CN103756721B - A kind of extraction-washing-hydrogenation combination technique producing low-sulphur oil - Google Patents
A kind of extraction-washing-hydrogenation combination technique producing low-sulphur oil Download PDFInfo
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Abstract
Produce a method for low-sulphur oil, gasoline stocks be cut into gently, last running, lighting end, through extracting de-thiophene, mercaptan, thioether, disulfides sulfide, is extracted desulfurization light gasoline fraction and extraction phase; Wherein, extraction light gasoline fraction enters washing device, extraction agent in removing gasoline, must extract-wash benzoline, selective hydrodesulfurization is carried out after the sulfur-bearing light gasoline fraction reclaimed from extraction phase mixes with heavy naphtha, obtain hydrogenation heavy distillate, extraction-washing light gasoline fraction and hydrogenated heavy gasoline cut are mixed to get gasoline products.The method energy production sulphur content meets the gasoline of state IV standard lower than 50ug/g, sulphur content, also production sulphur content can meet the gasoline of state V standard lower than 10ug/g, sulphur content.
Description
Technical field
The present invention relates to a kind of method reducing gasoline stocks sulphur content, particularly one reduces catalytically cracked gasoline feed sulphur content, produces the method for super low-sulfur oil.
Background technology
Along with the enhancing of mankind's environmental consciousness, in vehicle exhaust, objectionable impurities more and more causes the attention of people to the pollution of atmospheric environment, and the composition of countries in the world to motor spirit proposes increasingly strict requirement, especially sulphur content.European Union came into effect Europe IV automobile exhaust emission standard in 2005, require that content of sulfur in gasoline is less than 50ug/g, come into effect Euro V emissions on September 1st, 2009, require that content of sulfur in gasoline is less than 10ug/g, also plan to carry out more strict Europe VI standard at about 2014; China will implement state III gasoline standard (GB17930-2006) the end of the year 2009, require that sulphur content is not more than 150ug/g; Plan to implement integrally state four gasoline standard in 1 day January in 2014, require that sulphur content is not more than 50ug/g; Rise on January 1st, 2018 and implement integrally state five gasoline standard, require that sulphur content is not more than 10ug/g.The continuous upgrading of gasoline quality standard, makes the gasoline production technology of oil refining enterprise be faced with more and more stern challenge.
In current domestic gasoline product, the sulphur of more than 90% carrys out catalytic cracking (FCC) gasoline, and therefore catalytically cracked gasoline feed sulphur content reduces is the key point reducing finished product content of sulfur in gasoline.
The sulphur content reducing catalytically cracked gasoline raw material can adopt catalytically cracked material weighted BMO spaces (front-end hydrogenation), catalytically cracked gasoline raw material hydrogenating desulfurization (back end hydrogenation) two kinds of modes usually.Wherein, catalytically cracked material pre-treatment significantly can reduce the sulphur content of catalytically cracked gasoline raw material, but needs to operate under temperature and pressure all very exacting terms, simultaneously because unit capacity is large, cause hydrogen to consume also larger, these all will improve investment or the running cost of device.However, due to the heaviness of world's crude oil, increasing catalytic cracking unit starts to process the inferior raw material containing normal, vacuum residuum etc., and therefore catalytically cracked material hydrogenation unit amount is also increasing year by year.Meanwhile, along with the innovation of catalytic cracking technology, the application gradually of catalytic cracking desulfurization auxiliary, the sulfur content of catalytic cracking gasoline of China's Some Enterprises can reach below 500ug/g, or even below 150ug/g.But if the sulphur content of catalytically cracked gasoline will be reduced further, make it to be less than 50ug/g(and meet Europe IV emission standard to the restriction of content of sulfur in gasoline), even be less than 10ug/g(and meet the restriction of Euro V emissions to content of sulfur in gasoline), then must increase substantially the operating severity of catalytically cracked material hydrogenation unit, very uneconomical economically.
Compare front-end hydrogenation, catalytic gasoline hydrogenation desulfurization is all lower than catalytically cracked material weighted BMO spaces in plant investment, production cost and hydrogen consumption, and its different desulfurization depth can meet the requirement of different size sulphur content.If but it is saturated in a large number and make loss of octane number very large to adopt traditional hydrofinishing process can make to have in catalytically cracked gasoline high-octane olefin component.Therefore, develop that a kind of to invest low, that loss of octane number is little low-sulphur oil production technology extremely urgent.
In light fractions of FCC naphtha, olefin(e) centent is high, and in last running, olefin(e) centent is lower, so can adopt the method that cut cuts, catalytically cracked gasoline raw material is cut into lighting end and last running; Traditional hydrogenating desulfurization technology is taked in last running, and lighting end adopts non-hydrodesulfurization.Document shows that catalytically cracked gasoline raw material medium sulphide content is mainly divided into the large class of thio-alcohol, thioether class, thiophene-based 3: thiophene-based content is the highest, accounts for about 70% of sulfide; Next is thio-alcohol, accounts for sulfide about 16% ~ 20%; Thioether class content is relatively less compared with other two classes.In thiophene-type sulfide in gasoline, thiotolene content is higher, accounts for about 40%, is secondly that thiophene accounts for about 15%.Known from the boiling point of sulfide: gasoline light constituent, thio-alcohol mainly concentrates on less than 80 DEG C, and thiophene is present in the cut of 80 DEG C ~ 90 DEG C, within the scope of 100 DEG C ~ 120 DEG C, sulphur content is the highest, accounting for about 20% of total sulfur content, should major part be thiotolene and a small amount of tetramethylene sulfide etc.Adopt non-hydrodesulfurization when taking off the sulfide in gasoline lighting end, cut point that is light, last running is higher, and in last running, olefin(e) centent is fewer, then the olefin loss that causes of hydrogenation is less; When cut point is 80 DEG C, lighting end is mainly mercaptan; When cut point is 90 DEG C, in lighting end, thiophene content is higher, now must remove thiophene and just can make sulphur content ≯ 10ug/g in lighting end.Therefore the crucial thiophene being to remove in lighting end of non-hydrogenating desulfurization.
Summary of the invention
For above-mentioned situation, the present invention proposes a kind of method of producing low-sulphur oil, and fiuidized bed evaporator raw material is cut into light gasoline fraction and heavy naphtha, adopts hydrogenation and the desulfurization of non-hydrogenation combination technique; For the problem that thiophene content in feed gasoline cut is high, adopt abstraction technique, can thiophene be removed, also can remove mercaptan wherein, thioether, disulfides sulfide; Mainly be present in light gasoline fraction for alkene, adopt abstraction technique desulfurization, avoid the problem that hydrogenation causes light gasoline fraction olefin loss; Heavy naphtha adopts conventional Hydrofining Technology desulfurization; Finally extraction-washing light gasoline fraction and hydrogenated heavy gasoline cut are mixed to get sulphur content and are not more than 50ug/g or 10ug/g gasoline products.The present invention only need increase abstraction desulfurization device on the basis of former hydrogenation unit, and plant modification is simple, not only reduced investment, and can ensure that gasoline octane rating loss is little, and production sulphur content is not more than the gasoline products of 50ug/g or 10ug/g.
The method that the present invention produces low-sulphur oil comprises the following steps:
(1). catalytically cracked gasoline raw material is cut into light gasoline fraction, heavy naphtha, and wherein the cut point of light gasoline fraction and heavy naphtha is 60 DEG C ~ 100 DEG C;
(2). light gasoline fraction removes thiophene, mercaptan, thioether, disulfides sulfide wherein through extracting and refining, is extracted light gasoline fraction and extraction phase;
(3). in step (2), extraction phase enters reboiler, steams the sulfur-bearing light gasoline fraction in extraction phase, and reclaim extraction agent, regeneration temperature is 80 DEG C ~ 110 DEG C; The extraction agent of regeneration recycles, the sour gasoline steamed hydrogenating desulfurization together with heavy naphtha.
(4). in step (2), extraction light gasoline fraction washs through washing tower, the extraction agent that removing is dissolved, be extracted-wash light gasoline fraction.
(5). heavy naphtha contacts with Hydrobon catalyst with hydrogen together with after the sulfur-bearing light gasoline fraction mixing steamed from extraction phase, carries out selective hydrodesulfurization reaction, obtains hydrogenated heavy gasoline cut;
(6). the light gasoline fraction of hydrogenated heavy gasoline cut and extraction-washing is mixed to get sulphur content ≯ 50ug/g gasoline products or sulphur content ≯ 10ug/g gasoline products.
Accompanying drawing explanation
Accompanying drawing 1 is a kind of extraction-washing-hydrogenation combination technique schema producing low-sulphur oil of the present invention.
In figure: 1, gasoline stocks oil pipe laying; 2, separation column; 3, lighting end pipeline line; 4, last running pipeline line; 5, pipeline; 6, pump; 7, pipeline; 8, pipeline; 9, process furnace; 10, pipeline; 11, hydrogenator; 12, pipeline; 13, extraction tower; 14, pipeline; 15, pipeline; 16, revivifier; 17, pipeline; 18, pipeline; 19, separator; 20, pipeline; 21, pipeline; 22, compressor; 23, pipeline; 24, pipeline; 25, pipeline; 26, washing device; 27, pipeline; 28, pipeline; 29, stabilizer tower; 30, pipeline; 31, pipeline.
Embodiment
It is as follows that the present invention reduces content of sulfur in gasoline method flow: gasoline stocks enters separation column 2 through pipeline 1 and cuts into gently, heavy naphtha, wherein heavy naphtha is after pipeline 4 mixes with the sour distillate oil from pipeline 17, pump 6 is entered through pipeline 5, heavy naphtha after boosting is after pipeline 7 mixes with the hydrogen from pipeline 25, process furnace 9 is entered through pipeline 8, material after heating enters reactor 11 through pipeline 10 and contacts with Hydrobon catalyst, hydrogenated oil enters high-pressure separator 19 through pipeline 12, from separator 19 top, hydrogen-rich gas out enters compressor 22 through pipeline 21, hydrogen-rich gas after compression is through pipeline 23 inlet pipe line 25 together with the supplementary live gas from pipeline 24, mix with the heavy distillate from pipeline 7.Bottom separator 19, hydrogenated heavy gasoline cut out mixes stabilizer tower through pipeline 20 with the extraction-washing light gasoline fraction oil from pipeline 27.
Lighting end gasoline enters extraction tower 13 through pipeline 3, bottom extraction tower 13, extraction phase out enters revivifier 16 through pipeline 15, the extraction agent separated bottom revivifier 16 enters extraction tower 13 top through pipeline 18, oily through pipeline 17 and the heavy distillate mixing back end hydrogenation process from pipeline 4 from the sour distillate of revivifier 16 recovered overhead.From extraction tower 13 top, abstraction desulfurization benzoline out enters washing device 26 through pipeline 14, light gasoline fraction after washing mixes with the hydrogenated heavy gasoline cut from pipeline 20 through pipeline 27, mixed gasoline enters stabilizer tower 29 through pipeline 28, and separation obtains lighter hydrocarbons and gasoline products is drawn through pipeline 30,31 respectively.
The following examples will be further described method provided by the invention, but therefore not limit the scope of the invention.
Embodiment 1
With FCC gasoline A for raw material, first raw material is cut, cut point is 95 DEG C, and heavy naphtha accounts for the per-cent 52% of raw material, and the character of the full cut of gasoline (FCCN), light gasoline fraction (LCN), heavy naphtha (HCN) is as shown in table 1-1.Light gasoline fraction enters abstraction desulfurization unit, is extracted light gasoline fraction and extraction phase, and extraction agent is n-formylmorpholine, agent-oil ratio is 2:1, extraction progression is 4 grades, and extraction temperature is 55 DEG C, removes the thiophene in lighting end gasoline, mercaptan, thioether, disulfides sulfide; Extraction phase enters reboiler, and regeneration temperature is 110 DEG C, and the extraction agent of regeneration recycles, and the sour gasoline steamed mixes laggard hydrogenation unit with heavy naphtha; Extraction light gasoline fraction enters washing device, and washing composition is water, the extraction agent in removing extraction light gasoline fraction, must extract-wash light gasoline fraction.Hydrogenated heavy gasoline cut is obtained after heavy naphtha hydrotreatment.Extraction-washing light gasoline fraction and hydrogenated heavy gasoline cut are mixed to get gasoline products.
After gasoline adopts the technology of the present invention process, extraction-washing light gasoline fraction (LCN '), hydrogenated heavy gasoline cut (HCN '), gasoline products (FCCN ') character are as shown in table 1-2.
Table 1-1 gasoline stocks and cut character thereof
Table 1-2 gasoline stocks character after present invention process process
Contrast table 1-1 and table 1-2 can find out, gasoline stocks is after present invention process process, in light gasoline fraction, sulphur content is down to 21.6ug/g from 221ug/g, and namely abstraction desulfurization technique of the present invention possesses higher sweetening power, and light gasoline fraction sulphur content can be made to reach below 50ug/g; In heavy naphtha, sulphur content is down to 8.0ug/g from 1430ug/g; Content of sulfur in gasoline is down to 14.5ug/g from 849ug/g, shows to adopt this technique, production sulphur content can meet the gasoline of state IV standard lower than 50ug/g, sulphur content.
Embodiment 2
With FCC gasoline B for raw material first cuts raw material, cut point is 100 DEG C, and get lighting end gasoline and investigate extraction agent sweetening effectiveness, extraction agent is tetramethylene sulfone, and agent-oil ratio is 3:1, and extraction progression is 4 grades, and extraction temperature is 45 DEG C; Extraction light gasoline fraction enters washing device, and washing composition is ethanol, the extraction agent in removing gasoline fraction.Effect is as follows: raw material lighting end sulphur content 342.6ug/g, and after extracting and washing, sulphur content is reduced to 27.4ug/g, shows to adopt this technique, production sulphur content can meet the gasoline of state IV standard lower than 50ug/g, sulphur content.
Embodiment 3
The gasoline produced with the catalytic cracking after wax oil hydrogenation process is for raw material, and cut gasoline stocks, cut point is 93 DEG C, get lighting end gasoline and investigate extraction agent sweetening effectiveness, extraction agent is n-formylmorpholine, and agent-oil ratio is 2:1, extraction progression is 4 grades, and extraction temperature is 38 DEG C; Extraction light gasoline fraction enters washing device, and washing composition is methane amide, the extraction agent in removing gasoline fraction.Effect is as follows: raw material lighting end sulphur content 19.0ug/g, after extracting and washing, sulphur content is reduced to 8.3ug/g.Show that the gasoline that this invented technology is produced the catalytic cracking after wax oil hydrogenation process is effective equally.The gasoline produced with the catalytic cracking after wax oil hydrogenation process is for raw material, and light gasoline fraction sulphur content is lower, but does not reach the requirement of state V normal benzene sulphur content.Adopt this technique, production sulphur content can meet the gasoline of state V standard lower than 10ug/g, sulphur content.
Embodiment 4
With FCC gasoline C for raw material first cuts raw material, cut point is 90 DEG C, gets lighting end gasoline and investigates extraction agent sweetening effectiveness.Concrete grammar is as follows:
1. the preparation of gasoline
In light gasoline fraction, add thiophene, investigate extraction agent to the sweetening effectiveness of different sulphur content gasoline.
Add 1000ug/g in lighting end gasoline, be designated as sample 1;
Add 500ug/g in lighting end gasoline, be designated as sample 2;
Do not add thiophene in lighting end gasoline, be designated as sample 3;
2. respectively above-mentioned gasoline is carried out abstraction desulfurization process, extraction agent is tetramethylene sulfone, agent-oil ratio 3:1, and extraction progression is 4 grades, and extraction temperature is 25 DEG C; Extraction light gasoline fraction enters washing device, and washing composition is ethylene glycol, the extraction agent in removing gasoline fraction.The results are shown in Table 4-1.
Sulphur content after each lighting end gasoline desulfur of table 4-1
Table 4-1 shows, the abstraction desulfurization technique in present invention process has higher sweetening power, and de-thiophenic sulfur ability is remarkable.
Embodiment 5
Take analog gasoline as raw material, the mercaptan removal of high spot reviews extraction, de-thiophene effect.
1. the configuration of analog gasoline
Thiophene content in the analog gasoline prepared in experiment is about 500ug/g, and the content of mercaptan is about 190ug/g, and total sulfur is 241.57ug/g.Analog gasoline composition is in Table 5-1.
Table 5-1 analog gasoline composition
2. above-mentioned analog gasoline is carried out abstraction desulfurization process, extraction agent is tetramethylene sulfone, and agent-oil ratio is 3:1, and extraction progression is 4 grades, and extraction temperature is 60 DEG C; Extraction light gasoline fraction enters washing device, and washing composition is glycerol, the extraction agent in removing gasoline fraction.
3. after extracting and washing, result is as follows: sulfur removal rate reaches 92%, and after desulfurization, analog gasoline sulphur content is 19.32ug/g.As can be seen here, the abstraction desulfurization technique in present invention process has higher sweetening power, the Major Sulfides in light gasoline fraction: thiophenic sulfur and mercaptan sulfur, has good removal effect, makes the sulphur content in cut reach the ≯ standard of 50ug/g.
Embodiment 6
With FCC gasoline D for raw material, get the light gasoline fraction of boiling point 80 DEG C ~ 100 DEG C, investigate extraction agent sweetening effectiveness in present invention process.Extraction agent is n-formylmorpholine, agent-oil ratio is 2:1, extraction temperature is 30 DEG C, extraction light gasoline fraction enters washing device, and washing composition is methyl alcohol, the extraction agent in removing gasoline fraction, effect is as follows: raw material lighting end sulphur content 130.0ug/g, after extracting and washing, sulphur content is reduced to 24.7ug/g, shows to adopt this technique, and the light gasoline fraction sulphur content of 80 DEG C ~ 100 DEG C can be made lower than 50ug/g, the sulfur content in gasoline standard reaching state IV standard.
Embodiment 7
With FCC gasoline E for raw material cuts, cut point is 95 DEG C, gets lighting end gasoline, investigates regenerating extracting agent sweetening effectiveness.
Extraction agent is fresh dose of nitrogen dimethylformamide (DMF), and agent-oil ratio is 2:1, and extraction progression is 2 grades, and extraction temperature is 30 DEG C; Light gasoline fraction after abstraction desulfurization enters washing device, the extraction agent in removing gasoline fraction;
Reclaim extraction agent in 1, under the condition of 95 DEG C, act on 6h, the sulfur-bearing light gasoline fraction evaporated and the process of heavy naphtha mixing back end hydrogenation, the extraction agent of recovery carries out abstraction desulfurization experiment, and agent-oil ratio is 2:1, and extraction progression is 2 grades, and extraction temperature is 30 DEG C; Light gasoline fraction after abstraction desulfurization enters washing device, the extraction agent in removing gasoline fraction.
Result is as follows: the desulfurization degree of fresh extraction agent is 67.2%, and the desulfurization degree of the extraction agent recycled is 65.8%.Experimental result shows that extraction agent has and recycles performance preferably.
Embodiment 8
With FCC gasoline F for raw material, cut raw material, cutting temperature is 120 DEG C, gets light gasoline fraction, investigates extraction agent sweetening effectiveness in present invention process.Extraction agent is n-formylmorpholine, and agent-oil ratio is 2:1, and extraction progression is 4 grades, and extraction temperature is 25 DEG C; Extraction light gasoline fraction enters washing device, extraction agent in removing gasoline fraction, effect is as follows: raw material lighting end sulphur content 240.0ug/g, after extracting and washing, sulphur content is reduced to 49.0ug/g, as can be seen here, abstraction desulfurization technique in present invention process has higher sweetening power, and sulphur content in light gasoline fraction can be made to reach ≯ the standard of 50ug/g.
Claims (6)
1. reduce a method for gasoline stocks sulphur content, it is characterized in that comprising the following steps:
(1). catalytically cracked gasoline raw material is cut into light gasoline fraction, heavy naphtha, and wherein the cut point of light gasoline fraction and heavy naphtha is 60 DEG C ~ 100 DEG C;
(2). light gasoline fraction removes thiophene, mercaptan, thioether, disulfides sulfide wherein through extracting and refining, is extracted light gasoline fraction and extraction phase;
(3). in step (2), extraction phase enters reboiler, steams the sulfur-bearing light gasoline fraction in extraction phase, and reclaim extraction agent, regeneration temperature is 80 DEG C ~ 110 DEG C; The extraction agent of regeneration recycles, the sour gasoline steamed hydrogenating desulfurization together with heavy naphtha;
(4). in step (2), extraction light gasoline fraction washs through washing tower, the extraction agent that removing is dissolved, be extracted-wash light gasoline fraction;
(5). heavy naphtha contacts with Hydrobon catalyst with hydrogen together with after the sulfur-bearing light gasoline fraction mixing steamed from extraction phase, carries out selective hydrodesulfurization reaction, obtains hydrogenated heavy gasoline cut;
(6). the light gasoline fraction of hydrogenated heavy gasoline cut and extraction-washing is mixed to get sulphur content ≯ 50ug/g gasoline products or sulphur content ≯ 10ug/g gasoline products.
2. the method for reduction gasoline stocks sulphur content according to claim 1, it is characterized in that the flow process reducing gasoline stocks sulphur content method is as follows: gasoline stocks enters separation column (2) through pipeline (1) and cuts into gently, heavy naphtha, wherein heavy naphtha is after pipeline (4) mixes with the sour distillate oil from pipeline (17), pump (6) is entered through pipeline (5), heavy naphtha after boosting is after pipeline (7) mixes with the hydrogen from pipeline (25), process furnace (9) is entered through pipeline (8), material after heating enters reactor (11) through pipeline (10) and contacts with Hydrobon catalyst, hydrogenated oil enters high-pressure separator (19) through pipeline (12), compressor (22) is entered through pipeline (21) from separator (19) top hydrogen-rich gas out, hydrogen-rich gas after compression is through pipeline (23) inlet pipe line (25) together with the supplementary live gas from pipeline (24), mix with the heavy distillate from pipeline (7), stabilizer tower is mixed through pipeline (20) with from extraction-washing light gasoline fraction of pipeline (27) is oily from separator (19) bottom hydrogenated heavy gasoline cut out, lighting end gasoline enters extraction tower (13) through pipeline (3), revivifier (16) is entered through pipeline (15) from extraction tower (13) bottom extraction phase out, the extraction agent separated from revivifier (16) bottom enters extraction tower (13) top through pipeline (18), oily through pipeline (17) and the heavy distillate mixing back end hydrogenation process from pipeline (4) from the sour distillate of revivifier (16) recovered overhead, from extraction tower (13) top, abstraction desulfurization benzoline out enters washing device (26) through pipeline (14), light gasoline fraction after washing mixes with the hydrogenated heavy gasoline cut from pipeline (20) through pipeline (27), mixed gasoline enters stabilizer tower (29) through pipeline (28), and separation obtains lighter hydrocarbons and gasoline products is drawn through pipeline (30), (31) respectively.
3. the method for reduction gasoline stocks sulphur content according to claim 1 and 2, it is characterized in that full distillation gasoline raw material to cut into light gasoline fraction and heavy naphtha, cutting temperature is 60 DEG C ~ 100 DEG C.
4. the method for reduction gasoline stocks sulphur content according to claim 1 and 2, is characterized in that light gasoline fraction enters abstraction desulfurization unit, obtains desulfurization light gasoline fraction and extraction phase; Extraction temperature is 25 DEG C ~ 60 DEG C, and extraction cells mainly removes the thiophene in lighting end gasoline, removes mercaptan, thioether, disulfides sulfide simultaneously.
5. the method for reduction gasoline stocks sulphur content according to claim 1 and 2, is characterized in that extraction phase enters reboiler, and steam the sulfur-bearing light gasoline fraction in extraction phase, the extraction agent of regeneration recycles, and regeneration temperature is 80 DEG C ~ 110 DEG C.
6. the method for reduction gasoline stocks sulphur content according to claim 1 and 2, is characterized in that abstraction desulfurization light gasoline fraction enters washing tower washing, removes the extraction agent be dissolved in oil, be extracted-wash light gasoline fraction; Washing composition is water, methyl alcohol, ethanol, ethylene glycol, glycerol, methane amide, or its mixture, and washing times comprises one or many.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US5411658A (en) * | 1991-08-15 | 1995-05-02 | Mobil Oil Corporation | Gasoline upgrading process |
| CN1465668A (en) * | 2002-06-27 | 2004-01-07 | 中国石油化工股份有限公司 | Method for producing low sulfur gasoline |
| CN101376842A (en) * | 2007-08-31 | 2009-03-04 | 中国石油化工股份有限公司 | Method for reducing sulfur content in gasoline |
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| CN101649221B (en) * | 2008-08-13 | 2012-12-12 | 中国石油天然气股份有限公司 | Method for producing reforming feedstock by light and medium gasoline distillates |
| CN101358145B (en) * | 2008-09-27 | 2012-12-12 | 天津大学 | Extractive agent for depriving sulphide in C9 fuel oil and depriving method |
| CN103468307A (en) * | 2013-09-13 | 2013-12-25 | 西南石油大学 | Method and device for desulfurizing catalytically cracked gasoline |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US5411658A (en) * | 1991-08-15 | 1995-05-02 | Mobil Oil Corporation | Gasoline upgrading process |
| CN1465668A (en) * | 2002-06-27 | 2004-01-07 | 中国石油化工股份有限公司 | Method for producing low sulfur gasoline |
| CN101376842A (en) * | 2007-08-31 | 2009-03-04 | 中国石油化工股份有限公司 | Method for reducing sulfur content in gasoline |
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