CN1590509A - Modification method of gasoline cut fraction - Google Patents
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Abstract
一种汽油馏分的改质方法，汽油原料和氢气先与加氢精制催化剂接触，在氢分压0.5～6.0MPa、温度200～420℃、液时空速0.5～10.0h－1、氢油比50～1500v/v的条件下反应，反应流出物和氢气再与辛烷值恢复催化剂接触，在氢分压0.5～6.0MPa、温度200～460℃、液时空速0.5～10.0h－1、氢油比50～1500v/v的条件下反应，分离反应流出物得到汽油产品，回收的富氢气体循环使用。该方法能将汽油中硫含量降至30ppm以下，烯烃含量降至10v％以下，而辛烷值基本不损失，满足世界燃油规范中III类汽油标准。A method for upgrading gasoline fractions. The gasoline raw material and hydrogen are first contacted with a hydrorefining catalyst at a hydrogen partial pressure of 0.5-6.0MPa, a temperature of 200-420°C, a liquid hourly space velocity of 0.5-10.0h -1 , and a hydrogen-to-oil ratio of 50 Reaction under the condition of ~1500v/v, the reaction effluent and hydrogen are then contacted with the octane number recovery catalyst, at a hydrogen partial pressure of 0.5~6.0MPa, a temperature of 200~460℃, a liquid hourly space velocity of 0.5~10.0h -1 , hydrogen oil The reaction is carried out under the condition of ratio 50-1500v/v, the reaction effluent is separated to obtain a gasoline product, and the recovered hydrogen-rich gas is recycled. The method can reduce the sulfur content in gasoline to less than 30ppm, and the olefin content to less than 10v%, without substantially losing the octane number, and meets the standard of Class III gasoline in the world fuel oil specification.
Description
Technical field
The invention belongs in the method that has refining hydrocarbon ils under the situation of hydrogen, more particularly, is the method for modifying that belongs to a kind of gasoline fraction.
Background technology
Vehicle fuel all has significant effects to performance, efficient, weather resistance, the environmental protection effect of automobile or engine.The quality of initial vehicle fuel is mainly and satisfies the vehicle technology performance demands; along with the continuous reinforcement of society to environmental protection requirement; it should be noted that the material impact of vehicle fuel for the automobile product discharging; and corresponding requirement proposed; the discharging of hazardous and noxious substances will be strictly controlled in the vehicle exhaust, therefore require more and more tighter to oil quality.The U.S. requires reformulated gasoline to 2006 year sulphur content less than 30ppm, and olefin(e) centent is less than 14v%.The II that " world's fuel oil standard " proposes, III class gasoline standard require sulphur content less than 200ppm, 30ppm, and olefin(e) centent is respectively less than 20v%, 10v%.
The subject matter of the present gasoline of China is sulphur content, olefin(e) centent height, this mainly contains the reason of two aspects: 1. the working ability of China's catalytic cracking (FCC) accounts for the large percentage of secondary processing, the olefin(e) centent height of FCC gasoline, usually at 40～55v%, have up to 60v%, FCC gasoline is the main source of commercial gasoline, and other gasoline blend component is few, thereby makes the olefin(e) centent height of commercial gasoline.2. China's catalyzed cracking processing raw material develops to the heaviness direction, and import high-sulfur crude oil amount is also in continuous rising, and sulphur content, olefin(e) centent will continue to maintain higher level in the catalytically cracked gasoline.Therefore sulphur and the alkene in the FCC gasoline is commercial gasoline sulphur and alkene main source.Western developed country FCC gasoline proportion in whole gasoline blend component is about 1/3, olefin(e) centent is not high, be generally 20～30%, and aromaticity content height, usually about 40%, the difference of this and China FCC gasoline is bigger, and the FCC gasoline hydrogenation treatment technology of external exploitation is handled the lower raw material of olefin(e) centent and had result preferably, be used to handle the FCC gasoline of domestic high olefin content, loss of octane number is bigger.Therefore, exploitation is fit to the FCC desulfurizing and reducing olefine for gasoline technology of China, and the quality of gasoline that satisfies domestic increasingly stringent requires and enlarge fuel dispensing outlet to have important practical significance.
The pre-treatment of FCC raw material hydrogenation can reduce the FCC content of sulfur in gasoline, gasoline yield also can improve 7～9m% simultaneously, coke reduces about 10m%, but when requiring content of sulfur in gasoline further to be reduced to 30ppm when following, FCC gasoline still needs further desulfurization, deolefination.Though traditional FCC gasoline hydrofinishing technology can reduce sulphur content and olefin(e) centent, because the high-octane olefin component of hydrogenation process by saturated in a large number, causes the gasoline octane rating loss very big, desulfurization degree is high more, and the gasoline octane rating loss is big more.Therefore, press for a kind of new little FCC deep desulfurization olefin hydrocarbon reduction of gasoline technology of loss of octane number of exploitation at present.
US5510016 discloses a kind of method of gasoline upgrading, the process hydrofining earlier of FCC petroleum naphtha reduces the sulphur content in the raw material, in this process, can lose the part octane value, selective cracking takes place and reacts boosting of octane rating by containing mesoporous molecular sieve ZSM5 an acidic catalyst in the intermediate product behind the hydrogenation.Because be to recover octane value by cracking reaction takes place, in order to guarantee yield of gasoline, this method is fit to handle the FCC heavy naphtha fraction.
US5503734 discloses a kind of method of gasoline upgrading, the process hydrofining earlier of FCC petroleum naphtha reduces the sulphur content in the raw material, in this process, can lose the part octane value, intermediate product behind the hydrogenation passes through an acidic catalyst, this catalyzer comprises mesoporous molecular sieve (as ZSM5) and large pore molecular sieve (as contain metal Ni and Mo USY), selective cracking takes place on an acidic catalyst react boosting of octane rating.Under similarity condition, adopt the transformation efficiency height of two kinds of molecular sieves than any molecular sieve.
US6228254 discloses and has adopted mild hydrogenation to make with extra care and extract in conjunction with the method that obtains low-sulphur oil, first section than the demulcent hydroconversion condition under, ring-opening reaction can take place and be converted into mercaptan in 95% aromatic sulfur-containing heterogeneous ring compound, so the mercaptans content of intermediate product increases.Second section is adopted solid adsorbent or liquid extractant to remove mercaptan.This method can obtain high yield of gasoline, and the loss of octane number of product is very little or do not lose.
WO9853030 discloses two sections method for modifying of gasoline.First section under the demulcent treatment condition, low-octane paraffinic hydrocarbons and alkene are selected the type cracking reaction, thereby have reduced the alkene of raw material.Second section is carried out hydrofining reaction reduction sulphur content, owing to removed alkene at first section, second section hydrogenation is little to the octane value influence of raw material.Alkene obtains transforming before hydrofining, so this method reduced olefin saturation and reduced the hydrogen consumption, and back end hydrogenation has also been avoided the problem that hydrogen sulfide and alkene generate mercaptan and needs further to handle on molecular sieve catalyst.
US5599439 discloses a kind of technology of handling heavy FCC gasoline, and this technology can reduce the benzene content that is rich in aromatic fraction when recovering the hydrogenating desulfurization gasoline octane rating.First section is carried out hydrofining to the sour gasoline cut and removes impurity and saturation of olefins such as sulphur, nitrogen, and the sulphur content that obtains intermediate product reduces, octane value descends.Second section employing fluidized-bed reactor enters second section after intermediates oil mixes the raw material that is rich in aromatic hydrocarbons, obtains the high gasoline fraction of octane value under proper reaction conditions, thereby the octane value of raw material is restored.No longer mend new hydrogen for second section.Working pressure is low excessively, is unfavorable for the long-term operation of catalyzer.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology a kind of method for modifying of gasoline fraction to reduce its sulphur, olefin(e) centent and to guarantee that its octane value does not lose substantially.
Method provided by the invention comprises: gasoline stocks contacts with Hydrobon catalyst earlier with hydrogen, at hydrogen dividing potential drop 0.5～6.0MPa, 200～420 ℃ of temperature, liquid hourly space velocity 0.5～10.0h
-1, hydrogen-oil ratio 50～1500v/v condition under react, reaction effluent contacts with octane value recovering catalyst with hydrogen again, at hydrogen dividing potential drop 0.5～6.0MPa, 200～460 ℃ of temperature, liquid hourly space velocity 0.5～10.0h
-1, hydrogen-oil ratio 50～1500v/v condition under react, the separating reaction effluent obtains gasoline products, the hydrogen-rich gas of recovery recycles.
Method provided by the invention can be reduced to sulfur in gasoline content below the 30ppm, and olefin(e) centent is reduced to below the 10v%, and octane value does not lose substantially, satisfies III class gasoline standard in world's fuel oil standard.
Description of drawings
Accompanying drawing is the method for modifying synoptic diagram of gasoline fraction provided by the invention.
Embodiment
Basic thought of the present invention is as follows:
FCC gasoline can be divided into normal paraffin (n-P), isoparaffin (i-P), naphthenic hydrocarbon (N), alkene (O) and five components of aromatic hydrocarbons (A) from forming, and wherein the octane value of normal paraffin is low, and the long more octane value of carbochain is low more.The octane value of isoparaffin is higher, and the collateralization degree is high more, it is high more to arrange compact more octane value.Alkene, aromatic hydrocarbons are high-octane number components, especially with the octane value of aromatic hydrocarbons for the highest.China's catalytically cracked gasoline presents the feature of high olefin, low arene content, and about 50%, aromaticity content is less than 20% usually for olefin(e) centent.As seen alkene is the important component in China FCC gasoline octane rating source, thereby the variation of olefin(e) centent is very big to the influence of FCC gasoline octane rating.In FCC gasoline hydrogenation process, it is low-octane alkane that alkene is easy to hydrogenation saturated, causes gasoline octane rating to decline to a great extent.The full distillation gasoline of a kind of FCC gasoline is carried out hydropyrolysis experiment, catalyzer is conventional Hydrobon catalyst, when content of olefin in gasoline when 49.3v% drops to 19.3v%, gasoline research method octane value RON loss reaches 12.3 units, when the alkene saturation exponent reaches 100%, RON loss reaches 23.5 units, and obviously the full distillation gasoline of FCC adopts conventional method of hydrotreating to fall the alkene desulfurization to be difficult to accept.
By above in-depth analysis and understanding to FCC gasoline, established basic thought of the present invention: with FCC gasoline staging treating, the hydrofining of first section process removes impurity such as sulphur nitrogen, the intermediate product that obtains in this process causes octane value to reduce owing to hydrogenation of olefins is saturated, second section by cracking reaction and isomerization reaction, and low-octane paraffin conversion is the octane value recovering that high-octane isoparaffin makes product.Adopt stripping tower between first section and second section without step-down, can avoid the hydrogen sulfide of one section generation to be converted into a spot of mercaptan and second section activity of such catalysts of ammonia reduction, reduce FCC sulfur in gasoline, olefin(e) centent thereby reach, the purpose of the low loss of octane number that keeps simultaneously trying one's best.
Full cut FCC gasoline is carried out hydrogenation of total effluent make with extra care,, adopt the method for hydrogenation can realize deep desulfuration, and make hydrogenation of olefins saturated, thereby FCC sulfur in gasoline, olefin(e) centent are significantly reduced simultaneously for the high FCC gasoline of sulphur content.But alkene is the important component in China FCC gasoline octane rating source, the variation of olefin(e) centent is very big to the influence of FCC gasoline octane rating, if just simply FCC gasoline is carried out conventional hydrofining, still can there be the bigger problem of loss of octane number, therefore, the full cut of the FCC after the hydrofining is carried out the difficult point that octane value recovering becomes technology of the present invention.
Operational path of the present invention can be summarized as follows:
According to the product property of feedstock property and requirement, FCC gasoline enters fixed bed hydrogenation refining reaction device with after hydrogen mixes, and contacts with Hydrobon catalyst, at hydrogen dividing potential drop 0.5～6.0MPa, 200～420 ℃ of temperature, liquid hourly space velocity 0.5～10.0h
-1, hydrogen-oil ratio 50～1500v/v condition under react, stripping tower in the middle of entering through the reaction effluent that obtains after the refinement treatment removes the H that generates in the hydrogenation process
2S, NH
3After enter octane value recovering section reactor cracking reaction mainly take place, also have isomerization reaction simultaneously, this reactor outlet effluent obtains stop bracket gasoline after through high-pressure separator, stabilizer tower.The isolated hydrogen rich stream of high-pressure separator mixes by recycle compressor with new hydrogen delivers to hydrofining reactor.
Described gasoline stocks is to be selected from this group of being made of catalytically cracked gasoline, catalytic cracking gasoline, straight-run spirit, coker gasoline, pyrolysis gasoline, pressure gasoline one or more mixture among material.
The unifining process catalyst system therefor can be VIB or the VIII family non-precious metal catalyst that loads on unformed aluminum oxide or the silica-alumina supports, and the group vib metal is Mo and W normally, and VIII family metal is Ni and Co normally, is typically Ni-W, Co-Mo or Ni-Mo.
Octane value recovering process catalyst system therefor must have enough acid functions so that the octane value that cracking reaction recovers the loss of hydrofining stage to take place, stability and the required dual-function catalyst requirement of isomerization reaction that equally can loaded metal further improves catalyzer on molecular sieve be as supported V IB on molecular sieve carrier or VIII family base metal or precious metal.Can be VIB or VIII family base metal or the noble metal catalyst that loads on the molecular sieve carrier, preferred catalyzer be to constitute (is benchmark in oxide compound and with the total catalyst weight) by the VIII family metal of 0.5～10 weight %, the molecular sieve of 10～75 weight % and the aluminum oxide of surplus.Described molecular sieve is ZSM-5 zeolite and/or β zeolite.
Below in conjunction with accompanying drawing method provided by the present invention is further detailed.
Accompanying drawing is the method for modifying synoptic diagram of gasoline fraction provided by the invention.
The method for modifying flow process of gasoline fraction provided by the invention is described in detail as follows:
FCC gasoline is successively through pipeline 1, pump 2, pipeline 3, after hydrogen rich stream from pipeline 28 mixes, after pipeline 4 enters interchanger 5 and the reaction effluent heat exchange from pipeline 16, enter fixed bed hydrogenation refining reaction device 7 through pipeline 6, contact with Hydrobon catalyst, remove the sulphur in the raw material, stripping tower 9 in the middle of entering after impurity such as nitrogen and hydrogenation of olefins are saturated, under fresh hydrogen stripping effect, remove the influential hydrogen sulfide of catalyst activity from pipeline 10, ammonia, gaseous stream is mainly hydrogen, contain partial vulcanization hydrogen simultaneously, ammonia and lighter hydrocarbons, this gaseous stream is drawn from stripping tower 9 tops through pipeline 11; Liquid phase stream then mixes with hydrogen rich stream from pipeline 29 through pipeline 12, process furnace 13, pipeline 14 successively, enters octane value recovering section reactor 15 through pipeline 30 again, contacts with octane value recovering catalyst and carries out the octane value recovering reaction.The reaction effluent of reactor 15 enters interchanger 4 through pipeline 16, after raw material heat exchange from pipeline 4, enter high-pressure separator 18 through pipeline 17, in high-pressure separator, be divided into gas, liquid two-phase, wherein gas phase is a hydrogen rich stream, wherein be mainly hydrogen, comprise a small amount of hydrogen sulfide, ammonia and lighter hydrocarbons simultaneously.This gas phase is drawn from high-pressure separator 18 tops through pipeline 23, after gaseous stream from pipeline 11 mixes, behind pipeline 24, recycle compressor 25, pipeline 26, enter hydrogen recovery and desulfurizer 27 successively, hydrogen-rich gas after the purification is divided into two portions, wherein a part loops back reactor 15 through pipeline 29,30 successively, and another part then loops back reactor 7 through pipeline 28, pipeline 4, interchanger 5, pipeline 6 successively.The liquid phase stream of high-pressure separator 18 bottoms enters follow-up stable system 20 through pipeline 19, and lighter hydrocarbons and gasoline products are respectively through pipeline 21,22 caterpillars.
Method provided by the invention can be reduced to sulfur in gasoline content below the 30ppm, and olefin(e) centent is reduced to below the 10v%, and octane value does not lose substantially, satisfies III class gasoline standard in world's fuel oil standard.
The following examples will give further instruction to method provided by the invention, but therefore not limit the present invention.
Used raw material is a FCC gasoline among the embodiment, its character is as shown in table 1, the used Hydrobon catalyst and the trade names of octane value recovering catalyst are respectively CH-18 and RIDOS-1, and these two kinds of catalyzer are produced by Sinopec Group's Chang Ling oil-refining chemical head factory catalyst plant.
Comparative Examples
FCC gasoline A only contacts with Hydrobon catalyst CH-18 with hydrogen, at hydrogen dividing potential drop 3.2MPa, 290 ℃ of temperature, liquid hourly space velocity 1.1h
-1, hydrogen-oil ratio 400v/v condition under react, reaction effluent no longer contacts with hydrogen, octane value recovering catalyst RIDOS-1, the separating reaction effluent obtains gasoline products, the hydrogen-rich gas of recovery recycles.Operational condition and gasoline products character are as shown in table 2, and as can be seen from Table 2, though sulphur content only is 18.4ppm in the gasoline products, olefin(e) centent is 17.5v%, and anti-knock index loses up to 12 units.
Embodiment 1
FCC gasoline A contacts with Hydrobon catalyst CH-18 earlier with hydrogen, at hydrogen dividing potential drop 3.2MPa, 290 ℃ of temperature, liquid hourly space velocity 4.0h
-1, hydrogen-oil ratio 400v/v condition under react, reaction effluent contacts with octane value recovering catalyst RIDOS-1, at hydrogen dividing potential drop 3.2MPa, 350 ℃ of temperature, liquid hourly space velocity 1.5h after mixing without middle stripping and hydrogen again
-1, hydrogen-oil ratio 400v/v condition under react, the separating reaction effluent obtains gasoline products, the hydrogen-rich gas of recovery recycles.Operational condition and gasoline products character are as shown in table 2, and as can be seen from Table 2, sulphur content only is 21.5ppm in the gasoline products, and desulfurization degree is up to 97.0%, and olefin(e) centent drops to 1.6v% from 36.9v%, and the anti-knock index loss is 1.6 units only.
Embodiment 2
FCC gasoline A contacts with Hydrobon catalyst CH-18 earlier with hydrogen, at hydrogen dividing potential drop 3.2MPa, 290 ℃ of temperature, liquid hourly space velocity 4.0h
-1, hydrogen-oil ratio 400v/v condition under react, reaction effluent behind middle stripping and hydrogen mix, contact with octane value recovering catalyst RIDOS-1 again, at hydrogen dividing potential drop 3.2MPa, 350 ℃ of temperature, liquid hourly space velocity 1.5h
-1, hydrogen-oil ratio 300v/v condition under react, the separating reaction effluent obtains gasoline products, the hydrogen-rich gas of recovery recycles.Operational condition and gasoline products character are as shown in table 2, and as can be seen from Table 2, sulphur content only is 12.6ppm in the gasoline products, and desulfurization degree is up to 98.2%, and olefin(e) centent drops to 0.01v% from 36.9v%, and the anti-knock index loss is 0.3 unit only.
Embodiment 3
FCC gasoline B contacts with Hydrobon catalyst CH-18 earlier with hydrogen, at hydrogen dividing potential drop 3.2MPa, 280 ℃ of temperature, liquid hourly space velocity 5.0h
-1, hydrogen-oil ratio 450v/v condition under react, reaction effluent behind middle stripping and hydrogen mix, contact with octane value recovering catalyst RIDOS-1 again, at hydrogen dividing potential drop 3.2MPa, 370 ℃ of temperature, liquid hourly space velocity 1.5h
-1, hydrogen-oil ratio 300v/v condition under react, the separating reaction effluent obtains gasoline products, the hydrogen-rich gas of recovery recycles.Operational condition and gasoline products character are as shown in table 3, and as can be seen from Table 3, sulphur content only is 16.3ppm in the gasoline products, and desulfurization degree is up to 97.4%, and olefin(e) centent drops to 0.2v% from 46.4v%, and the anti-knock index loss is 0.5 unit only.
Embodiment 4
FCC gasoline C contacts with Hydrobon catalyst CH-18 earlier with hydrogen, at hydrogen dividing potential drop 3.2MPa, 290 ℃ of temperature, liquid hourly space velocity 7.0h
-1, hydrogen-oil ratio 500v/v condition under react, reaction effluent behind middle stripping and hydrogen mix, contact with octane value recovering catalyst RIDOS-1 again, at hydrogen dividing potential drop 3.2MPa, 350 ℃ of temperature, liquid hourly space velocity 1.5h
-1, hydrogen-oil ratio 300v/v condition under react, the separating reaction effluent obtains gasoline products, the hydrogen-rich gas of recovery recycles.Operational condition and gasoline products character are as shown in table 3, and as can be seen from Table 3, sulphur content only is 6ppm in the gasoline products, and desulfurization degree is up to 93.0%, and olefin(e) centent drops to 0.1v% from 49.3v%, and the anti-knock index loss is 0.1 unit only.
The character of table 1, gasoline stocks
| FCC gasoline stocks numbering | ????A | ????B | ????C |
| Density (20 ℃), g/cm 3 | ????0.7120 | ????0.7242 | ????0.7112 |
| Sulphur content, ppm | ????709 | ????628 | ????86 |
| Olefin(e) centent, v% | ????36.9 | ????46.4 | ????49.3 |
| Boiling range, ℃ | |||
| Initial boiling point | ????28 | ????42 | ????30 |
| 10％ | ????40 | ????51 | ????48 |
| 50％ | ????81 | ????101 | ????87 |
| 95％ | ????146 | ????182 | ????162 |
| Final boiling point | ????160 | ????194 | ????181 |
| Anti-knock index | ????81.5 | ????84 | ????85 |
Table 2
| Comparative Examples | Embodiment 1 | Embodiment 2 | |
| Operational condition | |||
| The hydrogen dividing potential drop, MPa | |||
| Hydrofining | ????3.2 | ????3.2 | ????3.2 |
| Octane value recovering | ????- | ????3.2 | ????3.2 |
| Temperature, ℃ | |||
| Hydrofining | ????290 | ????290 | ????290 |
| Octane value recovering | ????- | ????350 | ????350 |
| Liquid hourly space velocity, h -1 | |||
| Hydrofining | ????1.1 | ????4.0 | ????4.0 |
| Octane value recovering | ????- | ????1.5 | ????1.5 |
| Hydrogen-oil ratio, Nm 3/m 3 | |||
| Hydrofining | ????400 | ????400 | ????400 |
| Octane value recovering | ????- | ????400 | ????300 |
| Product property | |||
| Density (20 ℃), g/cm 3 | ????0.7120 | ????0.7124 | ????0.7123 |
| Sulphur content, ppm | ????18.4 | ????21.5 | ????12.6 |
| Olefin(e) centent, v% | ????17.5 | ????0.5 | ????0.01 |
| Anti-knock index | ????69.5 | ????79.9 | ????81.2 |
| The anti-knock index loss | ????12 | ????1.6 | ????0.3 |
| Desulfurization degree, % | ????97.4 | ????97.0 | ????98.2 |
Table 3
| Embodiment 3 | Embodiment 4 | |
| FCC gasoline stocks numbering | ????B | ????C |
| Operational condition | ||
| The hydrogen dividing potential drop, MPa | ||
| Hydrofining | ????3.2 | ????3.2 |
| Octane value recovering | ????3.2 | ????3.2 |
| Temperature, ℃ | ||
| Hydrofining | ????280 | ????290 |
| Octane value recovering | ????370 | ????350 |
| Liquid hourly space velocity, h -1 | ||
| Hydrofining | ????5.0 | ????7.0 |
| Octane value recovering | ????1.5 | ????1.5 |
| Hydrogen-oil ratio, Nm 3/m 3 | ||
| Hydrofining | ????450 | ????500 |
| Octane value recovering | ????300 | ????300 |
| Product property | ||
| Density (20 ℃), g/cm 3 | ????0.7235 | ????0.7123 |
| Sulphur content, ppm | ????16.3 | ????12.6 |
| Olefin(e) centent, v% | ????0.2 | ????0.01 |
| Anti-knock index | ????83.5 | ????84.7 |
| The anti-knock index loss | ????0.5 | ????0.3 |
| Desulfurization degree, % | ????97.4 | ????98.2 |
Claims (6)
1, a kind of method for modifying of gasoline fraction is characterized in that this method comprises that gasoline stocks contacts with Hydrobon catalyst earlier with hydrogen, at hydrogen dividing potential drop 0.5～6.0MPa, 200～420 ℃ of temperature, liquid hourly space velocity 0.5～10.0h
-1, hydrogen-oil ratio 50～1500v/v condition under react, the hydrofining reaction effluent contacts with octane value recovering catalyst with hydrogen again, at hydrogen dividing potential drop 0.5～6.0MPa, 200～460 ℃ of temperature, liquid hourly space velocity 0.5～10.0h
-1, hydrogen-oil ratio 50～1500v/v condition under react, the separating reaction effluent obtains gasoline products, the hydrogen-rich gas of recovery recycles.
2,, it is characterized in that described gasoline stocks is to be selected from this group of being made of catalytically cracked gasoline, catalytic cracking gasoline, straight-run spirit, coker gasoline, pyrolysis gasoline, pressure gasoline one or more mixture among material according to the method for claim 1.
3, according to the method for claim 1, it is characterized in that described hydrofining reaction effluent behind middle stripping, being mixed with hydrogen contacts with octane value recovering catalyst again.
4,, it is characterized in that described Hydrobon catalyst is VIB or the VIII family non-precious metal catalyst that loads on unformed aluminum oxide or the silica-alumina supports according to the method for claim 1.
5,, it is characterized in that described octane value recovering catalyst is VIB or VIII family base metal or the noble metal catalyst that loads on the molecular sieve carrier according to the method for claim 1.
6,, it is characterized in that described octane value recovering catalyst is to be made of the VIII family metal of 0.5～10 weight %, the molecular sieve of 10～75 weight % and the aluminum oxide of surplus according to the method for claim 1 or 5.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| 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 |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| 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 |
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