CN101368111B - Hydrogenation modification method for catalytically cracked gasoline - Google Patents
Hydrogenation modification method for catalytically cracked gasoline Download PDFInfo
- Publication number
- CN101368111B CN101368111B CN 200710120343 CN200710120343A CN101368111B CN 101368111 B CN101368111 B CN 101368111B CN 200710120343 CN200710120343 CN 200710120343 CN 200710120343 A CN200710120343 A CN 200710120343A CN 101368111 B CN101368111 B CN 101368111B
- Authority
- CN
- China
- Prior art keywords
- gasoline
- hydrogen
- fraction
- reaction
- octane value
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to a hydro-upgrading method for catalytic cracking gasoline; the method comprises the following steps: gasoline whole fraction is cut into light fraction and heavy fraction; the cutting point is 60 DEG C to 80 DEG C; mercaptan in the light gasoline fraction is removed through mercaptan removal alkali washing; the heavy gasoline fraction and hydrogen gas have catalytic hydrodesulfurization, denitrogenation and olefin saturated reaction; reactor effluent or the reactor effluent after removing hydrogen sulfide is contacted with octane value restore catalyzer, and isomerization, aromatizatian and building up reaction are implemented, hydrogenated oil is separated and lighter hydrocarbon gasoline fraction is obtained, hydrogen-rich gas at the top of a high partial tank is circularly used through hydrogen sulfide removal, and lighter hydrocarbon at the top of a stabilizer tower is feedback to a fractionation tank to be fractionated again; the condition of the hydrotreating reaction is that hydrogen partial pressure is 1.5 to 3.0 MPa; the reaction temperature is 250 to 320 DEG C; the liquid hourly space velocity is 3.0 to 5.0 h<-1>, and the hydrogen-oil ratio is 200 to 500 Nm<3>/m<3>; the sulfur content of the gasoline product is smaller than 100 ppm, the octane value is unchanged, and the yield of gasoline reaches 98.5 weight percent.
Description
Technical field
The present invention relates in a kind of situation of hydrogen existence the hydrogenation modification method of high-sulfur, high olefin, high-octane FCC gasoline.
Background technology
China's content of sulfur in gasoline and olefin(e) centent are high.The reason of sulfur in gasoline and olefin(e) centent superelevation is that mainly the ratio that catalytic cracking (FCC) gasoline accounts in the gasoline pool is too high, realize that content of olefin in gasoline is lower than 20% standard very difficult.In order to satisfy the clean gasoline specification requirement, olefin(e) centent needs to reduce significantly, and alkene is the important component in FCC gasoline octane rating source, and the decrease of olefin(e) centent will cause the obvious decline of FCC gasoline octane rating.Adopt conventional hydrofining technology that catalytically cracked gasoline is carried out upgrading, the loss of octane number of gasoline can reach tens units.
The disclosed gasoline modifying method of US5411658 is, adopt first traditional Hydrobon catalyst with the FCC gasoline hydrofinishing after, then adopt beta-zeolite catalyst that the effluent of hydrofining reaction is carried out octane value recovering.But the method uses the raw material final boiling point higher, and the too high aromatic saturation that makes of hydrofining section temperature of reaction is too much, causes research octane number (RON) (RON) loss more, is difficult to recover.
The disclosed gasoline of US5599439 and reformed oil method for modifying are, first paragraph carries out first hydrofining, remove impurity and the olefin saturateds such as sulphur, nitrogen, separate through middle again, the gas direct circulation that the process sub-argument goes out behind the impurity such as hydrogen sulfide, ammonia returns first paragraph, intermediates oil enters second segment, carries out the octane value recovering process in fluidized-bed reactor, and this section is no longer mended new hydrogen.The method has increased a separator between one, two section, increase facility investment, and working pressure is excessively low simultaneously, is unfavorable for the long-term operation of catalyzer.
The disclosed gasoline modifying method of US5399258 is that behind first paragraph process hydrogenation desulfurization and denitrogenation, the olefins hydrogenation, the intermediate product that obtains directly enters second segment and carries out the octane value recovering reaction.The temperature of reaction of first paragraph is higher, and is fair with the temperature of reaction of second segment.Because the temperature of reaction of first paragraph is too high, causes final product to produce a large amount of mercaptan sulfurs, temperature is higher, and the mercaptan sulfur of generation is more.
The disclosed a kind of inferior patrol hydrogenation modifying process of CN1621495A is that feed gasoline is cut into lighting end and last running at 60 ℃～90 ℃, last running mixes with hydrogen, again with the Hydrobon catalyst contact reacts, reaction effluent contacts with the aromatization modification catalyzer and carries out the aromatization modification reaction, but the content of sulfur in gasoline that uses the described catalyzer of the method to obtain drops to 150ppm.
The method of the disclosed deep desulfurization olefin hydrocarbon reduction of gasoline of CN1465666A be with gasoline stocks be cut into gently, last running, last running contacts with octane value recovering catalyst with Hydrobon catalyst successively, and light, last running after the desulfurization are mixed to get gasoline products.The content of sulfur in gasoline that the method is produced drops to 200ppm, and yield of gasoline is undesirable.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology a kind of and can keep the constant FCC gasoline hydrodesulfurizationmethod of octane value, fall olefins process.By stock oil being cut into light gasoline fraction and heavy naphtha, light gasoline fraction is carried out mercaptan removal to be processed, heavy naphtha contacts with octane value recovering catalyst with Hydrobon catalyst respectively, carry out the hydrofining desulfurization, fall alkene, hydroisomerizing, aromatization, cracking and superimposed polyfunctional reactant, light gasoline fraction behind reacted heavy naphtha and the mercaptan removal is in harmonious proportion, and product gasoline can reach following index:
(1) alkene in the product oil is reduced to 20%;
(2) sulphur is reduced to below the 100ppm;
(3) octane value recovering in addition be higher than the reaction before level;
(4) liquid is received in 98.5 (m) more than the %.
Process technology scheme provided by the invention comprises the following steps:
(1), the full fraction of gasoline is required the cutting fractionation according to the difference of purpose product, be divided into lighting end, heavy fraction; Wherein the cut point of light gasoline fraction and heavy naphtha is 60 ℃～80 ℃, and the cutting principle is for to cut last running with thiophene;
(2), the petroleum naphtha fraction removes wherein mercaptan through alkali cleaning refining desulfurization alcohol;
(3), at first the heavy petrol fraction contacts with Hydrobon catalyst with hydrogen one, carry out hydrogenating desulfurization, denitrogenation, olefin saturation, reaction effluent contacts with octane value recovering catalyst, carry out isomerization, aromizing and the reaction such as superimposed, separate hydrogenated oil and obtain lighter hydrocarbons and gasoline fraction, lighter hydrocarbons are returned head tank and are received to increase liquid, and hydrogen-rich gas removes hydrogen sulfide recirculation and uses through the depriving hydrogen sulphide tank;
(4), the heavy petrol fraction after the desulfurization with refining after light gasoline fraction be mixed to get gasoline products.
The reactor of the described heavy naphtha hydro-upgrading of above-mentioned steps (3) reaction member can be the fixed-bed reactor of two series connection, also can be the reactor of two independent fixed beds.This reaction member has the hydrofining desulfurization, falls alkene, hydroisomerizing, aromatization, cracking and superimposed polyfunctional reactant.
This Technology is respectively at loaded catalyst on the evaluating apparatus of 100ml and 1 liter scale and shows through the Activity and stabill evaluation effect, the present invention is guaranteeing that the product gasoline octane value does not lose, even under the prerequisite that increases to some extent, sulphur content in the product oil is reduced to 100ppm, olefin(e) centent satisfies world's fuel oil standard gasoline standard II class index and Europe III requirement less than 20%.
Description of drawings
Accompanying drawing is hydrogenating desulfurization provided by the invention, fall alkene, carry the method schematic diagram of octane value.
Embodiment
Method provided by the invention is such implementation:
(1), be lighting end, heavy fraction with gasoline 60 ℃～80 ℃ cuttings;
(2), the petroleum naphtha fraction removes wherein mercaptan through alkali cleaning refining desulfurization alcohol;
(3), at first the heavy petrol fraction contacts with Hydrobon catalyst with hydrogen one, carry out hydrogenating desulfurization, denitrogenation, olefin saturation, reaction effluent contacts with octane value recovering catalyst, carry out isomerization, aromizing and the reaction such as superimposed, separate hydrogenated oil and obtain lighter hydrocarbons and gasoline fraction, hydrogen-rich gas recycles;
(4), the heavy petrol fraction after the desulfurization with refining after light gasoline fraction be mixed to get gasoline products.
Reaction effluent after heavy fractioning hydrogenation described in the step (3) is refining can directly contact with octane value recovering catalyst without separating; Also can isolate effluent behind the hydrogenation, emit wherein and contact with octane value recovering catalyst again behind the hydrogen sulfide, can further reduce like this sulphur content of product gasoline, can also reduce the temperature of reaction of octane value recovering reaction, be conducive to reduce energy consumption.
The hydrofining reaction condition is hydrogen dividing potential drop 1.5～3.0MPa in the step (3); 250～320 ℃ of temperature of reaction; Liquid hourly space velocity 3.0～5.0h
-1, hydrogen-oil ratio 200～500Nm
3/ m
3Used Hydrobon catalyst can be that the commercial trade mark of Fushun Petrochemical Company catalyst plant market sale is the catalyzer of FF-11, also can be other catalyzer that possesses the hydrofining function.
Octane value recovering process catalyst system therefor is on disclosed one or more complex carriers that load in aluminum oxide or the molecular sieve of patent CN1743428A in the step (3), the content of catalyzer is by weight percentage: active component content is 5～25%, is one or both group vibs or VIII family metal; Modifier content is 1～10%, is one or both oxide compounds in IIB family or the group of the lanthanides; Vector contg 74～94%.The octane value recovering condition is 350～440 ℃ of temperature of reaction; Liquid hourly space velocity 0.5～3.0h
-1, hydrogen-oil ratio 200～500Nm
3/ m
3
The technology that FCC gasoline provided by the present invention keeps the octane value desulfurization, fall alkene mainly contains following advantage than prior art:
(1) the product gasoline sulphur content that adopts present technique to obtain is reduced to＜100ppm, and octane value remains unchanged, and is particularly suitable for the catalytic gasoline hydrogenation modifying of high-octane rating, high sulfur content;
(2) be that the cut point of light gasoline fraction and heavy naphtha is 60 ℃～80 ℃ with the full fraction of gasoline, the fractionation principle is that thiophene does not enter in the lighting end, because the petroleum naphtha fraction is when caustic wash desulfuration alcohol, thiophenic sulfur can not be participated in reaction.
(3) high-pressure separator hydrogen-rich gas out returns compressor through the depriving hydrogen sulphide tank, reduces the hydrogen sulfide content in the recycle hydrogen, improves the reaction desulfuration rate;
(4) adopt the described light constituent with stabilizer tower of this patent to return again fractionation of separation column, make the product gasoline yield improve yield of gasoline and reach 98.5 % by weight.
Description of drawings
The bright process flow sheet of Fig. 1 this law.
Embodiment
Below in conjunction with accompanying drawing method provided by the present invention is further detailed.But not thereby limiting the invention.
Desulfurization when accompanying drawing is maintenance octane value provided by the invention, the method schematic diagram of alkene falls.
The flow process of the method is as follows:
Gasoline stocks enters separation column 2 through pipeline 1 and is cut into light gasoline fraction, heavy naphtha, wherein light gasoline fraction enters to subtract through pipeline 3 and washes unit 5, light gasoline fraction after the alkali cleaning is drawn through pipeline 6, heavy naphtha enters pump 7 through pipeline 4, heavy naphtha after boosting through pipeline 8 with after hydrogen-rich gas from pipeline 22 mixes, successively through pipeline 9, interchanger 10, pipeline 11 enters fixed bed hydrogenation reactor 12 and contacts with Hydrobon catalyst, reaction effluent enters octane value recovering reactor 14 through pipeline 13 and contacts with octane value recovering catalyst, carries out the octane value recovering reaction.The reaction effluent of reactor 14 enters high-pressure separator 17 through pipeline 15, interchanger 10, pipeline 16 successively, out hydrogen-rich gas is through depriving hydrogen sulphide tank 28 from separator 17 tops, enter compressor 19 by pipeline 18, hydrogen-rich gas after the compression through pipeline 20 or with from the additional fresh hydrogen of pipeline 21 through pipeline 22, and enter fixed bed hydrogenation reactor 12 reactions through pipeline 9, interchanger 10, pipeline 11 successively after heavy naphtha from pipeline 8 mixes.Enter stabilizer tower 24 from separator 17 bottoms liquid product out through pipeline 23, separate the lighter hydrocarbons obtain and get back to separation column 2 through pipeline 25, enter pump 7 with the supplied materials of pipeline 4; Simultaneously, separation column 24 separates the heavy naphtha that obtains draws through pipeline 26, mixes afterwards with light gasoline fraction from pipeline 6 to go out device as gasoline products through pipeline 27.
The technology of the present invention is because the lighter hydrocarbons that stabilizer tower is separated return separation column, reduced loss, thereby the liquid receipts are increased to 98.5m%, can guarantee that in the gasoline high desulfurization rate gasoline octane rating does not lose, even increase to some extent, sulphur content in the product oil is reduced to 100ppm, and olefin(e) centent satisfies world's fuel oil standard gasoline standard II class index and Europe III requirement less than 20%.
The following examples will be further described method provided by the invention, but therefore not limit the present invention.
Embodiment 1
Take FCC gasoline A as raw material, first raw material is cut, cut point is 75 ℃, heavy naphtha accounts for stock oil 61 % by weight, its character is as shown in table 1, heavy naphtha, hydrogen contact with Hydrobon catalyst FF-11 and carry out hydrogenation reaction, and the heavy naphtha behind the hydrogenation and the light gasoline fraction behind the mercaptan removal obtain gasoline products after being in harmonious proportion, and hydrogenation technique condition and product property are as shown in table 2.
Embodiment 2
After cutting according to embodiment 1 described method take FCC gasoline A as raw material, heavy naphtha, hydrogen contact with Hydrobon catalyst FF-11, octane value recovering catalyst and carry out hydrotreatment, octane value recovering reaction.Heavy naphtha behind the hydrogenation and the light gasoline fraction behind the mercaptan removal obtain gasoline products after being in harmonious proportion, and processing condition and product property are as shown in table 2.
After cutting according to embodiment 1 described method take FCC gasoline A as raw material, heavy naphtha, hydrogen contact with Hydrobon catalyst FF-11, according to embodiment 1 the same terms, carry out hydrotreatment, separate the hydrofining reaction effluent, contact with recovering the octane value catalyzer again after removing hydrogen sulfide, recover the reaction of octane value.After being in harmonious proportion, heavy naphtha behind the recovery octane value and the light gasoline fraction behind the mercaptan removal obtain gasoline products.Recover octane value condition and product property as shown in table 2.
Take FCC gasoline B as raw material, first raw material is cut, cut point is 71 ℃, heavy naphtha accounts for stock oil 58.9 % by weight, its character is as shown in table 1, and heavy naphtha, hydrogen contact with Hydrobon catalyst FF-11, octane value recovering catalyst and carries out hydrotreatment, octane value recovering reaction.Obtain gasoline products after heavy naphtha behind the recovery octane value and the light gasoline fraction behind the mercaptan removal are in harmonious proportion, hydrogenation technique condition and product property are as shown in table 3.
Take FCC gasoline B as raw material, after cutting according to embodiment 4 described methods, heavy naphtha, hydrogen contact with Hydrobon catalyst FF-11, octane value recovering catalyst and carry out hydrotreatment, octane value recovering reaction.Heavy naphtha behind the hydrogenation and the light gasoline fraction behind the mercaptan removal obtain gasoline products after being in harmonious proportion, and hydrogenation technique condition and product property are as shown in table 3.
Table 1
Table 2
| Sulphur content ppm | 53.0 | 47.1 | 32.6 |
| Olefin(e) centent, v% | 19.6 | 21.0 | 20.0 |
| RON | 80.3 | 92.9 | 93.7 |
Table 3
Claims (1)
1. the method for a catalytic gasoline hydrogenation modifying is characterized in that: comprise the following steps:
(1), be light gasoline fraction, heavy petrol fraction with the full faction cut of gasoline, its cut point temperature is 60～80 ℃, the fractionation principle is that thiophene is cut in the last running;
(2), the petroleum naphtha fraction removes wherein mercaptan through caustic wash desulfuration alcohol;
(3), at first the heavy petrol fraction contact with Hydrobon catalyst with hydrogen one, carries out hydrogenating desulfurization, denitrogenation, olefin saturation;
The hydrofining reaction condition is hydrogen dividing potential drop 1.5～3.0MPa; 250～320 ℃ of temperature of reaction; Liquid hourly space velocity 3.0～5.0h
-1, hydrogen-oil ratio 200～500Nm
3/ m
3
Hydrobon catalyst is that the commercially available trade names of Fushun petrochemical corporation (complex) are the catalyzer of FF-11;
(4), reaction effluent or reaction effluent contact with octane value recovering catalyst after removing hydrogen sulfide, carries out isomerization, aromizing and building-up reactions, separates hydrogenated oil, obtains lighter hydrocarbons and heavy naphtha;
Octane value recovering catalyst is that patent CN1743428A is disclosed, load on one or more complex carriers in aluminum oxide or the molecular sieve, the content of catalyzer is by weight percentage: active component content is 5～25%, is one or both group vibs or VIII family metal; Modifier content is 1～10%, is one or both oxide compounds in IIB family or the group of the lanthanides; Vector contg 74～94%; The octane value recovering condition is 350～440 ℃ of temperature of reaction; Liquid hourly space velocity 0.5～3.0h
-1, hydrogen-oil ratio 200～500Nm
3/ m
3
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200710120343 CN101368111B (en) | 2007-08-16 | 2007-08-16 | Hydrogenation modification method for catalytically cracked gasoline |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200710120343 CN101368111B (en) | 2007-08-16 | 2007-08-16 | Hydrogenation modification method for catalytically cracked gasoline |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101368111A CN101368111A (en) | 2009-02-18 |
| CN101368111B true CN101368111B (en) | 2013-04-24 |
Family
ID=40412111
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200710120343 Active CN101368111B (en) | 2007-08-16 | 2007-08-16 | Hydrogenation modification method for catalytically cracked gasoline |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101368111B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2014197205A1 (en) * | 2013-06-04 | 2014-12-11 | Uop Llc | Naphtha cracking |
| US9328298B2 (en) | 2013-06-04 | 2016-05-03 | Uop Llc | Naphtha cracking |
| US9328299B2 (en) | 2013-06-04 | 2016-05-03 | Uop Llc | Naphtha cracking |
Families Citing this family (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101962564B (en) * | 2009-07-23 | 2013-04-24 | 中国石油化工股份有限公司 | Method for preventing ethylene device gasoline fractionating tower from scale formation and blockage |
| CN102199448A (en) * | 2010-03-26 | 2011-09-28 | 中国石油天然气股份有限公司 | Process method for reducing olefins by hydrogen desulfurization of catalytic gasoline |
| CN101885983B (en) * | 2010-07-02 | 2013-04-24 | 中国石油大学(北京) | Efficient coupling hydro-upgrading method for producing gasoline with ultra-low sulfur and high octane number |
| CN103059951B (en) * | 2011-10-21 | 2015-04-15 | 中国石油化工股份有限公司 | Catalytic cracking and catalytic gasoline hydrogenation combined technological method |
| CN103059945B (en) * | 2011-10-21 | 2015-09-30 | 中国石油化工股份有限公司 | A kind of process for catalyzed gasoline hydrogenation desulfurization |
| CN103074104B (en) * | 2011-10-26 | 2015-11-25 | 中国石油化工股份有限公司 | A kind of gasoline hydrodesulfurizationmethod method |
| CN103773432B (en) * | 2012-10-24 | 2015-11-25 | 中国石油化工股份有限公司 | A kind of gasoline desulfating method |
| CN103773431B (en) * | 2012-10-24 | 2016-01-20 | 中国石油化工股份有限公司 | A kind of gasoline desulfating method |
| CN103805269B (en) * | 2012-11-07 | 2015-11-18 | 中国石油化工股份有限公司 | A kind of catalytic gasoline deep hydrodesulfurizationmethod method |
| CN105733672A (en) * | 2014-12-11 | 2016-07-06 | 中国石油天然气股份有限公司 | Ultra low sulfur gasoline combination production method |
| RU2754030C2 (en) | 2016-10-21 | 2021-08-25 | Чайна Петролеум Энд Кемикал Корпорейшн | Method for purifying gasoline |
| CN111378503B (en) * | 2020-04-22 | 2022-02-25 | 中化弘润石油化工有限公司 | Method for producing clean gasoline by catalytically cracking gasoline |
| CN116004283B (en) * | 2021-10-22 | 2024-05-17 | 中国石油化工股份有限公司 | Hydrocracking method for producing low-sulfur heavy naphtha |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1621495A (en) * | 2004-10-18 | 2005-06-01 | 中国石油化工集团公司 | Hydrogenation modification process for low grade gasoline |
| CN1769388A (en) * | 2004-10-29 | 2006-05-10 | 中国石油化工股份有限公司 | Hydrogenation and quality improvement method for reducing sulfur and olefin content of inferior gasoline |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1208436C (en) * | 2002-06-27 | 2005-06-29 | 中国石油化工股份有限公司 | Method of heavily desulfurating and reducing olefinic hydrocarbon for gasoline |
-
2007
- 2007-08-16 CN CN 200710120343 patent/CN101368111B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1621495A (en) * | 2004-10-18 | 2005-06-01 | 中国石油化工集团公司 | Hydrogenation modification process for low grade gasoline |
| CN1769388A (en) * | 2004-10-29 | 2006-05-10 | 中国石油化工股份有限公司 | Hydrogenation and quality improvement method for reducing sulfur and olefin content of inferior gasoline |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2014197205A1 (en) * | 2013-06-04 | 2014-12-11 | Uop Llc | Naphtha cracking |
| US9328298B2 (en) | 2013-06-04 | 2016-05-03 | Uop Llc | Naphtha cracking |
| US9328299B2 (en) | 2013-06-04 | 2016-05-03 | Uop Llc | Naphtha cracking |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101368111A (en) | 2009-02-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101368111B (en) | Hydrogenation modification method for catalytically cracked gasoline | |
| CN101787307B (en) | Gasoline hydrodesulfurization method | |
| CN1224679C (en) | Method for producing low sulfur gasoline | |
| CN102311795B (en) | Hydrogenation method for producing high-octane gasoline components by diesel oil raw material | |
| CN102061194B (en) | Method for lowering content of sulphur in gasoline | |
| CN103074107B (en) | A kind of method of producing the full distillation gasoline product of super low sulfur | |
| CN101275084B (en) | Method for reducing sulfur content of catalytically cracked gasoline | |
| CN102337153B (en) | Hydrotreatment method of gasoline distillate oil | |
| CN103305269B (en) | Method for producing gasoline and diesel by directly hydrogenating medium and low temperature coal tar | |
| CN102757818A (en) | Sulfur-free gasoline production method | |
| CN103074106B (en) | A kind of method reducing content of sulfur in gasoline | |
| CN102399585B (en) | Method for producing sweet gasoline | |
| CN101993725B (en) | Method for producing low-sulfur gasoline | |
| CN1208436C (en) | Method of heavily desulfurating and reducing olefinic hydrocarbon for gasoline | |
| CN1782034A (en) | Method for simultanesusly reducing sulfur and olefine content in gasoline | |
| CN101161791B (en) | Method for producing clean gasoline | |
| CN1224675C (en) | Method for producing sweet gasoline | |
| CN100448955C (en) | Hydrogenization method for deep desulfurization of gasoline, and lowering olefin | |
| CN101314734B (en) | Selective hydrogenation desulfurization method for gasoline | |
| CN102199448A (en) | Process method for reducing olefins by hydrogen desulfurization of catalytic gasoline | |
| CN109722308B (en) | Method for producing low-sulfur low-olefin gasoline | |
| CN109988635B (en) | Hydrotreatment and hydrocracking combined process | |
| CN100510018C (en) | Method for improving quality of gasolene through hydrogenation | |
| CN109988600B (en) | Flexible hydrogenation modification process for poor diesel oil | |
| CN103087770A (en) | Clean gasoline production method through selective hydrogenation and desulfurization of catalytic gasoline |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |