CN201158633Y - System for producing high quality gasoline by catalyzing hydrocarbon regrouping - Google Patents
System for producing high quality gasoline by catalyzing hydrocarbon regrouping Download PDFInfo
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- CN201158633Y CN201158633Y CNU2007203020981U CN200720302098U CN201158633Y CN 201158633 Y CN201158633 Y CN 201158633Y CN U2007203020981 U CNU2007203020981 U CN U2007203020981U CN 200720302098 U CN200720302098 U CN 200720302098U CN 201158633 Y CN201158633 Y CN 201158633Y
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- gasoline
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- extraction system
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- 239000003502 gasoline Substances 0.000 title claims abstract description 107
- 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
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 78
- 238000000605 extraction Methods 0.000 claims abstract description 49
- 125000003118 aryl group Chemical group 0.000 claims abstract description 27
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 19
- 238000005520 cutting process Methods 0.000 claims description 29
- 239000003208 petroleum Substances 0.000 claims description 21
- 239000002283 diesel fuel Substances 0.000 claims description 17
- 238000004519 manufacturing process Methods 0.000 claims description 7
- 238000005345 coagulation Methods 0.000 claims description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 33
- 150000001336 alkenes Chemical class 0.000 abstract description 23
- 238000004821 distillation Methods 0.000 abstract description 19
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 abstract description 15
- 239000003054 catalyst Substances 0.000 abstract description 13
- 230000003197 catalytic effect Effects 0.000 abstract description 13
- 229910052717 sulfur Inorganic materials 0.000 abstract description 10
- 239000011593 sulfur Substances 0.000 abstract description 10
- 238000001833 catalytic reforming Methods 0.000 abstract 1
- 230000000694 effects Effects 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 51
- 238000009835 boiling Methods 0.000 description 34
- 239000002904 solvent Substances 0.000 description 31
- 239000005864 Sulphur Substances 0.000 description 24
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 21
- 238000000034 method Methods 0.000 description 17
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 15
- 150000001993 dienes Chemical class 0.000 description 12
- LCEDQNDDFOCWGG-UHFFFAOYSA-N morpholine-4-carbaldehyde Chemical compound O=CN1CCOCC1 LCEDQNDDFOCWGG-UHFFFAOYSA-N 0.000 description 12
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical class S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 11
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 8
- 238000005194 fractionation Methods 0.000 description 8
- 239000001257 hydrogen Substances 0.000 description 8
- 229910052739 hydrogen Inorganic materials 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
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 6
- 238000003556 assay Methods 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- 238000005406 washing Methods 0.000 description 6
- 238000004523 catalytic cracking Methods 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- 239000003209 petroleum derivative Substances 0.000 description 4
- 239000011148 porous material Substances 0.000 description 4
- 239000000126 substance Substances 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
- 239000000295 fuel oil Substances 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
- 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
- 230000006872 improvement Effects 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
- HRKQOINLCJTGBK-UHFFFAOYSA-N dihydroxidosulfur Chemical compound OSO HRKQOINLCJTGBK-UHFFFAOYSA-N 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
- 238000005215 recombination Methods 0.000 description 1
- 230000006798 recombination Effects 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 system for preparing high-quality gasoline by catalytic-reforming hydrocarbon. The system is characterized in that a hydrogenation unit is connected with a distillation unit; light and heavy gasoline pipelines are respectively disposed at the upper and the lower parts of the distillation unit, and a middle gasoline pipeline is disposed at the middle part of the distillation unit; the light and heavy gasoline pipelines are respectively connected with an extraction unit, upper and lower parts of which are respectively connected with a water wash system and the light gasoline pipeline at the upper part of a catalytic unit via pipeline; and the middle gasoline is respectively provided with hydrogenation units after being subjected to the extracted. Compared with the prior art, the catalyst and parameters in the adopted raffinate oil hydrogenation unit and the aromatic hydrogenation unit are more targeted, and the sulfur and olefin reduction effects are remarkable.
Description
Technical field
The utility model relates to a kind of catalytic hydrocarbon recombinant processing system, particularly a kind of system of catalyzing hydrocarbon for recombinant production of high-quality gasoline.
Background technology
Catalytic cracking, catalytic pyrolysis and heavy oil catalytic pyrolysis technology are the core technologies of oil refining, and catalytic cracking is divided into wax catalysis cracking, heavy oil fluid catalytic cracking; Be referred to as catalytic hydrocarbon from the generation oil of these explained hereafter, the gained catalytic hydrocarbon is through processing treatment, generally be the separation column fractionation, can fractionate out products such as net gas, liquefaction vapour, gasoline, diesel oil, heavy oil, wherein gasoline, more than 70% of diesel oil total supply on gasoline, the diesel oil occuping market.
More and more strictness along with environmental requirement, the standard of gasoline, diesel oil improves constantly, existing catalytic hydrocarbon is showed following deficiency through the fractionated processing and treating method of separation column: one is that the gasoline produced of this treatment process and the quality of diesel oil have much room for improvement: the olefin(e) centent of gasoline is higher, (RON) is on the low side for octane value, diesel-fuel cetane number is on the low side, and stability is undesirable; The 2nd, above-mentioned treatment process can not be produced the gasoline of multiple label simultaneously, and range of product is single; The 3rd, the demand in the diesel oil of being produced, the ratio of gasoline and market does not match, and diesel oil can not satisfy the demands, and gasoline supply exceed demand.
The patent No. is the Chinese invention patent of 03148181.7 " catalytic hydrocarbon reorganization treatment process ", and the patent No. is respectively 200310103541.9 and 200310103540.4 and discloses it and improve patent, but all do not mention the problem of how to fall sulphur and falling alkene in these patents.
Present GB17930 gasoline standard requires sulphur content to be not more than 0.05% (wt), olefin(e) centent to be not more than 35% (v), benzene content is not more than 2.5% (v), most refinerys can guarantee quality of gasoline.But, the state III gasoline standard requirement sulphur content that is about to implement in 2010 is not more than 0.015% (wt), alkene is not more than 30% (v), benzene content is not more than 1% (v), for most refinery, must be in the face of higher state IV standards requirement, promptly sulphur content ≯ 0.005% (wt), alkene ≯ 25% are (v) or lower.The quality of gasoline solution must be considered the transition from state III to state IV standards, and programme should be disposable according to state IV gasoline standard programme preferably.
Because ratio and developed country's difference of each blend component is very big in China's gasoline products, catalytically cracked gasoline occupies very high ratio, and reformed gasoline, gasoline alkylate proportion are less, and this situation is with long-term existence.Therefore, upgrade sulphur to be solved and alkene of quality of gasoline mainly is the problem that solves catalytic gasoline.
It is generally acknowledged, the 5-10% of total sulfur will enter gasoline in the catalytically cracked material,, secondary processing catalytic cracking ability very little according to China's refinery fcc raw material hydrofining ability is big and the characteristics of residuum coking are arranged, the about 200ppm of refinery catalytic gasoline sulphur content of processing low-sulfur (sulfur-bearing 0.3%) crude oil, the crude oil of processing sulfur-bearing 0.8%, the about 900ppm of sulphur content in the catalytic gasoline, therefore, the difficult point of quality of gasoline upgrading changes the problem of sulphur into from alkene.The improvement of catalytic cracking process or catalyzer can not fundamentally solve the problem of sulphur, the catalytically cracked material hydrogenating desulfurization is because investment is big, working cost is high, existing refinery condition is limited and impossible large-scale application, and it is also inapplicable for the refinery of the low sulphur-bearing crude of processing, simultaneously, catalytic cracking unit excessively reduces the loss that alkene also can aggravate light-end products and gasoline octane rating (RON).
Therefore, 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 low-cost preparation low sulfur content, low olefin-content and boosting of octane rating (RON) gasoline.
For achieving the above object, the utility model is taked following technical scheme:
A kind of system of catalyzing hydrocarbon for recombinant production of high-quality gasoline comprises water distilling apparatus and extraction system, it is characterized in that: described water distilling apparatus bottom is provided with the heavy petrol pipeline; The middle part of described water distilling apparatus is provided with middle medium gasoline pipeline; Medium gasoline pipeline is connected with middle gasoline extraction system in described; Gasoline extraction system top is connected with the hydrogenation unit of raffinating oil by pipeline in described; The bottom of gasoline extraction system is connected with the aromatic hydrogenation device by pipeline in described, and then is connected with the petroleum naphtha pipeline on water distilling apparatus top by pipeline; Be provided with light-middle gasoline cutting mouth in described between gasoline cutting mouth and the described water distilling apparatus top, and be connected with described aromatic hydrogenation device by pipeline; Described heavy petrol pipeline is connected with the heavy petrol extraction system; The bottom of described heavy petrol extraction system is connected with described aromatic hydrogenation device by pipeline; Described heavy petrol extraction system top is connected by the hydrogenation unit of raffinating oil of pipeline with described middle gasoline, perhaps directly goes out the low-coagulation diesel oil product.
A kind of optimal technical scheme is characterized in that: the described hydrogenation unit of raffinating oil is by being connected with extraction system.
A kind of method of catalyzing hydrocarbon for recombinant production of high-quality gasoline, its step is as follows: stable gasoline enters water distilling apparatus and carries out fractionation, fractionates out petroleum naphtha, light-middle gasoline, middle gasoline and heavy petrol; Described petroleum naphtha steams by water distilling apparatus top; The gasoline extraction system carried out extracting and separating during gasoline entered by pipeline in described, isolated aromatic hydrocarbons and raffinated oil; The petroleum naphtha that described aromatic hydrocarbons steams with water distilling apparatus top after by aromatic hydrogenation device hydrogenation again is in harmonious proportion and uses; Gasoline is raffinated oil behind the hydrogenation directly as feed ethylene in described, perhaps passes through the extraction system extracting and separating again, obtains reformer feed and diesel oil respectively; Described light-middle gasoline enters the hydrotreatment of described aromatic hydrogenation device, and then be in harmonious proportion with petroleum naphtha through hydrotreatment; Described heavy petrol enters heavy petrol extraction system extracting and separating by pipeline, isolates aromatic hydrocarbons and raffinates oil; Described aromatic hydrocarbons with described in after the gasoline extracting aromatic hydrocarbons and described petroleum naphtha 2 mixes after hydrotreatment, the petroleum naphtha mediation that steams with distillation top again; Described heavy petrol extraction back gained raffinate oil with middle gasoline after raffinating oil after the extracting is in harmonious proportion through hydrotreatment as high-quality ethylene, perhaps handle through extracting again and obtain reformer feed and diesel oil respectively.
A kind of preferred version is characterized in that: the tower top temperature of described water distilling apparatus is 67～68 ℃, and column bottom temperature is 186～188 ℃; 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 ℃; Described light-boiling range of middle gasoline is controlled at 65 ℃～90 ℃; The boiling range of gasoline is controlled at 90 ℃～160 ℃ in described; The boiling range of described heavy petrol is controlled at 160 ℃～205 ℃.
A kind of preferred version is characterized in that: the catalyzer in the described hydrogenation unit of raffinating oil is selective hydrogenation catalyst GHT-20; The volume space velocity ratio of the described hydrogenation unit of raffinating oil is 2～4; Hydrogen/oil volume ratio is 250～350; 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 selective hydrogenation catalyst GHT-20 in the described hydrogenation unit of raffinating oil 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 |
| C0O | m％ | 0.16 |
A kind of preferred version is characterized in that: the catalyzer in the described aromatic hydrogenation device is whole hydrogenation catalyst GHT-22; The volume space velocity ratio of described aromatic hydrogenation device is 2～4; Hydrogen/oil volume ratio is 250～350; 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 described aromatic hydrogenation device is as shown in table 2 below.
Table 2
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: earlier through after the reorganization, repeated hydrogenation, catalyzer and parameter in the used hydrogenation unit have more specific aim, the sulphur content of gained blended gasoline is lower, olefin(e) centent is also lower, and with low cost; Described light-cutting of middle gasoline further reduces the content of sulphur and alkene in the blended gasoline; The utility model is applicable to the processing of the stable gasoline of low thioalcohol and low olefin-content.
Below by the drawings and specific embodiments the utility model is described further, but and does not mean that restriction the utility model protection domain.
Description of drawings
Fig. 1 is the schematic flow sheet of the utility model embodiment 1.
Fig. 2 is the schematic flow sheet of the utility model embodiment 2.
Fig. 3 is the schematic flow sheet of the utility model embodiment 3.
Embodiment
Embodiment 1
As shown in Figure 1, be the schematic flow sheet of the utility model embodiment.With boiling range is 30-205 ℃, and sulphur content is 300ppm, and mercaptans content is 8.0ppm, and olefin(e) centent is 40%, and (v), diene content is 1% (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 67 ℃, column bottom temperature is 186 ℃, light-middle gasoline boiling range is 65-90 ℃; Middle gasoline boiling range is 90-160 ℃.Tower top pressure is 0.2MPa (cutting off), and tower bottom pressure is 0.25MPa (cutting off), and fractionation obtains petroleum naphtha, light-middle gasoline, middle gasoline and heavy petrol respectively, and described petroleum naphtha (boiling range is 30-65 ℃) steams by distillation tower 1 top, and its amount of steaming is 20,000 tons/year; Carry out extracting and separating among the gasoline extraction system 2-1 during gasoline (boiling range is 90-160 ℃) enters by pipeline with 2.5 ten thousand tons/year flows in described, isolate aromatic hydrocarbons and raffinate oil; The extraction solvent for use is the N-formyl morpholine among the described extraction system 2-1, 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 0.13MPa (cutting off); Described aromatic hydrocarbons with 0.6 ten thousand tons/year flow by pipeline in aromatic hydrogenation device 3-2 behind the hydrogenation, the petroleum naphtha behind hydrogenation that steams by pipeline and distillation tower 1 top is in harmonious proportion again, and the catalyzer among the described aromatic hydrogenation device 3-2 is selective hydrogenation catalyst GHT-20; The volume space velocity ratio of described aromatic hydrogenation device 3-2 is 2; Hydrogen/oil volume ratio is 250; Service temperature is 285 ℃, and working pressure is 1.5MPa (cutting off); Described raffinating oil connects as feed ethylene after by the hydrogenation unit 3-1 hydrogenation of raffinating oil with 1.9 ten thousand tons/year flow, and the catalyzer among the described hydrogenation unit 3-1 that raffinates oil is selective hydrogenation catalyst GHT-20; The volume space velocity ratio of the described hydrogenation unit 3-1 that raffinates oil is 2; Hydrogen/oil volume ratio is 250; Service temperature is 285 ℃, and working pressure is 1.5MPa (cutting off); Described light-middle gasoline (boiling range is 65-90 ℃) enters described aromatic hydrogenation device 3-2 with 2.5 ten thousand tons/year flows by pipeline; Described heavy petrol (boiling range is 160-205 ℃) enters extracting and separating among the heavy petrol extraction system 2-2 with 30,000 tons/year flows by pipeline, isolates aromatic hydrocarbons and raffinates oil; The extraction solvent for use is the N-formyl morpholine among the described extraction system 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 151 ℃, and solvent recuperation pressure is 0.112MPa (cutting off); Described aromatic hydrocarbons with 1.2 ten thousand tons/year flow with described in after aromatic hydrocarbons after the gasoline extracting mixes, enter aromatic hydrogenation device 3-2 hydrogenation, and then with described petroleum naphtha mediation; Described raffinate oil with 1.8 ten thousand tons/year flow and middle gasoline after raffinating oil after the extracting is mixed through hydrotreatment as high-quality ethylene.
The boiling range of gained blended gasoline is 30-205 ℃, and sulphur content is 36.8ppm, and mercaptans content is 3.2ppm, olefin(e) centent is 1.0%, and (v), diene content is that (v), aromaticity content is 4.0% (v) less than 0.01%, octane value (RON) is 74.2, and density is 759.2 kilograms/meter
3, produced quantity is 6.3 ten thousand tons/year.
The boiling range of gained high-quality ethylene is 65-160 ℃, and sulphur content is 5.0ppm, and mercaptans content is less than 1ppm, olefin(e) centent is 1.0%, and (v), diene content is that (v), aromaticity content is 4.0% (v) less than 0.01%, octane value (RON) is 74.7, and density is 759.2 kilograms/meter
3, produced quantity is 3.7 ten thousand tons/year.
The physico-chemical property of described selective hydrogenation catalyst GHT-20 is as shown in table 3 below.
Table 3
| Index name | Unit | Index |
| Outward appearance | The grey trilobal cross | |
| Specification | mm | φ1.7 |
| Intensity | N/cm | 170 |
| Bulk density | g/ml | 0.70 |
| Specific surface | m 2/g | 180 |
| Pore volume | ml/g | 0.55 |
| WO 3 | m％ | 6.6 |
| NiO | m％ | 2.1 |
| C 0O | m％ | 0.16 |
The used measuring method of the utility model is (down together):
1, boiling range: GB/T6536-1997 measured for petroleum product distillation method;
2, sulphur content: the total sulfur content assay method (ultraviolet fluorescence method) of SH/T0689-2000 light hydrocarbon and motor spirit and other oil products;
3, mercaptan sulfur: mercaptan sulfur assay method (potentiometric titration) in the GB/T1792-1988 distillate fuel oil;
4, alkene: GB/T11132-2002 liquid petroleum product hydro carbons assay method (fluorescent indicator adsorption method);
5, aromatic hydrocarbons: GB/T11132-2002 liquid petroleum product hydro carbons assay method (fluorescent indicator adsorption method);
6, octane value: GB/T5487 testing octane number of gasoline method (organon);
7, density: GB/T1884-2000 crude oil and liquid petroleum product density experiment chamber assay method (densimeter method);
8, the mensuration of diene: volumetry.
9, hydrogenation catalyst analytical procedure:
| Chemical constitution | Analytical procedure | The petrochemical industry standard that adopts |
| NiO | Colorimetry | SH/T0346-1992 |
| CoO | Colorimetry | SH/T0345-1992 |
| WO 3 | Colorimetry | |
| Physical property | Analytical procedure | The instrument that uses |
| Surface-area | Low-temperature nitrogen adsorption method | 2400 types absorption instrument |
| Pore volume | Mercury penetration method | Auto Pore II 9200 |
| Intensity | The crush strength assay method | DLII type intelligence granule strength determinator |
| Bulk density | Weighing method |
Embodiment 2
As shown in Figure 2, be the schematic flow sheet of the utility model embodiment.With boiling range is 30-205 ℃, and sulphur content is 300ppm, and mercaptans content is 8.0ppm, and olefin(e) centent is 40%, and (v), diene content is 1% (v), aromaticity content is that 19% (v), octane value (RON) is 91, and density is 728 kilograms/meter
3Stable gasoline in distillation tower 1, cut fractionation with 100,000 tons/year flow, the tower top temperature of distillation tower 1 is 67 ℃, column bottom temperature is 186 ℃, light-middle gasoline boiling range is 65-90 ℃; Middle gasoline boiling range is 90-160 ℃.Tower top pressure is 0.2MPa (cutting off), and tower bottom pressure is 0.25MPa (cutting off), and fractionation obtains petroleum naphtha, light-middle gasoline, middle gasoline and heavy petrol respectively, and described petroleum naphtha (boiling range is 30-65 ℃) steams by distillation tower 1 top, and its amount of steaming is 20,000 tons/year; Carry out extracting and separating among the gasoline extraction system 2-1 during gasoline (boiling range is 90-160 ℃) enters by pipeline with 2.5 ten thousand tons/year flows in described, isolate aromatic hydrocarbons and raffinate oil; The extraction solvent for use is the N-formyl morpholine among the described extraction system 2-1, 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 0.13MPa (cutting off); Described aromatic hydrocarbons with 0.6 ten thousand tons/year flow by pipeline in aromatic hydrogenation device 3-2 behind the hydrogenation, the petroleum naphtha behind hydrogenation that steams by pipeline and distillation tower 1 top is in harmonious proportion again, and the catalyzer among the described aromatic hydrogenation device 3-2 is selective hydrogenation catalyst GHT-20; The volume space velocity ratio of described aromatic hydrogenation device 3-2 is 3; Hydrogen/oil volume ratio is 300; Service temperature is 305 ℃, and working pressure is 2.0MPa (cutting off); Described raffinating oil connects as feed ethylene after by the hydrogenation unit 3-1 hydrogenation of raffinating oil with 1.9 ten thousand tons/year flow, and the catalyzer among the described hydrogenation unit 3-1 that raffinates oil is selective hydrogenation catalyst GHT-20; The volume space velocity ratio of the described hydrogenation unit 3-1 that raffinates oil is 3; Hydrogen/oil volume ratio is 300; Service temperature is 305 ℃, and working pressure is 2.0MPa (cutting off); Described light-middle gasoline (boiling range is 65-90 ℃) enters described aromatic hydrogenation device 3-2 with 2.5 ten thousand tons/year flows by pipeline; Described heavy petrol (boiling range is 160-205 ℃) enters extracting and separating among the heavy petrol extraction system 2-2 with 30,000 tons/year flows by pipeline, isolates aromatic hydrocarbons and raffinates oil; The extraction solvent for use is the N-formyl morpholine among the described extraction system 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 151 ℃, and solvent recuperation pressure is 0.112MPa (cutting off); Described aromatic hydrocarbons with 1.2 ten thousand tons/year flow with described in after aromatic hydrocarbons after the gasoline extracting mixes, enter aromatic hydrogenation device 3-2 hydrogenation, and then with described petroleum naphtha mediation; Described raffinating oil with the direct extraction of 1.8 ten thousand tons/year flow as low-coagulation diesel oil.
The boiling range of gained blended gasoline is 30-205 ℃, and sulphur content is 36.8ppm, and mercaptans content is 3.2ppm, olefin(e) centent is 12.9%, and (v), diene content is 0.4% (v), aromaticity content is 28.4% (v), octane value (RON) is 95.8, and density is 710.8 kilograms/meter
3, flow is 6.3 ten thousand tons/year.
The boiling range of gained high-quality ethylene is 90-160 ℃, and sulphur content is 5.0ppm, and mercaptans content is less than 1ppm, olefin(e) centent is 1.0%, and (v), diene content is that (v), aromaticity content is 4.0% (v) less than 0.01%, octane value (RON) is 77.2, and density is 733.0 kilograms/meter
3, flow is 1.9 ten thousand tons/year.
The boiling range of gained low-coagulation diesel oil is 160-205 ℃, and sulphur content is 30.0ppm, and mercaptans content is 4.0ppm, and olefin(e) centent is 60.0%, and (v), diene content is 0.1% (v), aromaticity content is that 4.0% (v), density is 789.0 kilograms/meter
3, flow is 1.8 ten thousand tons/year.
Embodiment 3
As shown in Figure 3, be the schematic flow sheet of the utility model embodiment.With boiling range is 30-205 ℃, and sulphur content is 100ppm, and mercaptans content is 5.0ppm, 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 68 ℃, column bottom temperature is 188 ℃, light-middle gasoline boiling range is 65-90 ℃; Middle gasoline boiling range is 90-160 ℃.Tower top pressure is 0.2MPa (cutting off), tower bottom pressure is 0.25MPa (cutting off), fractionation obtains petroleum naphtha, light-middle gasoline, middle gasoline and heavy petrol respectively, and described petroleum naphtha (boiling range is 30-65 ℃) steams by distillation tower 1 top, and its amount of steaming is 1.8 ten thousand tons/year; Carry out extracting and separating among the gasoline extraction system 2-1 during gasoline (boiling range is 90-160 ℃) enters by pipeline with 2.5 ten thousand tons/year flows in described, isolate aromatic hydrocarbons and raffinate oil; The extraction solvent for use is the N-formyl morpholine among the described extraction system 2-1, 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 0.13MPa (cutting off); Described aromatic hydrocarbons with 0.5 ten thousand tons/year flow by pipeline in aromatic hydrogenation device 3-2 behind the hydrogenation, the petroleum naphtha behind hydrogenation that steams by pipeline and distillation tower 1 top is in harmonious proportion again, and the catalyzer among the described aromatic hydrogenation device 3-2 is selective hydrogenation catalyst GHT-20; The volume space velocity ratio of described aromatic hydrogenation device 3-2 is 4; Hydrogen/oil volume ratio is 350; Service temperature is 325 ℃, and working pressure is 2.5MPa (cutting off); Described raffinating oil carried out extracting and separating through distillation tower 4 with 2.0 ten thousand tons/year flow after by the hydrogenation unit 3-1 hydrogenation of raffinating oil again, the tower top temperature of described distillation tower 4 is 150 ℃, column bottom temperature is 210 ℃, tower top pressure is 0.18MPa (cutting off), tower bottom pressure is 0.21MPa (cutting off), top steams reformer feed, and the bottom goes out diesel oil; Catalyzer among the described hydrogenation unit 3-1 that raffinates oil is selective hydrogenation catalyst GHT-20; The volume space velocity ratio of the described hydrogenation unit 3-1 that raffinates oil is 2; Hydrogen/oil volume ratio is 250; Service temperature is 285 ℃, and working pressure is 1.5MPa (cutting off); Described light-middle gasoline (boiling range is 65-90 ℃) enters described aromatic hydrogenation device 3-2 with 2.5 ten thousand tons/year flows by pipeline; Described heavy petrol (boiling range is 160-205 ℃) enters extracting and separating among the heavy petrol extraction system 2-2 with 3.2 ten thousand tons/year flows by pipeline, isolates aromatic hydrocarbons and raffinates oil; The extraction solvent for use is the N-formyl morpholine among the described extraction system 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 151 ℃, and solvent recuperation pressure is 0.112MPa (cutting off); Described aromatic hydrocarbons with 1.1 ten thousand tons/year flow with described in after aromatic hydrocarbons after the gasoline extracting mixes, enter aromatic hydrogenation device 3-2 hydrogenation, and then with described petroleum naphtha mediation; Described raffinating oil again through extraction system 4 carried out extracting and separating through hydrotreatment with 2.1 ten thousand tons/year flow and middle gasoline after raffinating oil after the extracting is mixed, obtain reformer feed and diesel oil.
The boiling range of gained blended gasoline is 30-205 ℃, and sulphur content is 4.9ppm, and mercaptans content is 1.8ppm, olefin(e) centent is 9.1%, and (v), diene content is 0.04% (v), aromaticity content is 23.8% (v), octane value (RON) is 93.4, and density is 712.5 kilograms/meter
3, produced quantity is 5.9 ten thousand tons/year.
The boiling range of gained reformer feed is 90-160 ℃, 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 84.8, and density is 733.0 kilograms/meter
3, produced quantity is 2.0 ten thousand tons/year.
The boiling range of gained diesel oil is 160-205 ℃, and sulphur content is 0.5ppm, and mercaptans content is less than 1ppm, and olefin(e) centent is that (v), diene content is that (v), aromaticity content is that 3.0% (v), density is 770.0 kilograms/meter less than 0.01% less than 0.1%
3, produced quantity is 2.1 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 bottom is provided with the heavy petrol pipeline; The middle part of described water distilling apparatus is provided with middle medium gasoline pipeline; Medium gasoline pipeline is connected with middle gasoline extraction system in described; Gasoline extraction system top is connected with the hydrogenation unit of raffinating oil by pipeline in described; The bottom of gasoline extraction system is connected with the aromatic hydrogenation device by pipeline in described, and then is connected with the petroleum naphtha pipeline on water distilling apparatus top by pipeline; Be provided with light-middle gasoline cutting mouth in described between gasoline cutting mouth and the described water distilling apparatus top, and be connected with described aromatic hydrogenation device by pipeline; Described heavy petrol pipeline is connected with the heavy petrol extraction system; The bottom of described heavy petrol extraction system is connected with described aromatic hydrogenation device by pipeline; Described heavy petrol extraction system top is connected by the hydrogenation unit of raffinating oil of pipeline with described middle gasoline, perhaps directly goes out the low-coagulation diesel oil product.
2, the system of catalyzing hydrocarbon for recombinant production of high-quality gasoline according to claim 1 is characterized in that: the described hydrogenation unit of raffinating oil is by being connected with extraction system.
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| CNU2007203020981U CN201158633Y (en) | 2007-11-09 | 2007-11-09 | System for producing high quality gasoline by catalyzing hydrocarbon regrouping |
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| CNU2007203020981U CN201158633Y (en) | 2007-11-09 | 2007-11-09 | System for producing high quality gasoline by catalyzing hydrocarbon regrouping |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2009067893A1 (en) * | 2007-11-09 | 2009-06-04 | Ranfeng Ding | A system and a process for recombining catalytic hydrocarbon to produce high quality gasoline |
| EP2390303A1 (en) * | 2009-01-21 | 2011-11-30 | Beijing Grand Golden-Bright Engineering & Technologi Co., Ltd. | System and process for producing high quality gasoline by recombination and subsequent hydrogenation of catalytic hydrocarbons |
| CN101429445B (en) * | 2007-11-09 | 2012-10-03 | 丁冉峰 | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline |
| CN102102031B (en) * | 2009-12-22 | 2014-01-22 | 北京金伟晖工程技术有限公司 | Method for preparing high-quality diesel oil by increasing cetane number through non-hydrodesulfurization |
| CN108102703A (en) * | 2016-11-24 | 2018-06-01 | 中国石油化工股份有限公司 | A kind of processing and treating method of catalytic diesel oil |
-
2007
- 2007-11-09 CN CNU2007203020981U patent/CN201158633Y/en not_active Expired - Lifetime
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2009067893A1 (en) * | 2007-11-09 | 2009-06-04 | Ranfeng Ding | A system and a process for recombining catalytic hydrocarbon to produce high quality gasoline |
| CN101429445B (en) * | 2007-11-09 | 2012-10-03 | 丁冉峰 | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline |
| EA017164B1 (en) * | 2007-11-09 | 2012-10-30 | Жаньфэн Дин | A system and a process for recombining catalytic hydrocarbon to produce high quality gasoline |
| EP2390303A1 (en) * | 2009-01-21 | 2011-11-30 | Beijing Grand Golden-Bright Engineering & Technologi Co., Ltd. | System and process for producing high quality gasoline by recombination and subsequent hydrogenation of catalytic hydrocarbons |
| EP2390303A4 (en) * | 2009-01-21 | 2015-03-18 | Beijing Grand Golden Bright Engineering & Technologi Co Ltd | System and process for producing high quality gasoline by recombination and subsequent hydrogenation of catalytic hydrocarbons |
| CN102102031B (en) * | 2009-12-22 | 2014-01-22 | 北京金伟晖工程技术有限公司 | Method for preparing high-quality diesel oil by increasing cetane number through non-hydrodesulfurization |
| CN108102703A (en) * | 2016-11-24 | 2018-06-01 | 中国石油化工股份有限公司 | A kind of processing and treating method of catalytic diesel oil |
| CN108102703B (en) * | 2016-11-24 | 2020-06-09 | 中国石油化工股份有限公司 | Processing method of catalytic diesel oil |
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