CN1312257C - Method for reducing olefin sulfur content in gasoline - Google Patents
Method for reducing olefin sulfur content in gasoline Download PDFInfo
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- CN1312257C CN1312257C CNB031022731A CN03102273A CN1312257C CN 1312257 C CN1312257 C CN 1312257C CN B031022731 A CNB031022731 A CN B031022731A CN 03102273 A CN03102273 A CN 03102273A CN 1312257 C CN1312257 C CN 1312257C
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Abstract
The present invention relates to a method for reducing the contents of olefin and sulfur in gasoline. The full fraction of gasoline is cut into light gasoline fraction and heavy gasoline fraction, wherein the light gasoline fraction is processed by alkali washing; the olefin of the heavy gasoline fraction is firstly saturated by hydrogenation reaction when the heavy gasoline fraction is desulfurized and denitrified, and then the dehydrogenation reaction is carried out to obtain the heavy gasoline fraction. The processed light gasoline fraction and the heavy gasoline fraction are mixed to obtain gasoline products with low olefin and sulfur contents and high octane values. The method can effectively reduce the contents of olefin and sulfur in gasoline. Meanwhile, the octane number of gasoline is basically unchanged, and the liquid yield of gasoline is high. Hydrogen gas generated by the dehydrogenation reaction can be used for the hydrogenation reaction, and therefore, the total hydrogen consumption of the hydrotreating process of gasoline is reduced.
Description
Technical field
The present invention relates to a kind of method for modifying of gasoline, more particularly, is a kind of method that reduces alkene in the gasoline, sulphur content.
Background technology
Along with the increasingly stringent of environmental regulation, the sulphur content and the olefin(e) centent of gasoline products are had higher requirement.The gasoline of China is formed to form with the gasoline of world market bigger difference, and the gasoline of China is based on catalytically cracked gasoline, and the shared share of reformed gasoline, gasoline alkylate and gasoline blend component MTBE is very little, and the production of isomerization gasoline is at the early-stage.Because the olefin(e) centent of catalytically cracked gasoline is very high and sulphur content is also higher, therefore have only the alkene and the sulphur content that reduce effectively in the gasoline could satisfy environmental protection requirement.The gasoline national standard that China implements at present requires content of sulfur in gasoline less than 800ppm, olefin(e) centent is less than 35v%, by 2003 and 2006, supply Shanghai, Beijing and Guangzhou three metropolitan gasoline require to reach " world's fuel oil standard " II class and III class standard, be sulphur content respectively less than 200ppm and 30ppm, olefin(e) centent is respectively less than 20v% and 10v%.
The gasoline desulfur technology has hydrogenation and non-hydrogenation two classes, hydrogen addition technology is industrial mature and feasible and highly effective desulfurization technology, non-hydrogenating desulfurization technology has: adsorption desulfurize technology, biological desulfurizing technology, oxidative desulfurization techniques etc., non-hydrogenating desulfurization technology is in the research and development stage, realize that industrial application also has many problems to need to solve.Reducing olefin content in gasoline has only the method for employing hydrogenation to realize.Therefore, solve China's content of olefin in gasoline and the higher problem of sulphur content and have only the employing hydrogen addition technology.
Adopt hydrogen addition technology can reduce olefin content in gasoline and sulphur content, yet the alkene in the gasoline is high-octane number component, adopt hydrogen addition technology to make the saturated decline that will cause gasoline octane rating of alkene, therefore, adopting hydrogen addition technology merely is the requirement that is difficult to satisfy to gasoline quality.For when adopting hydrogen addition technology to reduce gasoline olefin and sulphur content, keep the octane value of gasoline effectively, also must carry out suitable processing, to recover the octane value of gasoline products to the logistics behind the gasoline hydrogenation.USP5,391,288 have proposed a kind of catalytically cracked gasoline sulfur removal technology, catalytically cracked gasoline at first passes through hydrotreating reactor, saturated contained alkene, and remove impurity such as sulphur, nitrogen, logistics after the hydrotreatment is sent in the octane value recovering reactor at rear portion, also have one material that is rich in benzene to enter the rear portion reactor in addition, the cracking reaction of straight-chain paraffin and the alkylated reaction of benzene take place in the reactor of rear portion, make gasoline octane rating after the hydrotreatment that to a certain degree recovery be arranged.USP5,399, the characteristics of the 258 catalytically cracked gasoline sulfur removal technologies that propose are, saturation of olefins in the at first fore hydrotreating reactor of catalytically cracked gasoline, and desulfurization removing nitric, in the octane value recovering reactor at rear portion, carry out the isomerization reaction of cracking reaction and normal paraffin, so that the octane value of gasoline has the recovery of a degree.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology alkene, sulphur content method in a kind of reduction gasoline, but oily octane value does not lose substantially.
Method provided by the invention comprises:
(1), with the full feedstock of gasoline be cut into light, weigh two kinds of gasoline fractions, cut point is 70 ℃～100 ℃;
(2), light gasoline fraction is handled through alkali cleaning;
(3), heavy naphtha is earlier through hydrogenation reaction saturated its alkene desulfurization simultaneously and denitrogenation, and then through dehydrogenation reaction generating portion aromatic hydrocarbons, hydrogenation conditions is: hydrogen dividing potential drop 1.0～4.0MPa; 200～280 ℃ of temperature of reaction, liquid hourly space velocity 2.0～8.0h
-1, hydrogen-oil ratio 200～1000Nm
3/ m
3, dehydrogenation reaction conditions is: the temperature in of reactor is 480～540 ℃, and working pressure is 0.2～3.0MPa, and volume space velocity is 3～6h
-1, hydrogen/oil mol ratio is 1.0～6.0;
(4), light, the heavy naphtha mixing after handle step (2), (3) obtains gasoline products respectively.
Method provided by the invention is when reducing gasoline olefin, sulphur content effectively, and gasoline octane rating does not lose substantially, and the liquid yield height of gasoline; The hydrogen that dehydrogenation reaction produces can be used for hydrogenation reaction, reduces the total hydrogen consumption of gasoline hydrogenation treating processes.
Description of drawings
Accompanying drawing is that heavy naphtha is handled synoptic diagram in the method provided by the invention.
Embodiment
The present invention is so concrete enforcement:
Earlier with the full cut of gasoline through separation column cut into light, weigh two kinds of gasoline fractions, cut point is 70 ℃～100 ℃; Respectively light gasoline fraction is carried out alkali cleaning then and handles, to heavy naphtha carry out hydrotreatment successively, dehydrogenation is handled, light, the heavy naphtha mixing after will handling at last obtains alkene, sulphur content is low and octane value is higher gasoline products.
Described gasoline stocks is catalytically cracked gasoline, catalytic cracking gasoline, coker gasoline, pressure gasoline etc. or its mixture.The preferred raw material of the present invention is a catalytically cracked gasoline.The characteristics of catalytically cracked gasoline are: lighting end internal olefin content is higher, is high-octane number component, and is bigger to the contribution of octane value, and the sulphur content in the lighting end is less, mainly exists with the mercaptan form, and mercaptan sulfur can be removed with the alkali cleaning method of routine.Concentrated the most of sulphur in the catalytically cracked gasoline in the last running, and mainly be based on thiophene sulphur, be difficult to remove with conventional alkali cleaning method, saturated to the hydrogenation of olefins in the last running in addition, the loss of gasoline octane rating is less.As above characteristics in view of catalytically cracked gasoline, to realize simultaneously that catalytically cracked gasoline reduces olefin(e) centent and reduces sulphur content again, can catalytically cracked gasoline be divided into light, weigh two kinds of cuts, lighting end removes wherein mercaptan sulfur with conventional alkali cleaning method, and the method for hydrotreatment is adopted in last running, make the saturated and desulfurization of alkene,, can adopt appropriate means to recover its octane value for the loss of octane number that last running produces owing to alkene is saturated.
In the alkali cleaning treating processes of light gasoline fraction, mercaptan in the light gasoline fraction and alkaline reaction generate thiolate, thiolate is oxidized to disulphide under the effect of metallo-chelate, with organic solvent disulphide is extracted again, thereby realization reduces the purpose of sulphur content in the light gasoline fraction.
The present invention relates generally to the processing of heavy naphtha.After handling through front and back two portions reactive system, heavy naphtha obtains not having the gasoline component of alkene super low sulfur.
The flow process of anterior reactive system is: the at first incoming stock oily surge tank of heavy naphtha, behind fresh feed pump, mix with recycle hydrogen, heat exchange enters hydrogenator after reaching 200～280 ℃, hydrogenation reactions such as the saturated and desulfurization of alkene, denitrogenation take place in hydrogenator, and reaction conditions is as follows: hydrogen dividing potential drop 1.0～4.0MPa; 200～280 ℃ of temperature of reaction, liquid hourly space velocity 2.0～8.0h
-1, hydrogen-oil ratio 200～1000Nm
3/ m
3Because of hydrogenation reaction is a strong exothermal reaction, for the effectively temperature rise of control reaction, generally the beds in the hydrogenator is divided into a plurality of beds, between two adjacent beds, add cold hydrogen, temperature is that 300～350 ℃ hydrogenation reaction logistics goes out behind the reactor and the charging heat exchange, pass through air cooling, water-cooled then respectively, enter gas-liquid separator and carry out the separation of gas-liquid two-phase, the liquid phase of gas-liquid separator enters stripping tower, isolate a spot of light constituent, and removing institute's dissolved hydrogen sulfide, ammonia and moisture, the heavy naphtha at the bottom of the tower removes the rear portion reactive system.The used hydrogenation catalyst of anterior reactive system is made up of VIB and/or VIII family base metal and unformed aluminum oxide or silica-alumina supports.
The flow process of rear portion reactive system is: the heavy naphtha at the bottom of the stripping tower mixes with recycle hydrogen after through the fresh feed pump of rear portion reactive system, enter process furnace through after the heat exchange, temperature is that 480～540 ℃ logistics enters dehydrogenation reactor, the number of dehydrogenation reactor is one or two, in dehydrogenation reactor, carry out naphthenic hydrocarbon dehydrogenation reaction, part cyclization of paraffins dehydrogenation reaction etc., the temperature in of reactor is 480～540 ℃, and working pressure is 0.2～3.0MPa, and volume space velocity is 3～6h
-1, hydrogen/oil mol ratio is 1.0～6.0.Dehydrogenation reaction is thermo-negative reaction, after the reactant outflow dehydrogenation reactor of certain temperature drop is arranged, with the charging heat exchange, pass through air cooling and water-cooled subsequently successively, enter gas-liquid separator, in gas-liquid separator, finish the separation of gas-liquid two-phase, the liquid phase of gas-liquid separator is sent into gasoline stabilizer, remove the wherein following light constituent of C4, obtain super low sulfur, no alkene and the very little gasoline component of loss of octane number, mix the gasoline products that promptly obtains low alkene, low sulfur content with the light gasoline fraction that passes through after alkali cleaning is handled.It is carrier that reactive system used dehydrogenation catalyst in rear portion is formed with the aluminum oxide, is active ingredient with VIII family metals such as platinum, palladium, iridium, rhodiums, is promotor with metals such as rhenium, tin.Catalyzer in the dehydrogenation reactor is with the filling of fixed bed form, and the beds in the dehydrogenation reactor also can be moving-bed, catalyzer cyclic regeneration in independent revivifier.
Forwardly the hydrogenator of reactive system is interior except that olefin saturation takes place refining reactions such as desulfurization, denitrogenation takes place also, produces hydrogen sulfide and ammonia.The amine absorption process is adopted in removing of hydrogen sulfide, and promptly the gas phase of gas-liquid separator removes wherein hydrogen sulfide by the amine absorption tower; The removal methods of ammonia is to inject a certain amount of water before air cooler, and ammonia is dissolved in the water, and the water that will be dissolved with ammonia at gas-liquid separator drains into sink drainage.After the gas phase on anterior reactive system process amine absorption tower and the gas phase of rear portion reactive system gas-liquid separator are converged, through the recycle compressor supercharging, respectively as the recycle hydrogen of anterior reactive system and the recycle hydrogen of cold hydrogen and rear portion reactive system.What take place in the anterior reactor is hydrogenation reaction, and what take place in the reactor of rear portion is dehydrogenation reaction, and the dehydrogenation degree of depth in the reactor of rear portion is not high, when intrasystem hydrogen can not reach self-equilibrating, need replenish a spot of hydrogen in system.
What take place in the hydrogenator of anterior reactive system is thermopositive reaction, adds hot feed with this reaction institute liberated heat, can save the charging process furnace of anterior reactive system, thus the economizer energy consumption.Going into operation the stage of device, be that charging is operated with refining virgin naphtha or hydrocracking petroleum naphtha earlier in the reactive system of rear portion, the outlet logistics of dehydrogenation reactor and the charging heat exchange of anterior hydrogenator, make the charging of hydrogenator reach the reactor inlet temperature requirement, thereby make the olefin saturation in the hydrogenator, reactions such as desulfurization removing nitric are normally carried out, utilize this moment the outlet logistics of hydrogenator just can keep normal running to the charging heating, anterior reactive system just can transfer the ordinary production flow process to, and then the rear portion reactive system is switched to the ordinary production flow process.
Hydrogenation reaction and dehydrogenation reaction can be shared a cover hydrogen gas circulating system, also can have an independently cover hydrogen gas circulating system respectively.When the working pressure grade of hydrogenation reaction and dehydrogenation reaction is identical, the shared cover hydrogen gas circulating system of hydrogenation reaction and dehydrogenation reaction; When the working pressure of hydrogenation reaction and dehydrogenation reaction differed big, hydrogenation reaction and dehydrogenation reaction had an independently cover hydrogen gas circulating system respectively.
Below in conjunction with accompanying drawing method provided by the present invention is further detailed, but not thereby limiting the invention.
Accompanying drawing is that heavy naphtha is handled synoptic diagram in the method provided by the invention.
The flow process of this method is as follows: heavy naphtha enters fresh feed pump 2 through pipeline 1, by fresh feed pump 2 superchargings after pipeline 3 with enter pipeline 4 after recycle hydrogen from pipeline 69 mixes, successively through interchanger 5, pipeline 6, interchanger 7, pipeline 8 enters hydrogenator 9, beds in the hydrogenator is divided into three sections, cold hydrogen enters between one or two sections beds through pipeline 67 and pipeline 68 respectively, between two or three sections beds, hydrogenator outlet logistics is drawn by pipeline 10, through interchanger 5 with after the water that injects through pipeline 11 mixes, successively through pipeline 12, air-cooler 13, pipeline 14, water cooler 15 and pipeline 16 enter gas-liquid separator 17, sewage enters sink drainage through pipeline 18, the oil phase of gas-liquid separator 17 is then successively through pipeline 19, interchanger 20 and pipeline 21 enter stripping tower 22, the gas phase of stripping cat head is passed through pipeline 23 successively, air-cooler 24, pipeline 25, watercooler 26 and pipeline 27 enter stripping return tank of top of the tower 28, the water of return tank is through pipeline 30 decontaminated water treatment systems, gas phase is then gone fuel gas system through pipeline 29, the part of oil phase is made trim the top of column through pipeline 32, another part is made pentane oil and is gone out device through pipeline 31, stripping tower 22 bottoms are drawn by pipeline 33, a part is successively through pipeline 34, return at the bottom of the tower behind the reboiler 35, another part is then successively through pipeline 36, interchanger 20, pipeline 37, pump 38 and pipeline 39 are with after recycle hydrogen from pipeline 66 mixes, successively through pipeline 40, interchanger 41 and pipeline 42 enter process furnace 43, the logistics that is heated to preset temperature enters dehydrogenation reactor 45 through pipeline 44, cycloalkanes dehydrogenation reaction and part cyclization of paraffins dehydrogenation reaction take place in dehydrogenation reactor, pipeline 46 is passed through in the outlet logistics of dehydrogenation reactor successively, interchanger 7, pipeline 47, interchanger 41, pipeline 48, air-cooler 49, pipeline 50, watercooler 51 and pipeline 52 enter gas-liquid separator 53, water in the gas-liquid separator 53 enters sink drainage through pipeline 54, and oil phase is then sent to gasoline stabilizer through pipeline 55 and removed the following light constituent of C4.
The gas phase of gas-liquid separator 17 enters amine absorption tower 58 through pipeline 57, poor amine is introduced the amine absorption tower through pipeline 59, rich amine is then drawn through pipeline 60, the gas phase of absorb handling through amine through pipeline 61 with mix from the gas phase of pipeline 56 after enter recycle compressor 62, the new hydrogen that replenishes through pipeline 64 with enter pipeline 65 after the gas phase in the recycle compressor outlet line 63 is mixed, gas phase in the pipeline 65 is divided into four the tunnel: the recycle hydrogen of anterior reactive system mixes with charging through pipeline 69, the recycle hydrogen of rear portion reactive system mixes with charging through pipeline 66, and the cold hydrogen of hydrogenator is introduced hydrogenator by pipeline 67 and 68 respectively.
Method advantage provided by the invention is:
1, method provided by the invention is when reducing gasoline olefin, sulphur content effectively, and gasoline octane rating does not lose substantially, and the liquid yield height of gasoline.
2, hydrogenation reaction is the consumption H-H reaction, the catalytic cracking treatment capacity of domestic refinery is generally all bigger, and catalytically cracked gasoline is carried out hydrotreatment, can consume a large amount of hydrogen, the hydrogen balance that this can have influence on full factory on the one hand can increase the cost that gasoline hydrogenation is handled on the other hand.What the present invention adopted is to carry out hydrogenation reaction in the fore reactor of catalytically cracked gasoline, in the reactor at rear portion, carry out the dehydrogenation reaction of naphthenic hydrocarbon, the hydrogen that dehydrogenation reaction produces can be used for the hydrogenation reaction of front reactor, the total hydrogen consumption that this has just reduced the catalytic gasoline hydrogenation treating processes has effectively reduced tooling cost.
3, hydrogenation reaction is a strong exothermal reaction, and the present invention has effectively utilized hydrogenation reaction institute liberated heat.Go into operation the stage at device, need the outlet logistics of rear portion reactor to heat for the charging of anterior reactor, activate the hydrogenation reaction in the anterior reactor, generation along with hydrogenation reaction, because a large amount of heats is emitted in reaction, the outlet logistics of anterior reactor has had higher temperature, just can satisfy the needs of normal running with the outlet logistics heating inlet logistics of this reactor, therefore, the present invention has effectively utilized hydrogenation reaction institute liberated heat, anterior reactor is not being established separately under the condition of process furnace, also can be realized the needs of ordinary production.
4, because the aromatization degree in the dehydrogenation reactor of rear portion is not high, so dehydrogenation reaction can carry out under higher air speed, and the catalyst levels in the reactive system is little, helps reducing investment outlay.
5, when anterior hydrogenator and rear portion dehydrogenation reactor are operated under close pressure, can satisfy the needs of front and rear reactive system gas circulation with same recycle compressor, help save energy, and save facility investment.
The following examples will give further instruction to present method, but therefore not limit present method.
Embodiment
Present embodiment has provided the reaction conditions and the reaction result of 100,000 tons/year catalytically cracked gasoline last running medium-sized test.In this embodiment, anterior hydrogenation reaction system and rear portion dehydrogenation reactor system have independently hydrogen gas circulating system separately.
The research octane number (RON) of the full feedstock of catalytically cracked gasoline is 90.5, and olefin(e) centent is 50.3v%, and sulphur content is 130ppm, and flow is 18657kg/h,
1. the cutting of the full feedstock of gasoline
Gently, the last running cut point is 73 ℃, the cutting ratio is: lighting end 33.0 heavy %, last running 67.0 heavy %, then the flow of lighting end is 6157kg/h, the flow of last running is 12500kg/h.
2. the alkali cleaning of light gasoline fraction is handled
The sulphur content of light gasoline fraction is 59ppm, handles the back mercaptan sulfur content with alkali lye and reduces to 18ppm.
3. the processing of heavy naphtha
(1). anterior hydrogenation reaction system
Beds in the hydrogenator is divided into three sections, between one or two sections beds, replenish cold hydrogen between two or three sections beds, in order to control reaction temperature.
Feed properties and composition:
Charging density: 748kg/m
3Feed sulphur content: 162ppm
Feed composition: alkane 26.28 heavy %, alkene 41.42 heavy %, naphthenic hydrocarbon 8.42 heavy %, aromatic hydrocarbons 23.81 heavy %
Charging research octane number (RON): 86.5
Feed rate: 12500kg/h
Loaded catalyst: 4.18m
3
Catalyzer model: RS-1 (producing) by Chang Ling oil-refining chemical head factory catalyst plant
Volume space velocity: 4h
-1
Recycle hydrogen flow: 10100Nm
3/ h
One section cold hydrogen flow: 2240Nm
3/ h
Two sections cold hydrogen flow: 3136Nm
3/ h
Working pressure: 3.8MPa
Hydrogen dividing potential drop: 3.0MPa
Reactor inlet hydrogen-oil ratio: 600Nm
3/ m
3
Reactor inlet temperature: 220 ℃
Reactor outlet temperature: 310 ℃
Chemistry hydrogen consumption: 1.36 heavy %
Hydrogenation products character and composition:
Product is formed: alkane 57.53 heavy %, alkene 0, naphthenic hydrocarbon 15.66 heavy %, aromatic hydrocarbons 26.34 heavy %
Hydrogenation products research octane number (RON): 58.7
Stripping tower bottom product flow: 12543kg/h
Sulphur content: less than 0.5ppm
(2). the rear portion dehydrogenation reactor system
Dehydrogenation reactor system comprises two reactors, and the reactant flow order is through two reactors.
Inlet amount: 12543kg/h
Loaded catalyst: 2586kg
Catalyzer model: CB-6 (producing) by Chang Ling oil-refining chemical head factory catalyst plant
Volume space velocity: 5h
-1
Working pressure: 1.4MPa
First reactor inlet temperature: 520 ℃
First reactor outlet temperature: 470 ℃
Second reactor inlet temperature: 520 ℃
Second reactor outlet temperature: 484 ℃
Reaction product research octane number (RON): 84.2
Hydrogen yield: 1.40 heavy %
C5+ liquid yield: 93.9 heavy %
Reaction product aromaticity content: 53.5 heavy %
Sulphur content: less than 0.5ppm
4. light, heavy naphtha after handling are in harmonious proportion
Heavy naphtha is after hydrotreatment and dehydrogenation reaction, and the C5+ liquid yield is 94.2 heavy %, and flow is 11778kg/h.Through the heavy naphtha of hydrotreatment and dehydrogenation reaction with become gasoline products after light gasoline fraction through caustic wash desulfuration alcohol mixes, this product is 96.1 heavy % to the liquid yield of the full feedstock of gasoline, olefin(e) centent is reduced to 19.3v%, sulphur content only is 6ppm, aromaticity content is 30.2v%, research octane number (RON) is 89.6, only loses 0.9 unit.
Claims (6)
1, alkene and sulphur content method in a kind of reduction gasoline is characterized in that this method comprises the following steps:
(1), with the full feedstock of gasoline be cut into light, weigh two kinds of gasoline fractions, cut point is 70 ℃～100 ℃;
(2), light gasoline fraction is handled through alkali cleaning;
(3), heavy naphtha is earlier through hydrogenation reaction saturated its alkene desulfurization simultaneously and denitrogenation, and then through dehydrogenation reaction generating portion aromatic hydrocarbons, hydrogenation conditions is: hydrogen dividing potential drop 1.0～4.0MPa; 200～280 ℃ of temperature of reaction, liquid hourly space velocity 2.0～8.0h
-1, hydrogen-oil ratio 200～1000Nm
3/ m
3, dehydrogenation reaction conditions is: the temperature in of reactor is 480～540 ℃, and working pressure is 0.2～3.0MPa, and volume space velocity is 3～6h
-1, hydrogen/oil mol ratio is 1.0～6.0;
(4), light, the heavy naphtha mixing after handle step (2), (3) obtains gasoline products respectively.
2,, it is characterized in that the full feedstock of described gasoline is catalytically cracked gasoline, catalytic cracking gasoline, coker gasoline, pressure gasoline or its mixture according to the method for claim 1.
3,, it is characterized in that the hydrogenation reaction and the shared cover hydrogen gas circulating system of dehydrogenation reaction of step (3) according to the method for claim 1.
4,, it is characterized in that the hydrogenation reaction of step (3) and dehydrogenation reaction have an independently cover hydrogen gas circulating system respectively according to the method for claim 1.
5,, it is characterized in that the interior catalyzer of dehydrogenation reactor of step (3) loads with the fixed bed form according to the method for claim 1.
6,, it is characterized in that the interior beds of dehydrogenation reactor of step (3) is a moving-bed, catalyzer cyclic regeneration in independent revivifier according to the method for claim 1.
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|---|---|---|---|
| CNB031022731A CN1312257C (en) | 2003-01-30 | 2003-01-30 | Method for reducing olefin sulfur content in gasoline |
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|---|---|---|---|
| CNB031022731A CN1312257C (en) | 2003-01-30 | 2003-01-30 | Method for reducing olefin sulfur content in gasoline |
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| CN1312257C true CN1312257C (en) | 2007-04-25 |
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| CNB031022731A Expired - Lifetime CN1312257C (en) | 2003-01-30 | 2003-01-30 | Method for reducing olefin sulfur content in gasoline |
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Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101275085B (en) * | 2007-03-30 | 2012-01-25 | 中国石油化工股份有限公司 | Combined method for gasoline desulfurization |
| CN102851068B (en) * | 2011-06-29 | 2015-02-25 | 中国石油化工股份有限公司 | Gasoline desulfurization method |
| CN103059956B (en) * | 2011-10-21 | 2015-01-14 | 中国石油化工股份有限公司 | Deep hydrodesulfurization method for catalytic gasoline |
| CN103695035B (en) * | 2012-09-28 | 2015-08-26 | 中国石油化工股份有限公司 | A kind of combined method of producing super low-sulfur oil |
| CN103409162B (en) * | 2013-07-17 | 2015-12-09 | 辽宁石油化工大学 | Pretreatment process before a kind of hydrogenation of coker gasoline |
| CN103740407B (en) * | 2014-01-21 | 2015-07-01 | 武汉工程大学 | Alkali cleaning-extraction-washing-hydrogenation combined process for producing low-sulfur-content gasoline |
| CN107011941A (en) * | 2016-01-28 | 2017-08-04 | 中国石油天然气集团公司 | The device and method of gasoline hydrogenation modification production super low-sulfur oil inferior |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5391288A (en) * | 1991-08-15 | 1995-02-21 | Mobil Oil Corporation | Gasoline upgrading process |
| US5399258A (en) * | 1991-08-15 | 1995-03-21 | Mobil Oil Corporation | Hydrocarbon upgrading process |
| CN1253993A (en) * | 1998-11-18 | 2000-05-24 | 法国石油公司 | Production method of low-sulfur gasoline |
| EP1031622A1 (en) * | 1999-02-24 | 2000-08-30 | Institut Francais Du Petrole | Process for the production of low sulphur gasolines |
| CN1319644A (en) * | 2000-03-29 | 2001-10-31 | 法国石油公司 | Gasoline desulfurating method containing process for rectifying of at least three fractions and intermediate fraction desulfurating |
-
2003
- 2003-01-30 CN CNB031022731A patent/CN1312257C/en not_active Expired - Lifetime
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5391288A (en) * | 1991-08-15 | 1995-02-21 | Mobil Oil Corporation | Gasoline upgrading process |
| US5399258A (en) * | 1991-08-15 | 1995-03-21 | Mobil Oil Corporation | Hydrocarbon upgrading process |
| CN1253993A (en) * | 1998-11-18 | 2000-05-24 | 法国石油公司 | Production method of low-sulfur gasoline |
| US6334948B1 (en) * | 1998-11-18 | 2002-01-01 | Institut Francais Du Petrole | Process for producing gasoline with a low sulphur content |
| EP1031622A1 (en) * | 1999-02-24 | 2000-08-30 | Institut Francais Du Petrole | Process for the production of low sulphur gasolines |
| CN1319644A (en) * | 2000-03-29 | 2001-10-31 | 法国石油公司 | Gasoline desulfurating method containing process for rectifying of at least three fractions and intermediate fraction desulfurating |
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| CN1521241A (en) | 2004-08-18 |
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