CN102382678B - Method for producing aromatic hydrocarbon from coked gasoline - Google Patents
Method for producing aromatic hydrocarbon from coked gasoline Download PDFInfo
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- CN102382678B CN102382678B CN201010267301.2A CN201010267301A CN102382678B CN 102382678 B CN102382678 B CN 102382678B CN 201010267301 A CN201010267301 A CN 201010267301A CN 102382678 B CN102382678 B CN 102382678B
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Abstract
The invention discloses a method for producing aromatic hydrocarbon from coked gasoline, which solves the problems that in the prior art, after the coked gasoline is hydrogenated, the potential aromatic hydrocarbon content is low, and in addition, the conversion is difficult, and so catalytic reforming processing is unfavorable to singly carry out. The method has the steps that: coked gasoline raw materials are subjected to aromatic hydrocarbon extraction, raffinate oil after the separation of raffinate oil phases at the top of an extraction tower is subjected to aromatization reaction, liquid products of the aromatization reaction return to be used as inlet materials of the aromatic hydrocarbon extraction, mixed aromatic hydrocarbon after the separation of solvents at the bottom of the extraction tower is refined through hydrogenation, and aromatic hydrocarbon products such as benzene, toluene, dimethylbenzene and the like are obtained after the aromatic hydrocarbon rectification of the refined mixed aromatic hydrocarbon, wherein the hydrocarbon refining conditions of the mixed aromatic hydrocarbon comprise the reaction temperature being 200 to 340 DEG C, the volume space velocity being 0.1 to 10.0h<-1> and the hydrogen partial pressure being 1.5 to 6.5 Mpa; and the aromatization reaction conditions comprise the reaction temperature being 400 to 600 DEG C, the mass space velocity being 0.1 to 10.0h<-1> and the reaction pressure being 0.1 to 1.0 MPa.
Description
Technical field
The present invention relates to a kind of method of producing aromatic hydrocarbon from coked gasoline inferior, more particularly, is a kind of combination process of aromatic hydrocarbons of producing through processes such as Aromatics Extractive Project, the aromizing of raffinating oil, BTX aromatics hydrofining and aromatic hydrocarbons separation by coker gasoline.
Background technology
Coking is in refining of petroleum, to take the important hot procedure that residual oil or heavy crude oil with poor quality be raw material, and coker gasoline is the gasoline fraction that coking produces.Coker gasoline is a kind of low-grade inferior patrol, and it is rich in alkene, and the foreign matter content such as sulphur, nitrogen compound and diolefine is high, has the features such as stench, poor stability and octane value are low.Although can significantly reduce its impurity and olefin(e) centent by hydrorefined method, improve stability, octane value also declines to a great extent simultaneously, still cannot use as fuel gasoline component.In recent years, the in the situation that, gasoline product quality increasingly strict in environmental requirement constantly being upgraded, how to reduce coker gasoline impurity and olefin(e) centent as far as possible and increase substantially its octane value, making substantially coker gasoline become proper fuel gasoline component or transform and produce high-quality aromatic hydrocarbon product, is the problem meriting attention.
Catalytic reforming is as an approach that improves coker gasoline quality.Conventionally first coker gasoline is carried out to hydrofining, remove the impurity such as sulphur nitrogen, mix by a certain percentage in reformer feed again, but because the coker gasoline after hydrogenation has that the reforming catalyst of making deactivation rate is accelerated and because of the low more difficult conversion of arene underwater content, therefore coker gasoline mixed ratio in reformer feed is generally no more than 35%, and in actual application coker gasoline in reformer feed mixed ratio generally 10～25%.
USP5643441, USP5685972 disclose and a kind ofly first coker gasoline have been carried out to hydrogenating desulfurization processing, then with the ZSM-5 molecular sieve catalyzer containing molybdenum modification, carry out the method for aromatization modification.These two kinds of methods are all that aromizing after the first hydrogenation of coker gasoline is recovered to gasoline octane rating, and aromatics yield is lower.
CN1715372A discloses the hydrogenation mixture of the distillate of coking distillate or its blending virgin oil or the generation of other secondary processing process refining, then carries out strict cut cutting, obtains the reforming raw oil with suitable boiling range scope; And to this stock oil pre-refining of reforming, further remove the impurity such as sulphur, nitrogen, to meet the specification of quality of reforming raw oil, make reforming catalyst performance unaffected.Then by introducing reforming system after the strict dehydration of the coker gasoline after pre-refining, the water in reformation circulating hydrogen is strictly controlled simultaneously, under the reaction conditions of catalytic reforming, coker gasoline is reformed, produce stop bracket gasoline blend component.The method need be to the reforming raw oil after hydrofining further pre-refining and processed, and be one and face hydrogen, reaction process with pressure.
Summary of the invention
A kind of method that the object of this invention is to provide producing aromatic hydrocarbon from coked gasoline, main process is under non-hydrogen, normal pressure or low-pressure state, not hydrorefined coker gasoline to be raffinated oil and carried out aromatization production aromatic hydrocarbons.Overcome prior art because of Hydrogenation of Coker Gasoline after arene underwater content low and should not carry out separately the problem of catalytic reforming processing compared with difficult conversion.
A kind of method that the invention provides producing aromatic hydrocarbon from coked gasoline, comprises the steps:
1) Aromatics Extractive Project: coker gasoline raw material carries out Aromatics Extractive Project, the raffinating oil after separation of raffinating oil of extracting tower top enters step 2), the BTX aromatics of the solvent phase at the bottom of extraction tower after separation enters step 3);
2) aromatization is carried out in raffinating oil aromizing: from step 1), and aromatization reaction products returns to step 1 after isolating the by products such as liquefied gas and dry gas) as the charging of Aromatics Extractive Project;
3) aromatic hydrogenation is refining: from step 1) BTX aromatics enter hydrofining unit and carry out hydrofining, the sulfide in Arene removal and nitride;
4) BTX aromatics separation: from step 3) BTX aromatics after hydrofining enters aromatic hydrocarbons rectification cell, obtains the aromatic hydrocarbon products such as benzene, toluene and dimethylbenzene.
Aromatic hydrogenation purification condition of the present invention is: 200～340 ℃ of temperature of reaction, volume space velocity 0.1～10.0h
-1, hydrogen dividing potential drop 1.5～6.5Mpa.
The present invention produces aromatic hydrocarbons with coker gasoline through hydrofining, catalytic reforming, Aromatics Extractive Project and aromatic hydrocarbons rectifying and compares, the present invention is not directly to coking gasoline hydrogenation refining, but being carried out to hydrofining, product BTX aromatics removes sulfide and nitride, reduced on the one hand the treatment capacity of hydro-refining unit, reduced on the other hand the hydrogen consumption in hydrogenation process, the content and the BTX aromatics yield that have improved aromatic hydrocarbons in the aromizing product liquid of raffinating oil, be beneficial to aromatic hydrocarbons separation more; Meanwhile, the present invention compares with the direct aromizing of coker gasoline, and the content of the middle nitride of raffinating oil reduces, the on-line operation time of having improved the aromatized catalyst of raffinating oil.
By the drawings and specific embodiments, describe the present invention in detail below, but do not limit the scope of the invention.
Accompanying drawing and accompanying drawing explanation
Figure is the simple flow chart of the method for a kind of producing aromatic hydrocarbon from coked gasoline of the present invention.
In figure: 1-coker gasoline raw material, 2-Aromatics Extractive Project tower, the 3-separation system of raffinating oil, 4-solvent phase separation system, 5-aromizing device, 6-aromizing product separation system, 7-hydro-refining unit, 8-aromatic hydrocarbons rectifier unit, 9-dry gas, 10-liquefied gas, 11-aromizing product liquid, 12-benzene, 13-toluene, 14-dimethylbenzene, 15-heavy aromatics.
Embodiment
As shown in the figure: first coker gasoline raw material 1 enters Aromatics Extractive Project tower 2 and carry out Aromatics Extractive Project, at the bottom of the tower of Aromatics Extractive Project tower 2 dissolving out the solvent phase of aromatic hydrocarbons, through solvent phase separation system 4, carry out the separated of BTX aromatics and solvent, BTX aromatics after separation is entered hydro-refining unit 7, remove sulfide and nitride in BTX aromatics, isolated solvent returns to extraction tower 2, the tower top of Aromatics Extractive Project tower 2 raffinating oil through separation system 3 separation of raffinating oil out, reclaim a small amount of solvent, recovered solvent returns to extraction tower 2, isolated the raffinating oil of the separation system of raffinating oil 3 carried out aromatization into aromizing device 5, aromatization reaction products carries out separation through aromizing product separation system 6, after isolating the by products such as dry gas 9 and liquefied gas 10, go out device, aromizing product liquid 11 after separation returns to Aromatics Extractive Project tower 2, mix with coker gasoline raw material 1 or enter separately Aromatics Extractive Project tower 2, hydro-refining unit 7 BTX aromatics after hydrofining is out entered aromatic hydrocarbons rectifier unit 8 and is carried out aromatic hydrocarbons separation, obtain benzene 12, toluene 13, dimethylbenzene 14 and heavy aromatics (C
9 +) 15 aromatic hydrocarbon products such as grade.
In the inventive method, coker gasoline raw material 1 adopts conventional Aromatics Extractive Project method while carrying out Aromatics Extractive Project, comprise solvent extraction process, extractive distillation method, azeotropic distn and absorption method etc., preferred solvent extraction process.
Aromatization of the present invention aromatized catalyst used is mainly with metal-modified shape-selective molecular sieve catalyzer.Molecular sieve is HZSM-5, HZSM-7, HZSM-8, HZSM-11, HZSM-12, HZSM-35 or HZSM-48 etc., preferred HZSM-5, its content is 10～90 % by weight that account for total catalyst weight, preferably 20～85 % by weight, the silica alumina ratio of molecular sieve is 20～400, preferably 30～300; Modified metal is Zn-Al, Ga-Zn, Zn-Re, Al-Re or Zn-Al-Re etc., and its content (by metallic state, accounting for total catalyst weight) is 0.5～10 % by weight, preferably 1.0～8.0 % by weight; Binding agent comprises Al
2o
3, SiO
2, Al
2o
3and SiO
2mixture, clay etc.Also can use other catalyzer suitable with stability with above-mentioned catalyst activity, such as: the HZSM-5 catalyzer and other catalyzer with similar functions that use the modified metals such as Ga, Ga-Zn, Pd-Zn or Ga-Re to carry out modification.
Aromatization condition of the present invention is: temperature of reaction is 400～600 ℃, and mass space velocity is 0.1～10.0h
-1, reaction pressure is 0.1～1.0MPa.
In the inventive method, BTX aromatics hydrofining removes sulphur nitrogen impurity and can adopt conventional method to carry out, and Hydrobon catalyst used can be selected conventional catalyst used for hydrogenation of distilled oil fraction.
BTX aromatics hydrofining reaction condition of the present invention is: temperature of reaction is 200～340 ℃, and volume space velocity is 0.1～10.0h
-1, hydrogen dividing potential drop is 1.5～6.5MPa.
In the inventive method, the conventional aromatic hydrocarbons separation method of the separated employing of BTX aromatics after hydrofining.
Below by embodiment, further illustrate the solution of the present invention and effect, but therefore do not limit the present invention.The processing condition of each operating unit of the present invention and catalyzer are conventional, and concrete selection can be determined by the general knowledge of association area according to the requirement of the character of raw material, product etc.
The present embodiment has provided the effect of a kind of high-sulfur, high nitrogen-containing producing aromatic hydrocarbon from coked gasoline.
Coker gasoline and the character of raffinating oil is in Table 1, and raffinate oil aromatization condition and product of coker gasoline distributes in Table 2, and the product of producing aromatic hydrocarbon from coked gasoline distributes and forms in Table 3, and before and after BTX aromatics hydrofining, product property is in Table 4.
Table 1 coker gasoline and the character of raffinating oil
| Project | Coker gasoline | Raffinate oil |
| Density, (20 ℃) g/cm 3 | 0.7413 | 0.7363 |
| Alkane, % by weight | 65.8 | 69.6 |
| Alkene, % by weight | 25.7 | 29.7 |
| Aromatic hydrocarbons, % by weight | 8.5 | 0.7 |
| Sulphur content, μ gg -1 | 4000 | 1150 |
| Nitrogen content, μ gg -1 | 200 | 45 |
| Octane value, (MON) | 62.4 | |
| Boiling range, ℃ | ||
| Initial boiling point | 57 | 56 |
| 10％ | 91 | 89 |
| 50％ | 159 | 155 |
| 90％ | 167 | 167 |
| Final boiling point | 192 | 189 |
Raffinate oil aromatization condition and product of table 2 distributes
| Project | Numerical value |
| Temperature of reaction, ℃ | 520 |
| Reaction velocity, h -1 | 1.0 |
| Reaction pressure, Mpa | 0.1 |
| Product distributes, % by weight | |
| Dry gas | 14.71 |
| Liquefied gas | 26.75 |
| Product liquid | 57.54 |
| Coke+loss | 1.00 |
| Aromaticity content in aromatization carburetion, % by weight | 93.94 |
| In aromatization carburetion, aromatic hydrocarbons distributes, % by weight | |
| Benzene | 17.80 |
| Toluene | 44.50 |
| Dimethylbenzene (ethylbenzene) | 25.38(1.50) |
| C 9 + | 6.26 |
The product of table 3 producing aromatic hydrocarbon from coked gasoline distributes and aromatic hydrocarbons forms
| Product distributes, % by weight | Numerical value |
| Dry gas | 13.82 |
| Liquefied gas | 23.90 |
| BTX aromatics | 61.27 |
| Coke+loss | 1.01 |
| In BTX aromatics, aromatic hydrocarbons distributes, % by weight | |
| Benzene | 18.17 |
| Toluene | 48.33 |
| Dimethylbenzene (ethylbenzene) | 26.89(1.56) |
| C 9 + | 6.61 |
Character before and after the hydrofining of table 4 BTX aromatics
| Project | Numerical value |
| Temperature of reaction, ℃ | 285 |
| Reaction velocity, h -1 | 1.0 |
| Reaction pressure, Mpa | 3.0 |
| Feedstock property | |
| Sulphur content, μ gg -1 | 480 |
| Nitrogen content, |
6 |
| Product characteristics | |
| Sulphur content, μ gg -1 | ＜1 |
| Nitrogen content, μ gg -1 | ＜0.5 |
Embodiment 2
The present embodiment has provided the effect of a kind of moderate sulfur, medium nitrogen content producing aromatic hydrocarbon from coked gasoline.
Coker gasoline and the character of raffinating oil is in Table 5, and raffinate oil aromatization condition and product of coker gasoline distributes in Table 6, and the product of producing aromatic hydrocarbon from coked gasoline distributes and forms in Table 7, and before and after BTX aromatics hydrofining, product property is in Table 8.
Table 5 coker gasoline and the character of raffinating oil
| Project | Coker gasoline | Raffinate oil |
| Density, (20 ℃) g/cm 3 | 0.7401 | 0.7358 |
| Alkane, % by weight | 58.1 | 65.6 |
| Alkene, % by weight | 31.3 | 33.4 |
| Aromatic hydrocarbons, % by weight | 10.6 | 1.0 |
| Sulphur content, μ gg -1 | 1100 | 340 |
| Nitrogen content, μ gg -1 | 140 | 30 |
| Octane value, (MON) | 58.5 | |
| Boiling range, ℃ | ||
| Initial boiling point | 52 | 50 |
| 10％ | 89 | 88 |
| 50％ | 127 | 124 |
| 90％ | 162 | 161 |
| Final boiling point | 190 | 188 |
Raffinate oil aromatization condition and product of table 6 distributes
| Project | Numerical value |
| Temperature of reaction, ℃ | 520 |
| Reaction velocity, h -1 | 0.5 |
| Reaction pressure, Mpa | 0.1 |
| Product distributes, % by weight | |
| Dry gas | 17.35 |
| Liquefied gas | 18.42 |
| Product liquid | 63.23 |
| Coke+loss | 1.00 |
| Aromaticity content in aromatization carburetion, % by weight | 98.15 |
| In aromatization carburetion, aromatic hydrocarbons distributes, % by weight | |
| Benzene | 18.04 |
| Toluene | 47.27 |
| Dimethylbenzene (ethylbenzene) | 26.26(1.57) |
| C 9 + | 6.58 |
The product of table 7 producing aromatic hydrocarbon from coked gasoline distributes and aromatic hydrocarbons forms
| Product distributes, m% | Numerical value |
| Dry gas | 15.58 |
| Liquefied gas | 18.27 |
| BTX aromatics | 65.13 |
| Coke+loss | 1.02 |
| In BTX aromatics, aromatic hydrocarbons distributes, % by weight | |
| Benzene | 18.23 |
| Toluene | 48.09 |
| Dimethylbenzene (ethylbenzene) | 26.96(1.64) |
| C 9 + | 6.72 |
Character before and after the hydrofining of table 8 BTX aromatics
| Project | Numerical value |
| Temperature of reaction, ℃ | 225 |
| Reaction velocity, h -1 | 1.0 |
| Reaction pressure, Mpa | 2.5 |
| Feedstock property | |
| Sulphur content, μ gg -1 | 150 |
| Nitrogen content, μ gg -1 | 5 |
| Product characteristics | |
| Sulphur content, μ gg -1 | ＜1 |
| Nitrogen content, μ gg -1 | ＜0.5 |
Comparative example 1
By the coker gasoline raw material hydrofining of embodiment 1, take this hydrotreated coker gasoline as raw material, on fixed bed Catalytic Reformer Pilot Plant, carry out catalytic reforming reaction, the catalyzer of filling has carried out conventional reduction within packing reactor into, at reactive system, set up hydrogen recycle simultaneously, then under the reaction conditions of regulation, stock oil is introduced to reactive system and react, reaction result is in Table 9.
Reaction conditions and the product of the burnt vapour catalytic reforming of table 9 hydrogenation distribute
| Project | Numerical value |
| Temperature of reaction, ℃ | 520 |
| Reaction velocity, h -1 | 1.0 |
| Reaction pressure, Mpa | 1.2 |
| Product distributes, % by weight | |
| Gaseous product | 14.65 |
| Product liquid | 84.23 |
| Liquid aromaticity content, % by weight | 66.35 |
| Aromatics yield, % by weight | 55.89 |
Claims (7)
1. a method for producing aromatic hydrocarbon from coked gasoline, is characterized in that steps of the method are:
1) Aromatics Extractive Project: coker gasoline raw material carries out Aromatics Extractive Project, the raffinating oil after separation of raffinating oil of extracting tower top enters step 2), the BTX aromatics of the solvent phase at the bottom of extraction tower after separation enters step 3);
2) aromatization is carried out in raffinating oil aromizing: from step 1), and aromatization reaction products returns to step 1 after isolating the by product that comprises liquefied gas and dry gas) as the charging of Aromatics Extractive Project;
3) aromatic hydrogenation is refining: from step 1) BTX aromatics enter hydrofining unit and carry out hydrofining, the sulfide in Arene removal and nitride;
4) BTX aromatics separation: from step 3) BTX aromatics after hydrofining enters aromatic hydrocarbons rectification cell, obtains benzene, toluene and dimethylbenzene aromatic hydrocarbon product.
2. method according to claim 1, is characterized in that: the aromatic hydrogenation purification condition described step 3) is: 200～340 ℃ of temperature of reaction, and volume space velocity 0.1～10.0h～, hydrogen dividing potential drop 1.5～6.5MPa.
3. method according to claim 1, is characterized in that: the aromatization condition described step 2) is: 400～600 ℃ of temperature of reaction, mass space velocity 0.1～10.0h-1, reaction pressure 0.1～1.0MPa.
4. method according to claim 1, it is characterized in that: the aromizing of raffinating oil described step 2) aromatized catalyst used is metal-modified shape-selective molecular sieve catalyzer, wherein modified metal is Zn-Al, Ga-Zn, Zn-Re, Al-Re or Zn-Al-Re, by metallic state, modified metal accounts for 0.5～10 % by weight of total catalyst weight.
5. method according to claim 4, is characterized in that: described shape-selective molecular sieve is HZSM-5, HZSM-7, HZSM-8, HZSM-11, HZSM-12, HZSM-35 or HZSM-48, and the silica alumina ratio of molecular sieve is 20～400.
6. method according to claim 5, is characterized in that: described shape-selective molecular sieve is HZSM-5.
7. method according to claim 5, is characterized in that: the silica alumina ratio of described shape-selective molecular sieve is 30～300.
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| CN104045499B (en) * | 2013-03-12 | 2016-09-14 | 中石化洛阳工程有限公司 | A kind of utilize the method for ethylene production aromatic hydrocarbons in oil refinery dry gas |
| CN106367116B (en) * | 2015-07-23 | 2019-02-22 | 中国石油化工股份有限公司 | A method of light aromatics is prepared using reforming raffinate oil |
| CN105130737A (en) * | 2015-08-06 | 2015-12-09 | 江苏中泰生物科技有限公司 | Method for preparing benzene-based aromatic hydrocarbon through petroleum olefin hydrogenation |
| CN108349853B (en) | 2015-11-12 | 2022-03-15 | 沙特基础工业全球技术公司 | Process for producing aromatic hydrocarbons and olefins |
| CN105925306A (en) * | 2016-06-24 | 2016-09-07 | 郭怡彬 | Process for producing arene through naphtha |
| CN107970988B (en) * | 2016-10-24 | 2020-05-12 | 中国科学院大连化学物理研究所 | Catalyst for synthesizing aromatic hydrocarbon and preparation method thereof |
| CN107011942B (en) * | 2017-05-03 | 2018-08-28 | 武汉工程大学 | A method of reducing extractant regeneration energy consumption in gasoline sweetening process |
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| CN1080313A (en) * | 1992-03-05 | 1994-01-05 | 中国石化洛阳石油化工工程公司 | Catalytic upgrading-aromatization process of poor gasoline |
| CN1814708A (en) * | 2005-02-05 | 2006-08-09 | 中国石油化工股份有限公司 | Method for modifying poor-quality diesel-oil by cut fraction |
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| DE1908868C3 (en) * | 1969-02-21 | 1975-10-30 | Universal Oil Products Co., Des Plaines, Ill. (V.St.A.) | Process for the preparation of a paraffinic, aromatic-free solvent for edible oils |
| JP4812436B2 (en) * | 2006-01-19 | 2011-11-09 | 石油コンビナート高度統合運営技術研究組合 | Process for producing benzene and gasoline base from petrochemical raffinate |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1080313A (en) * | 1992-03-05 | 1994-01-05 | 中国石化洛阳石油化工工程公司 | Catalytic upgrading-aromatization process of poor gasoline |
| CN1814708A (en) * | 2005-02-05 | 2006-08-09 | 中国石油化工股份有限公司 | Method for modifying poor-quality diesel-oil by cut fraction |
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