as the high-quality ethylene extraction.
The boiling range of gained blended gasoline is 30-205 ℃, and sulphur content is 8.89ppm, and mercaptans content is 2.86ppm, olefin(e) centent is 18.82%, and (v), diene content is 0.04% (v), aromaticity content is 25.1% (v), octane value (RON) is 94.5, and density is 704.7 kilograms/meter
3, produced quantity is 5.6 ten thousand tons/year.
The boiling range of gained high-quality ethylene is 80-205 ℃, and sulphur content is 0.5ppm, and mercaptans content is less than 1ppm, olefin(e) centent is that (v), diene content is that (v), aromaticity content is 3.0% (v) less than 0.01% less than 0.1%, octane value (RON) is 79.7, and density is 760.0 kilograms/meter
3, produced quantity is 4.4 ten thousand tons/year.
Claims (2)
1, a kind of system of catalyzing hydrocarbon for recombinant production of high-quality gasoline comprises water distilling apparatus and extraction system, it is characterized in that: described water distilling apparatus top is provided with the petroleum naphtha pipeline; Described water distilling apparatus bottom is connected with the heavy petrol hydrogenation unit by the heavy petrol pipeline; Described heavy petrol hydrogenation unit is connected with extraction system by pipeline; The bottom of described extraction system is connected by the petroleum naphtha pipeline of pipeline with described water distilling apparatus top; The top of described extraction system is by the direct extraction product of pipeline.
2, the system of catalyzing hydrocarbon for recombinant production of high-quality gasoline according to claim 1 is characterized in that: the top of described water distilling apparatus is connected with hydrogenation unit by the petroleum naphtha pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007203020943U CN201144229Y (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 |
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| CNU2007203020943U CN201144229Y (en) | 2007-11-09 | 2007-11-09 | System for preparing high-quality petrol by recombination of catalytic hydrocarbon |
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| CN201144229Y true CN201144229Y (en) | 2008-11-05 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2009067885A1 (en) * | 2007-11-09 | 2009-06-04 | Ranfeng Ding | A system and process for producing high quality gasoline by catalytic hydrocarbon recombination |
| CN102021024A (en) * | 2009-09-18 | 2011-04-20 | 北京金伟晖工程技术有限公司 | System for producing diesel of high quality and method thereof |
| CN101429449B (en) * | 2007-11-09 | 2012-10-10 | 丁冉峰 | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline |
-
2007
- 2007-11-09 CN CNU2007203020943U patent/CN201144229Y/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2009067885A1 (en) * | 2007-11-09 | 2009-06-04 | Ranfeng Ding | A system and process for producing high quality gasoline by catalytic hydrocarbon recombination |
| CN101429449B (en) * | 2007-11-09 | 2012-10-10 | 丁冉峰 | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline |
| CN102021024A (en) * | 2009-09-18 | 2011-04-20 | 北京金伟晖工程技术有限公司 | System for producing diesel of high quality and method thereof |
| CN102021024B (en) * | 2009-09-18 | 2014-03-26 | 北京金伟晖工程技术有限公司 | System for producing diesel of high quality and method thereof |
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