CN101294108A - Combination method of catalytic cracking production separation and hydrogen refining - Google Patents
Combination method of catalytic cracking production separation and hydrogen refining Download PDFInfo
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- CN101294108A CN101294108A CNA2007100988459A CN200710098845A CN101294108A CN 101294108 A CN101294108 A CN 101294108A CN A2007100988459 A CNA2007100988459 A CN A2007100988459A CN 200710098845 A CN200710098845 A CN 200710098845A CN 101294108 A CN101294108 A CN 101294108A
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Abstract
A combined method for separating and hydro-refining catalytic cracking product comprises the following steps: (1) introducing oil gas escaping from a settler of a catalytic cracking reaction system into a main fractionating tower, sequentially separating slurry oil, cycle oil, heavy diesel oil, diesel oil and overhead oil gas from bottom to top of the main fractionating tower, and feeding the overhead oil gas to an oil gas separation system to separate a fraction less than C4, light gasoline fraction and heavy gasoline fraction; (2) introducing the separated fraction less than C4 and the light gasoline fraction into an absorbing, stabilizing and refining system of the catalytic cracking device to obtain the product of the fraction less than C4 and the light gasoline product; and (3) introducing the separated heavy gasoline fraction into a hydrogenation reaction, contacting with a hydro-refining catalyst, and feeding hydrogen to carry out hydro-refining reaction to obtain heavy gasoline product. The method provided by the invention can produce clean gasoline and improve the absorption effect, and has the advantages of lowered energy consumption, simple and flexible flow, less investment and easy implementation.
Description
Technical field
The present invention relates to treating process under the situation that there is not hydrogen in a hydroprocessing technique process and at least one and handle the method for hydrocarbon ils, more particularly, relate to a kind of separation and process for purification of catalytic cracking production.
Background technology
Along with the increasingly stringent of environmental regulation, countries in the world have all proposed more and more harsher restriction index to sulphur content, the olefin(e) centent of motor spirit.At present, China's motor spirit accounts for 80% of gasoline product amount based on catalytic cracking (FCC) gasoline.FCC content of sulfur in gasoline, olefin(e) centent height, and along with the heaviness that FCC processes raw material, FCC sulfur in gasoline content and olefin(e) centent will further increase.Therefore, reduce the main path that FCC sulfur in gasoline content and olefin(e) centent are sulphur and olefin(e) centent in the control motor spirit.
At present, reduce sulfur content of catalytic cracking gasoline following several treatment process is generally arranged both at home and abroad: 1) improve catalytic cracking process and catalyzer; 2) hydrotreating of FCC feedstock; 3) catalytically cracked gasoline being carried out the back desulfurization handles.
Aspect catalytic cracking process, mainly the partial vulcanization thing in the gasoline is converted into H by strengthening hydrogen transfer reactions and cracking reaction
2S is to reduce the sulphur content in the gasoline.Because the sulfide major part in the catalytic gasoline is a thiophene-type sulfide, general thiophene and thiophenes are lower at the transformation efficiency of catalytic-cracking reaction system, are difficult to the quality of gasoline requirement that reaches strict.Sulfur content of catalytic cracking gasoline can be reduced about 15% as CN1279270A.Aspect catalytic cracking catalyst and auxiliary agent, also do a lot of work both at home and abroad, but sulfur content of catalytic cracking gasoline can only be reduced by 10～30% usually.
Hydrotreating of FCC feedstock is to solve one of valid approach of sulfur content of catalytic cracking gasoline, can improve the catalytic cracking product on the one hand to distribute, and reduces the catalytic gasoline sulphur content; Can reduce NO in the catalytic cracking flue gas on the other hand
XAnd SO
XQuantity discharged.The pre-treatment of catalytically cracked material hydrogenation is comparative maturity technically, and its shortcoming is to invest greatlyyer, and consumption hydrogen is higher, and is short to heavy and inferior raw material catalyzer life cycle.
Research and method that desulfurization behind the catalytically cracked gasoline is handled are maximum, comprise non-hydrotreatment and hydroprocessing process.Non-hydrogenation method has adsorption desulfurize, biocatalytic desulfurization and water vapour catalytic desulfurization.
CN1465666A has proposed a kind of method of deep desulfurization olefin hydrocarbon reduction of gasoline, with gasoline fraction be cut into gently, last running, lighting end is through the soda finishing mercaptan removal, last running is through hydrofining, and then light, last running after will making with extra care mix and obtains gasoline products.
US 6103105 discloses a kind of method that reduces content of sulfur in gasoline, it is characterized in that with catalytically cracked gasoline be divided into gently, in, weigh three kinds of cuts, wherein in, last running goes hydrogenating desulfurization.
CN1542085A discloses a kind of separation method of catalytically cracked gasoline.Its content is to set up gasoline fractionation part in conventional catalytic cracking system device.The stable gasoline that goes out stabilizer tower in the old process enters the gasoline fractionation and partly isolates petroleum naphtha and heavy petrol product.For gasoline deep processing is fallen alkene and sulfur removal technology, etherification technology are supplied raw materials.
CN1458227A discloses a kind of method that reduces catalytic cracking gasoline olefine content, set up the B-grade condensation cooling system on the original conventional condensation cooling system of catalytic cracking fractionating tower cat head, the lighting end (＜80～110 ℃ of cuts) that is used to isolate raw gasline is carried out in order to reduce the catalytic reforming reaction of gasoline olefin again.The olefin(e) centent that returns the petroleum naphtha of upgrading riser tube is exactly the olefin(e) centent of main riser catalytic cracking petroleum naphtha, needed processing condition comparatively relax, need the corresponding reduction of amount of gasoline of upgrading, the olefin(e) centent of catalytically cracked gasoline can reduce greatly, octane value does not reduce, and satisfies relevant environmental requirement.
Above several method is cuts apart gasoline, handles respectively by the distribution in the different flow process scopes in gasoline of alkene, sulphur, reaches the purpose of producing clean gasoline.But, all be that the stable gasoline that absorbs after stablizing with catalytic cracking is the cutting raw material, it is poor to absorb the stabilization process assimilation effect, and the absorption agent consumption is big, absorbing-stabilizing system energy consumption height.
Summary of the invention
The purpose of this invention is to provide a kind of catalytic cracking production and separate and hydrorefined combined method, with the sulphur content in the lower energy consumption reduction gasoline.
A kind of catalytic cracking production separates and hydrorefined combined method, may further comprise the steps:
(1) oil gas of the catalytic-cracking reaction system settling vessel being selected is introduced main fractionating tower, isolate slurry oil, recycle stock, heavy gas oil, diesel oil and cat head oil gas from the bottom up successively through main fractionating tower, the overhead oil pneumatic transmission to the gasoline separation system, is isolated the following cut of C4, light gasoline fraction and heavy naphtha;
(2) following cut of isolated C4 and light gasoline fraction are introduced former catalytic cracking unit and are absorbed stable, refining system and obtain following cut product of C4 and petroleum naphtha product;
(3) isolated heavy naphtha is introduced hydrogenator, contacts with Hydrobon catalyst with hydrogen to carry out hydrofining reaction, obtains the heavy petrol product after the reaction.
In the method provided by the invention, petroleum naphtha product and the blending of heavy petrol product with obtaining obtain the clean gasoline product.
In the method provided by the invention, described gasoline separation system is fractional condensation cooling system or raw gasline separation column, when being the fractional condensation cooling system, through first step condensation refrigerated separation, is under 100～150 ℃ the condition cat head oil gas to be separated into the following cut of heavy naphtha and petroleum naphtha and C4 with described main fractionating tower cat head oil gas at cut point; The following cut of petroleum naphtha and C4 is following cut of C4 and light gasoline fraction through second stage condensation refrigerated separation, separates back following cut of C4 and light gasoline fraction and enters stable, the refining system of catalytic cracking absorption respectively.Wherein preferred scheme is at first to introduce heavy petrol through the isolated heavy naphtha of first step condensation cooling system and carry and heat up in a steamer tower light constituent is wherein told described, and then introduces hydrofining reactor and carry out hydrofining reaction.
When described gasoline separation system is the raw gasline separation column, described main fractionating tower cat head oil gas is introduced the raw gasline separation column, be under 100～150 ℃ the condition cat head oil gas to be separated into the following cut of heavy naphtha and petroleum naphtha and C4 at cut point.The following cut of petroleum naphtha and C4 enters former catalytic cracking condensation cooling system and isolates following cut of C4 and light gasoline fraction, separates back following cut of C4 and light gasoline fraction and enters stable, the refining system of catalytic cracking absorption respectively.
The thermal source of the bottom reboiler of described raw gasline separation column is steam or main fractionating tower stage casing heat-obtaining, preferably in the mode of main fractionating tower stage casing heat-obtaining.The typical operational condition of gasoline splitter is: 35～45 ℃ of overhead condensation temperature, and tower top pressure 0.1～0.3MPa, 130～180 ℃ of column bottom temperatures, full tower pressure drop 0.01～0.02MPa, reflux ratio is 1～3.
In the method provided by the invention, hydrorefined reaction conditions is in the described step (3): temperature of reaction is 200～400 ℃, and the hydrogen dividing potential drop is 1.0～4.0MPa, and volume space velocity is 3.0～5.0h during liquid
-1, hydrogen to oil volume ratio is 200～600Nm
3/ m
3
In the method provided by the invention, the Hydrobon catalyst described in the step (3) be on unformed aluminum oxide or silica-alumina supports load the catalyzer of VIB or VIII family metal.
The advantage of method provided by the invention is:
Method provided by the invention, raw gasline is separated into light gasoline fraction and heavy naphtha, light gasoline fraction goes absorbing-stabilizing system to make absorption agent, absorbing-stabilizing system is not advanced in heavy constituent in the raw gasline, maximally utilise that the most effective composition absorbs in the gasoline, reduce absorption tower, desorption tower and stabilizer tower liquid phase load, reach the effect that cuts down the consumption of energy; Isolated heavy naphtha carries out hydrogenating desulfurization, and then mixes with lighting end, and it is saturated to have reduced gasoline olefin, has reduced loss of octane number.
In a word, adopt method provided by the invention, can produce clean gasoline and can improve assimilation effect again, reduce energy consumption, the flow process simple and flexible invest for a short time, is easy to realization.
Description of drawings
Fig. 1 is the schematic flow sheet that method gasoline provided by the invention adopts fractional condensation cooling system scheme.
Fig. 2 is that method gasoline provided by the invention adopts raw gasline distillation tower scheme schematic flow sheet.
Embodiment
Below in conjunction with accompanying drawing method provided by the present invention is further detailed.But it is not thereby limiting the invention.
Fig. 1 is the schematic flow sheet that method gasoline provided by the invention adopts fractional condensation cooling system scheme.Reaction oil gas from the catalyst cracker outlet is introduced main fractionating tower 2 through pipeline 1, isolate slurry oil, recycle stock, heavy gas oil, diesel oil from the bottom up successively (for simplifying flow process through main fractionating tower, do not draw among the figure), the oil gas of drawing from the main fractionating tower top enters knockout drum 5 after pipeline 3 introducing overhead condensation water coolers 4 are cooled to 60～100 ℃.Knockout drum 5 isolated liquid phase streams are heavy naphtha, deliver to heavy petrol through pipeline 6 and carry heating up in a steamer in the tower 7 further light gasoline fraction is wherein separated.Heavy petrol is provided with reboiler 8 at the bottom of carrying and heating up in a steamer tower 7 towers.Heavy petrol carry heat up in a steamer discharging pressurization at the bottom of tower 7 towers after behind the hydrogen that pipeline 9 and pipeline 19 are introduced, compression that pipeline 16 is introduced hydrogen-rich gas mix, after pipeline 10 introducing hydrofining reactors 11 contact, react with Hydrobon catalyst, remove sulfocompound through heating.Hydrotreated product is sent into high-pressure gas-liquid separating tank 13 through pipeline 12.The liquid phase discharging that the high-pressure gas-liquid separating tank is separated is sent to stabilizer tower 15 through pipeline 14, and separating the cat head discharging that obtains is that light ends fractionation is drawn through pipeline 17, and discharging is that heavy naphtha is drawn through pipeline 18 at the bottom of the tower.Main fractionating tower 2 cat head knockout drums 5 isolated gases are after pipeline 20 and heavy petrol are proposed the cat head discharging of heating up in a steamer tower 7 and mixed, enter together and enter knockout drum 22 after light gasoline fraction condensate cooler 21 further is cooled to 35～40 ℃ and separate, the following gas of isolated C4 through pipeline 23, that isolated light gasoline fraction enters absorption-stabilization system by catalytic cracking 25 through pipeline 24 is further refining.Mix by a certain percentage from the petroleum naphtha of absorbing-stabilizing system 25 and heavy petrol and can obtain the clean gasoline product from hydrogenated gasoline stabilizer tower 15.
Fig. 2 is that method gasoline provided by the invention adopts raw gasline distillation tower scheme schematic flow sheet.Reaction oil gas from the catalyst cracker outlet is introduced main fractionating tower 2 through pipeline 1 at the bottom of separation column, main fractionating tower ejects material after pipeline 3, overhead condensation water cooler 4 are cooled to about 40 ℃, enters knockout drum 5.Knockout drum 5 isolated liquid phases are through pipeline 6, and after heat exchange, enter gasoline splitter 26 with raw gasline cut into gently, heavy naphtha fraction.From the cat head discharging, heavy naphtha is through pipeline 28 discharging at the bottom of the tower through pipeline 27 for light gasoline fraction.The parameter regulation such as stage number of load, trim the top of column amount, tower bottom reboiler load and gasoline splitter 26 that can be by adjusting overhead condenser are light, the cut point and the separation accuracy of heavy petrol.The heavy petrol that comes out from gasoline splitter 26 goes hydrofining through pipeline 28.Mix after pipeline 23 enters absorbing-stabilizing system with gas stream through pipeline 30 from the gas stream of knockout drum 5 from gasoline splitter return tank of top of the tower 29; It is further refining to enter absorbing-stabilizing system 25 from the part petroleum naphtha of gasoline splitter return tank of top of the tower 29 through pipeline 24.Follow-up hydrogenation, separation, mixture length are with identical shown in the accompanying drawing 1.
The following examples and Comparative Examples will give further instruction to present method, but therefore not limit the present invention.
According to the method provided by the invention shown in the accompanying drawing 1, utilize Aspen plus software that flow process is stablized in catalytic cracking fractionation absorption and carry out analog calculation, main operational condition: the oil and gas content that enters main fractionating tower is 309215kg/h, main fractionating tower cat head interchanger 4 outlet oil gas temperature are 70 ℃, the outlet oil gas temperature of rich gas interchanger 21 is 40 ℃, and petroleum naphtha 95% recovered temperature point is 165 ℃.Calculation result sees Table 1.
According to the method provided by the invention shown in the accompanying drawing 2, utilize Aspen plus software that flow process is stablized in catalytic cracking fractionation absorption and carry out analog calculation, main operational condition: the oil and gas content that enters main fractionating tower is 309215kg/h, gasoline splitter overhead condensation temperature is 40 ℃, tower still temperature is 180 ℃, reflux ratio is 1.2, and petroleum naphtha 95% recovered temperature is 150 ℃.Calculation result sees Table 1.
Comparative Examples
Utilize Aspen plus software that flow process is stablized in certain catalytic cracking unit fractionation absorption and carry out analog calculation, main operational condition: the oil and gas content that enters main fractionating tower is 309215kg/h, it is 40 ℃ that chiller temperature is coagulated in overhead oil air cooling, the raw gasline that cooling obtains all enters follow-up absorbing-stabilizing system, and absorption agent is that raw gasline adds stable gasoline.Calculation result sees Table 1.
Catalytic cracking unit produced raw gasline A is cut into gently, heavy naphtha, cut point is 96 ℃, heavy naphtha is carried out hydrofining, the RSDS-1 catalyzer that Hydrobon catalyst adopts Sinopec Group's Chang Ling oil-refining chemical head factory catalyst plant to produce.Light gasoline fraction is mixed into light, last running refining back gasoline products then through caustic wash desulfuration alcohol.Raw material A heavy naphtha character sees Table 2, and hydrogenation conditions and reaction result see Table 3, and the character of raw material A and mixing back gasoline products sees Table 4.
Embodiment 4
The MIP catalytic cracking unit is produced light, the heavy naphtha of raw gasline B cutting, cut point is 100 ℃, heavy naphtha is carried out hydrofining, the RSDS-1 catalyzer that Hydrobon catalyst adopts Sinopec Group's Chang Ling oil-refining chemical head factory catalyst plant to produce.Is (light gasoline fraction handled?) light, last running are mixed into make with extra care the back gasoline products then.Raw material B heavy naphtha character sees Table 2, and hydrogenation conditions and reaction result see Table 3, and the character of raw material A and mixing back gasoline products sees Table 4.
Table 1
| Project | | Embodiment | 1 | |
|
| Dry gas flow | kg/h | 16028 | 15744 | 16092 | |
| C in the dry gas 3 +Content | mol％ | 0.93 | 0.70 | 0.76 | |
| ?LPG | kg/h | 71046 | 71070 | 71990 | |
| Stable gasoline | kg/h | 82845 | 50901 | 59643 | |
| Replenish absorption agent | kg/h | 95621 | 115208 | 103207 | |
| The raw gasline amount | kg/h | 60212 | 21297 | 37655 | |
| The absorption agent total amount | kg/h | 155833 | 136505 | 140862 | |
| Heavy petrol | kg/h | - | 32359 | 22684 | |
| Stable gasoline+heavy petrol | kg/h | 82845 | 83260 | 82327 |
Annotate: Comparative Examples and embodiment are basic identical from diesel oil, the slurry oil product production of main fractionating tower.
From the embodiment 1,2 of table 1 and Comparative Examples as seen, adopt method provided by the invention, C3 in the dry gas
+Content reduces by 0.17～0.23 percentage point, and assimilation effect is better than conventional catalyst cracking method.Partly make absorption agent owing to adopt the gasoline lighting end, absorption dose reduces, make that replenishing the absorption agent consumption increases, but total absorption agent consumption descends 9.6%～12.4%, explanation is when having improved assimilation effect, also make liquid phase load decline in absorption tower, desorption tower, the stabilizer tower, thereby reduced energy consumption.
Table 2
| Project | Raw gasline A last running | Raw gasline B last running |
| Density (20 ℃), g/cm 3 | 0.7865 | 0.7701 |
| Sulphur content, μ g/g | 1670 | 1450 |
| Olefin(e) centent, heavy % | 21.89 | 12.15 |
| Boiling range, ℃ | ||
| Initial boiling point | 93 | 92 |
| 5％ | 108 | 105 |
| 50％ | 136 | 132 |
| Final boiling point | 195 | 195 |
| RON | 89.2 | 90.5 |
| Anti-knock index | 84.5 | 85.6 |
Table 3
| | Embodiment | 3 | Embodiment 4 |
| The hydrogen dividing potential drop, MPa | 1.6 | 1.6 | |
| Temperature of reaction, ℃ | 290 | 285 | |
| Liquid hourly space velocity, h -1 | 4.0 | 4.0 | |
| Hydrogen-oil ratio, Nm 3/m 3 | 200 | 300 | |
| Heavy naphtha behind the hydrogenation | |||
| Density (20 ℃), g/cm 3 | 0.7815 | 0.7649 | |
| Sulphur, μ g/g | 55 | 48 | |
| Olefin(e) centent, heavy % | 13.6 | 9.8 | |
| Desulfurization degree, % | 96.7 | 96.7 | |
| RON | 87.3 | 89.0 | |
| Uprising index | 83.0 | 84.3 |
Table 4
| Project | Raw gasline A | |
Raw gasline B | Embodiment 4 blended products |
| Density (20 ℃), g/cm 3 | 0.7226 | 0.7185 | 0.7205 | 0.7180 |
| Sulphur content, μ g/g | 1025 | 135 | 925 | 95 |
| Olefin(e) centent, heavy % | 38.6 | 28.8 | 28.1 | 23.1 |
| RON | 91.2 | 90.3 | 91.8 | 91.0 |
| Anti-knock index | 86.7 | 85.9 | 87.0 | 86.5 |
By the embodiment 3,4 of table 4 as can be seen, adopt method provided by the invention, final gasoline products removal of sulfur compounds 86.8%～89.7%, reach 135 μ g/g and 95 μ g/g respectively, both can produce the motor spirit that meets state III standard (alkene 30%, sulphur 150ppm), even can produce and satisfy capital mark B standard (alkene 25%, sulphur 150ppm) motor spirit satisfies national up-to-date motor spirit emission standard.
Claims (7)
1, a kind of catalytic cracking production separates and hydrorefined combined method, it is characterized in that may further comprise the steps:
(1) oil gas of the catalytic-cracking reaction system settling vessel being selected is introduced main fractionating tower, isolate slurry oil, recycle stock, heavy gas oil, diesel oil and cat head oil gas from the bottom up successively through main fractionating tower, the overhead oil pneumatic transmission to the gasoline separation system, is isolated the following cut of C4, light gasoline fraction and heavy naphtha;
(2) isolated light gasoline fraction is introduced former catalytic cracking unit and is absorbed stable, refining system and obtain the petroleum naphtha product;
(3) isolated heavy naphtha is introduced hydrogenator, contacts with Hydrobon catalyst with hydrogen to carry out hydrofining reaction, obtains the heavy petrol product after the reaction.
2, according to the method for claim 1, it is characterized in that described gasoline separation system is the fractional condensation cooling system, through first step condensation refrigerated separation, is under 100～150 ℃ the condition cat head oil gas to be separated into the following cut of heavy naphtha and petroleum naphtha and C4 with described main fractionating tower cat head oil gas at cut point; It is following cut of C4 and light gasoline fraction that the following cut of petroleum naphtha and C4 enters second stage condensation refrigerated separation, enters catalytic cracking after the separation respectively and absorbs stable, refining system.
3,, it is characterized in that the isolated heavy naphtha of described classified condensation cooling system at first introduces heavy petrol and carry and heat up in a steamer the light constituent that tower will be wherein and tell, and then introduce hydrofining reactor according to the method for claim 2.
4, according to the method for claim 1, it is characterized in that described gasoline separation system is the raw gasline separation column, described main fractionating tower cat head oil gas is introduced the raw gasline separation column, be under 100～150 ℃ the condition cat head oil gas to be separated into the following cut of heavy naphtha and petroleum naphtha and C4 at cut point, the following cut of petroleum naphtha and C4 enters former catalytic cracking condensation cooling, absorbs stable, refining system.
5, according to the method for claim 4, the thermal source that it is characterized in that the bottom reboiler of described raw gasline separation column is a main fractionating tower stage casing heat-obtaining.
6, according to claim 1,2,3 or 4 method, it is characterized in that hydrorefined reaction conditions is in the described step (3): temperature of reaction is 200～400 ℃, and the hydrogen dividing potential drop is 1.0～4.0MPa, and volume space velocity is 3.0～5.0h during liquid
-1, hydrogen-oil ratio is 200～600Nm
3/ m
3
7, according to claim 1,2,3 or 4 method, it is characterized in that the Hydrobon catalyst described in the step (3) be on unformed aluminum oxide or silica-alumina supports load the catalyzer of VIB or VIII family metal.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101942331A (en) * | 2009-07-09 | 2011-01-12 | 中国石油化工股份有限公司抚顺石油化工研究院 | Gasoline and diesel oil combined hydrogenation method |
| CN103059946A (en) * | 2011-10-21 | 2013-04-24 | 中国石油化工股份有限公司 | Low-energy consumption catalytic gasoline hydrodesulfurization method |
| CN102051221B (en) * | 2009-10-30 | 2013-12-25 | 中国石油化工股份有限公司 | Method for more producing light oil by using hydrocarbon oil |
| CN103571534A (en) * | 2013-09-17 | 2014-02-12 | 中国石油大学(华东) | Device and method for producing clean gasoline by combining catalytic cracking and hydrofining |
| CN103571536A (en) * | 2013-09-17 | 2014-02-12 | 中国石油大学(华东) | Device and method for producing clean gasoline and increasing propylene yield through catalytic cracking and hydrogenation |
| CN109777515A (en) * | 2017-11-14 | 2019-05-21 | 中国石油化工股份有限公司 | A kind of method of heavy-oil hydrogenation high-knock rating gasoline |
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| CN100532507C (en) * | 2005-06-24 | 2009-08-26 | 中国石油大学(北京) | Catalytic cracking gasoline modifying method |
| FR2889539B1 (en) * | 2005-08-08 | 2011-05-13 | Inst Francais Du Petrole | PROCESS FOR THE DESULFURATION OF SPECIES COMPRISING ADSORPTION DESULFURATION OF LIGHT FRACTION AND HYDRODESULFURATION OF HEAVY FRACTION |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101942331A (en) * | 2009-07-09 | 2011-01-12 | 中国石油化工股份有限公司抚顺石油化工研究院 | Gasoline and diesel oil combined hydrogenation method |
| CN101942331B (en) * | 2009-07-09 | 2013-06-19 | 中国石油化工股份有限公司 | Gasoline and diesel oil combined hydrogenation method |
| CN102051221B (en) * | 2009-10-30 | 2013-12-25 | 中国石油化工股份有限公司 | Method for more producing light oil by using hydrocarbon oil |
| CN103059946A (en) * | 2011-10-21 | 2013-04-24 | 中国石油化工股份有限公司 | Low-energy consumption catalytic gasoline hydrodesulfurization method |
| CN103571534A (en) * | 2013-09-17 | 2014-02-12 | 中国石油大学(华东) | Device and method for producing clean gasoline by combining catalytic cracking and hydrofining |
| CN103571536A (en) * | 2013-09-17 | 2014-02-12 | 中国石油大学(华东) | Device and method for producing clean gasoline and increasing propylene yield through catalytic cracking and hydrogenation |
| CN103571536B (en) * | 2013-09-17 | 2014-07-30 | 中国石油大学(华东) | Device and method for producing clean gasoline and increasing propylene yield through catalytic cracking and hydrogenation |
| CN103571534B (en) * | 2013-09-17 | 2014-07-30 | 中国石油大学(华东) | Device and method for producing clean gasoline by combining catalytic cracking and hydrofining |
| CN109777515A (en) * | 2017-11-14 | 2019-05-21 | 中国石油化工股份有限公司 | A kind of method of heavy-oil hydrogenation high-knock rating gasoline |
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