CN1465666A - Method of heavily desulfurating and reducing olefinic hydrocarbon for gasoline - Google Patents

Method of heavily desulfurating and reducing olefinic hydrocarbon for gasoline Download PDF

Info

Publication number
CN1465666A
CN1465666A CNA021215952A CN02121595A CN1465666A CN 1465666 A CN1465666 A CN 1465666A CN A021215952 A CNA021215952 A CN A021215952A CN 02121595 A CN02121595 A CN 02121595A CN 1465666 A CN1465666 A CN 1465666A
Authority
CN
China
Prior art keywords
gasoline
heavy
catalyst
fraction
heavy naphtha
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.)
Granted
Application number
CNA021215952A
Other languages
Chinese (zh)
Other versions
CN1208436C (en
Inventor
李大东
石玉林
胡云剑
习远兵
李明丰
石亚华
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Sinopec Research Institute of Petroleum Processing
China Petroleum and Chemical Corp
Original Assignee
Sinopec Research Institute of Petroleum Processing
China Petroleum and Chemical Corp
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Sinopec Research Institute of Petroleum Processing, China Petroleum and Chemical Corp filed Critical Sinopec Research Institute of Petroleum Processing
Priority to CNB021215952A priority Critical patent/CN1208436C/en
Priority to KR1020030042481A priority patent/KR100980324B1/en
Publication of CN1465666A publication Critical patent/CN1465666A/en
Application granted granted Critical
Publication of CN1208436C publication Critical patent/CN1208436C/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
    • C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
    • C10G45/12—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/1048—Middle distillates
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/202—Heteroatoms content, i.e. S, N, O, P

Abstract

The method for further desulfurization and reducing olefine content in the gasoline includes the following steps: cutting the gasoline raw material into light fraction and heavy fraction, making the light fraction undergo the processes of alkali refinement treatment and removing mercaptans, and making the heavy fraction and hydrogen gas successively contact with hydrogenation refining catalyst and octane value restoring agent, then mixing the above-mentioned desulfurized light fraction and heavy fraction so as to obtain the invented gasoline product in which the sulfur content is less than 200 ppm and olefine content is less than 20 V%.

Description

A kind of method of deep desulfurization olefin hydrocarbon reduction of gasoline
Technical field
The invention belongs in the method that has refining hydrocarbon ils under the situation of hydrogen, more particularly, is that olefins process falls in the hydrogenating desulfurization that belongs to a kind of gasoline fraction.
Background technology
Along with the continuous enhancing of people to environmental consciousness, the discharging of hazardous and noxious substances will be strictly controlled in the vehicle exhaust, and therefore the oil quality as motor spirit requires more and more tighter.Various countries have all proposed very harsh restriction index to motor spirit specification such as oxygen level, vapour pressure, benzene content, aromatic hydrocarbons total content, boiling point, olefin(e) centent and sulphur content etc. for this reason, to reduce emission of harmful substances.Contrast China's motor spirit new standard and " world's fuel oil standard " II class gasoline index can find that the subject matter of China's quality of gasoline is sulphur content and olefin(e) centent height.The major cause of sulfur in gasoline and olefin(e) centent superelevation is because the ratio that catalytic cracking (FCC) gasoline accounts in the gasoline pool is too high.In China, catalytically cracked gasoline is a main blend component in the gasoline mediation pond, accounts for more than 80%.FCC content of sulfur in gasoline height, olefin(e) centent height.And, the raw material of processing along with FCC develops to the heaviness direction, to cause sulphur content and olefin(e) centent in the FCC gasoline further to increase, and realize that content of olefin in gasoline will be lower than very difficulty of 20% standard, the gasoline produced of national many refineries all is difficult to satisfy the requirement of New standard gasoline at present.Therefore reduce FCC sulfur in gasoline and olefin(e) centent and be the main path of sulphur and olefin(e) centent in the control motor spirit.
Though traditional FCC gasoline hydrogenation technology can reduce sulphur content significantly, reduce olefin(e) centent simultaneously, but because the olefin component of hydrogenation process high-octane rating performance is by saturated in a large number, cause the gasoline octane rating loss very big, the domestic gasoline particularly higher to olefin(e) centent, that aromaticity content is lower, loss of octane number is bigger.Therefore, it is extremely urgent to develop a kind of FCC deep desulfurization olefin hydrocarbon reduction of gasoline technology of new loss of octane number minimum.
The disclosed gasoline modifying method of US5411658 is that elder generation adopts beta-zeolite catalyst that hydrorefined reaction effluent is carried out octane value recovering after adopting traditional Hydrobon catalyst with the FCC gasoline hydrofinishing then.But the employed raw material final boiling point of this method is higher, and the too high aromatic hydrocarbons that makes of hydrofining section temperature of reaction is saturated more, causes research octane number (RON) (being RON) loss bigger, is difficult to recover.
Disclosed gasoline of US5599439 and reformed oil method for modifying are, first section is carried out hydrofining earlier, it is saturated to remove impurity such as sulphur, nitrogen and alkene, pass through again intermediate section from, the gas that process is isolated behind the impurity such as hydrogen sulfide, ammonia directly loops back first section, intermediates oil enters second section and carry out the octane value recovering process in fluidized-bed reactor, and this section is no longer mended new hydrogen.This method has increased a separator between one, two section, increase facility investment, and working pressure is low excessively simultaneously, is unfavorable for the long-term operation of catalyzer.
The disclosed gasoline modifying method of US5391288 is, to separate the mixed distillate of the distillate that is rich in benzene that obtains in FCC gasoline and the reformate is raw material, first section is carried out hydrofining earlier, with foreign matter contents such as the sulphur in the reduction raw material, nitrogen, hydrogenation of olefins is saturated simultaneously, intermediate product enters second section, carries out octane value recovering reaction under the acid function catalyst action having, and cracking reaction, alkylation reaction of arene and the transalkylation reaction of alkane mainly takes place.But it is on the low side to make with extra care the section reaction velocity, and catalyst levels is big.Owing to sneak into benzene in the raw material, cause aromaticity content increase in the product simultaneously.
The disclosed gasoline modifying method of US5399258 is, first section through hydrogenation desulfurization and denitrogenation, hydrogenation of olefins saturated after, the intermediate product that obtains directly enters second section and carries out the octane value recovering reaction.First section temperature of reaction is higher, and is fair with second section temperature of reaction.Because first section temperature of reaction is too high, causes final product to produce a large amount of mercaptan sulfurs, temperature is high more, and the mercaptan sulfur of generation is many more.
Because the final boiling point of domestic FCC gasoline is lower than external FCC gasoline final boiling point, the olefin(e) centent of domestic FCC gasoline is higher simultaneously, and aromaticity content is lower.Therefore use above-mentioned prior art that domestic FCC gasoline is carried out hydrogenating desulfurization, alkene is saturated too many, makes loss of octane number bigger.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology a kind of method of deep desulfurization olefin hydrocarbon reduction of gasoline, produce the II class gasoline that meets world's fuel oil standard, guarantee that simultaneously the anti-knock index loss of gasoline is minimum.
Method provided by the invention comprises the following steps:
(1), gasoline stocks is cut into light gasoline fraction, heavy naphtha, wherein the cut point of light gasoline fraction and heavy naphtha is respectively 70 ℃～100 ℃, and the yield of light gasoline fraction and heavy naphtha is respectively the heavy % in 30 heavy %～60 and the heavy % in 40 heavy %～70 of gasoline stocks;
(2), light gasoline fraction removes wherein mercaptan through alkali cleaning refining desulfurization alcohol;
(3), at first heavy naphtha contacts with Hydrobon catalyst with hydrogen one, carry out hydrogenation desulfurization and denitrogenation, olefin saturation, reaction effluent directly contacts with octane value recovering catalyst without separating, and separates hydrogenated oil and obtains lighter hydrocarbons and gasoline fraction, and hydrogen-rich gas recycles;
(4), the heavy naphtha after the desulfurization with refining after light gasoline fraction mix and obtain gasoline products.
The loss of octane number minimum of the present invention's gasoline under the situation of gasoline desulfur rate maximum, sulfur in gasoline content is lower than 200ppm, and olefin(e) centent satisfies II class content of sulfur in gasoline standard in world's fuel oil standard less than 20v%.
Description of drawings
Accompanying drawing is the method synoptic diagram of deep desulfurization olefin hydrocarbon reduction of gasoline provided by the invention.
Embodiment
Method provided by the invention is so concrete enforcement:
(1), gasoline stocks is cut into light gasoline fraction, heavy naphtha under 70 ℃～100 ℃, the yield of light gasoline fraction, heavy naphtha is respectively the heavy % in the heavy % in 30 heavy %～60,40 heavy %～70 of gasoline stocks;
(2), light gasoline fraction is through the refining mercaptan that removes wherein of alkali extracting;
(3), at first heavy naphtha contacts with Hydrobon catalyst with hydrogen one, carry out hydrogenation desulfurization and denitrogenation, olefin saturation, reaction effluent directly contacts the isomerization reaction that low octane rating alkane molecule cracking reaction and alkane molecule take place without separating with octane value recovering catalyst, separate hydrogenated oil and obtain lighter hydrocarbons and gasoline fraction, hydrogen-rich gas recycles;
(4), the heavy naphtha after the desulfurization with refining after light gasoline fraction mix and obtain gasoline products.
The used gasoline stocks of the present invention is FCC gasoline, catalytic cracking gasoline, straight-run spirit, coker gasoline, pyrolysis gasoline, pressure gasoline or its mixture.The final boiling point of this raw material ≯ 220 ℃, lower than external FCC gasoline final boiling point, sulphur content is not more than 1500ppm.The FCC sulfur in gasoline mainly concentrates in the high boiling point molecule, and alkene distributes to be increased along with the reduction of cut boiling point, because the olefin(e) centent of domestic FCC gasoline is higher, aromaticity content is lower.A large amount of alkene are saturated by hydrogenation in to the FCC gasoline hydrodesulfurizationmethod, and alkene is a kind of high-octane number component, so the loss of octane number of gasoline is very big, must carry out the recovery of octane value after the desulfurization.
Used alkali is sodium hydroxide solution etc. in the step (2).
The middle hydrogenation desulfurization and denitrogenation of step (3), the reaction conditions that alkene is saturated are: hydrogen dividing potential drop 1.0～4.0MPa; 200～380 ℃ of temperature of reaction, liquid hourly space velocity 3.0～5.0h -1, hydrogen-oil ratio 200～600Nm 3/ m 3The 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.The condition of octane value recovering is: 300～460 ℃ of temperature of reaction; Liquid hourly space velocity can be 0.5～4.0h -1, hydrogen-oil ratio can be 200～1000Nm 3/ m 3
Octane value recovering process catalyst system therefor must have enough acid functions, 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.
Below in conjunction with accompanying drawing method provided by the present invention is further detailed.But it is not thereby limiting the invention.
Accompanying drawing is the method synoptic diagram of deep desulfurization olefin hydrocarbon reduction of gasoline provided by the invention.
The flow process of this 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 alkali cleaning unit 5 through pipeline 3, 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, the hydrogen-rich gas that comes out from separator 17 tops enters compressor 19 through 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.The liquid product that comes out from separator 17 bottoms enters stabilizer tower 24 through pipeline 23, separate the lighter hydrocarbons and the heavy naphtha that obtain and draw through pipeline 25,26 respectively, light gasoline fraction, the heavy naphtha from pipeline 6,26 goes out device as gasoline products through pipeline 27 after mixing respectively.
At China's content of olefin in gasoline height (can up to 55v%), aromaticity content low (＜20v%), characteristics that final boiling point is low, the present invention is cut into earlier gently, last running, respectively mercaptan removal is carried out in lighting end again, hydrotreatment, octane value recovering are carried out in last running successively, light, last running blending after will making with extra care at last are final gasoline products, satisfying world fuel oil standard II class gasoline index is that sulphur content is lower than 200ppm, olefin(e) centent is lower than 20v%, guarantees the minimum even slightly increase of anti-knock index (RON+MON)/2 loss simultaneously.
The following examples will give further instruction to method provided by the invention, but therefore not limit the present invention.
The used Hydrobon catalyst and the trade names of octane value recovering catalyst are respectively CH-18 and RIDOS-1 among the embodiment, and these two kinds of catalyzer are produced by Sinopec Group's Chang Ling oil-refining chemical head factory catalyst plant.
Comparative Examples
With FCC gasoline A is raw material, earlier raw material is cut, and cut point is 80 ℃, and heavy naphtha accounts for 67.5 weight % of raw material, and its character is as shown in table 1.Heavy naphtha, hydrogen contact with catalyzer CH-18 and carry out hydrogenation reaction, and do not carry out octane value recovering.Obtain gasoline products after heavy naphtha behind the hydrogenation and the blending of the light gasoline fraction behind the mercaptan removal, hydrogenation technique condition and product property are as shown in table 2.As can be seen from Table 2, though the sulphur content of product is 8ppm, anti-knock index (RON+MON)/2 loses up to 9.9 units.
Embodiment 1
Compare with Comparative Examples, under the identical situation of raw material, heavy naphtha, hydrogen contact with catalyzer CH-18, RIDOS-1 successively and carry out hydrotreatment, octane value recovering.Obtain gasoline products after heavy naphtha behind the hydrogenation and the blending of the light gasoline fraction behind the mercaptan removal, processing condition and product property are as shown in table 2.As can be seen from Table 2, the sulphur content of heavy naphtha is 9ppm, and olefin(e) centent is 18.2v%, and anti-knock index has increased by 0.2 unit.
Embodiment 2
With FCC gasoline B is raw material, earlier raw material is cut, and cut point is 88 ℃, and heavy naphtha accounts for 69.8 weight % of raw material, and its character is as shown in table 1.Heavy naphtha, hydrogen contact with catalyzer CH-18, RIDOS-1 successively and carry out hydrotreatment, octane value recovering.Obtain gasoline products after heavy naphtha behind the hydrogenation and the blending of the light gasoline fraction behind the mercaptan removal, hydrogenation technique condition and product property are as shown in table 3.As can be seen from Table 3, the sulphur content of heavy naphtha is 161ppm, and olefin(e) centent is 16.9v%, and anti-knock index has increased by 1.2 units.
Embodiment 3
With FCC gasoline C is raw material, earlier raw material is cut, and cut point is 95 ℃, and heavy naphtha accounts for 60.1 weight % of raw material, and its character is as shown in table 1.Heavy naphtha, hydrogen contact with catalyzer CH-18, RIDOS-1 successively and carry out hydrotreatment, octane value recovering.Obtain gasoline products after heavy naphtha behind the hydrogenation and the blending of the light gasoline fraction behind the mercaptan removal, hydrogenation technique condition and product property are as shown in table 3.As can be seen from Table 3, the sulphur content of heavy naphtha is 100ppm, and olefin(e) centent is 19.8v%, and the anti-knock index loss is 0.6 unit only.
Table 1
Raw material A Raw material B Raw material C
Density (20 ℃), g/cm 3 ????0.7112 ????0.7083 ????0.7382
Sulphur content, ppm ????85 ????1400 ????1300
Olefin(e) centent, v% ????49.3 ????38.6 ????54.3
Boiling range, ℃
Initial boiling point ????30 ????34 ????45
10％ ????48 ????44 ????50
50％ ????87 ????84 ????100
Final boiling point ????181 ????196 ????211
Anti-knock index ????85.2 ????86.6 ????87.3
Table 2
Comparative Examples Embodiment 1
The hydrogen dividing potential drop, MPa ????3.2
T，℃
Hydrotreatment ????280 ????280
Octane value recovering ????- ????370
Liquid hourly space velocity, h -1
Hydrotreatment ????4.0 ????4.0
Octane value recovering ????0.8 ????0.8
Hydrogen-oil ratio, Nm 3/m 3 ????500 ????500
Product property
Density (20 ℃), g/cm 3 ????0.7077 ????0.6997
Sulphur content, ppm ????8 ????9
Olefin(e) centent, v% ????19.3 ????18.2
Anti-knock index ????75.3 ????85.4
Table 2
Embodiment 2 Embodiment 3
The hydrogen dividing potential drop, MPa ????3.2 ????3.2
T，℃
Hydrotreatment ????280 ????290
Octane value recovering ????370 ????380
Liquid hourly space velocity, h -1
Hydrotreatment ????4.0 ????4.0
Octane value recovering ????0.8 ????0.8
Hydrogen-oil ratio, Nm 3/m 3 ????500 ????500
Product property
Density (20 ℃), g/cm 3 ????0.7077 ????0.7300
Sulphur content, ppm ????161 ????100
Olefin(e) centent, v% ????16.9 ????19.8
Anti-knock index ????87.8 ????86.7

Claims (6)

1, a kind of method of deep desulfurization olefin hydrocarbon reduction of gasoline comprises the following steps:
(1), gasoline stocks is cut into light gasoline fraction, heavy naphtha, wherein the cut point of light gasoline fraction and heavy naphtha is respectively 70 ℃～100 ℃, and the yield of light gasoline fraction and heavy naphtha is respectively the heavy % in 30 heavy %～60 and the heavy % in 40 heavy %～70 of gasoline stocks;
(2), light gasoline fraction removes wherein mercaptan through alkali cleaning refining desulfurization alcohol;
(3), at first heavy naphtha contacts with Hydrobon catalyst with hydrogen one, carry out hydrogenation desulfurization and denitrogenation, olefin saturation, reaction effluent directly contacts with octane value recovering catalyst without separating, and separates hydrogenated oil and obtains lighter hydrocarbons and gasoline fraction, and hydrogen-rich gas recycles;
(4), the heavy naphtha after the desulfurization with refining after light gasoline fraction mix and obtain gasoline products.
2,, it is characterized in that described gasoline stocks is catalytically cracked gasoline, catalytic cracking gasoline, straight-run spirit, coker gasoline, pyrolysis gasoline, pressure gasoline or its mixture according to the method for claim 1.
3,, it is characterized in that hydrorefined reaction conditions is in the described step (3): hydrogen dividing potential drop 1.0～4.0MPa according to the method for claim 1; 200～380 ℃ of temperature of reaction, liquid hourly space velocity 3.0～5.0h -1, hydrogen-oil ratio 200～600Nm 3/ m 3
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.
CNB021215952A 2002-06-27 2002-06-27 Method of heavily desulfurating and reducing olefinic hydrocarbon for gasoline Expired - Lifetime CN1208436C (en)

Priority Applications (2)

Application Number Priority Date Filing Date Title
CNB021215952A CN1208436C (en) 2002-06-27 2002-06-27 Method of heavily desulfurating and reducing olefinic hydrocarbon for gasoline
KR1020030042481A KR100980324B1 (en) 2002-06-27 2003-06-27 A process for reducing sulfur and olefin contents in gasoline

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CNB021215952A CN1208436C (en) 2002-06-27 2002-06-27 Method of heavily desulfurating and reducing olefinic hydrocarbon for gasoline

Publications (2)

Publication Number Publication Date
CN1465666A true CN1465666A (en) 2004-01-07
CN1208436C CN1208436C (en) 2005-06-29

Family

ID=34142216

Family Applications (1)

Application Number Title Priority Date Filing Date
CNB021215952A Expired - Lifetime CN1208436C (en) 2002-06-27 2002-06-27 Method of heavily desulfurating and reducing olefinic hydrocarbon for gasoline

Country Status (2)

Country Link
KR (1) KR100980324B1 (en)
CN (1) CN1208436C (en)

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN100344733C (en) * 2004-11-30 2007-10-24 中国石油化工股份有限公司 Method for simultanesusly reducing sulfur and olefine content in gasoline
CN100448955C (en) * 2005-10-31 2009-01-07 中国石油化工股份有限公司 Hydrogenization method for deep desulfurization of gasoline, and lowering olefin
CN101368111A (en) * 2007-08-16 2009-02-18 中国石油天然气集团公司 Hydrogenation modification method for catalytically cracked gasoline
CN101037615B (en) * 2006-03-15 2011-04-20 中国石油化工股份有限公司 Catalytic cracking gasoline modification method
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
CN102212394A (en) * 2010-04-07 2011-10-12 中国石油天然气股份有限公司 Fluid catalytic cracking (FCC) gasoline modification method comprising light gasoline etherification process
CN101275084B (en) * 2007-03-30 2012-02-22 中国石油化工股份有限公司 Method for reducing sulfur content of catalytically cracked gasoline
CN102443432A (en) * 2010-10-15 2012-05-09 中国石油化工股份有限公司 Method for producing low-sulfur gasoline by non-hydroforming sulfur and alcohol removal
CN102533330A (en) * 2010-12-31 2012-07-04 中国石油化工股份有限公司 Method for producing low-sulfur gasoline
US8597494B2 (en) 2009-03-19 2013-12-03 China University of Petroleum—Beijing (CUPB) Method for producing ultra-clean gasoline
US8603324B2 (en) 2009-03-19 2013-12-10 China University of Petroleum—Bejing (CUPB) Method for hydro-upgrading inferior gasoline via ultra-deep desulfurization and octane number recovery

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5298150A (en) 1991-08-15 1994-03-29 Mobil Oil Corporation Gasoline upgrading process
US5326463A (en) * 1991-08-15 1994-07-05 Mobil Oil Corporation Gasoline upgrading process

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN100344733C (en) * 2004-11-30 2007-10-24 中国石油化工股份有限公司 Method for simultanesusly reducing sulfur and olefine content in gasoline
CN100448955C (en) * 2005-10-31 2009-01-07 中国石油化工股份有限公司 Hydrogenization method for deep desulfurization of gasoline, and lowering olefin
CN101037615B (en) * 2006-03-15 2011-04-20 中国石油化工股份有限公司 Catalytic cracking gasoline modification method
CN101275084B (en) * 2007-03-30 2012-02-22 中国石油化工股份有限公司 Method for reducing sulfur content of catalytically cracked gasoline
CN101368111A (en) * 2007-08-16 2009-02-18 中国石油天然气集团公司 Hydrogenation modification method for catalytically cracked gasoline
US8597494B2 (en) 2009-03-19 2013-12-03 China University of Petroleum—Beijing (CUPB) Method for producing ultra-clean gasoline
US8603324B2 (en) 2009-03-19 2013-12-10 China University of Petroleum—Bejing (CUPB) Method for hydro-upgrading inferior gasoline via ultra-deep desulfurization and octane number recovery
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
CN102212394A (en) * 2010-04-07 2011-10-12 中国石油天然气股份有限公司 Fluid catalytic cracking (FCC) gasoline modification method comprising light gasoline etherification process
CN102212394B (en) * 2010-04-07 2013-11-06 中国石油天然气股份有限公司 Fluid catalytic cracking (FCC) gasoline modification method comprising light gasoline etherification process
CN102443432A (en) * 2010-10-15 2012-05-09 中国石油化工股份有限公司 Method for producing low-sulfur gasoline by non-hydroforming sulfur and alcohol removal
CN102443432B (en) * 2010-10-15 2014-05-28 中国石油化工股份有限公司 Method for producing low-sulfur gasoline by non-hydroforming sulfur and alcohol removal
CN102533330A (en) * 2010-12-31 2012-07-04 中国石油化工股份有限公司 Method for producing low-sulfur gasoline
CN102533330B (en) * 2010-12-31 2014-05-28 中国石油化工股份有限公司 Method for producing low-sulfur gasoline

Also Published As

Publication number Publication date
KR100980324B1 (en) 2010-09-06
KR20040002776A (en) 2004-01-07
CN1208436C (en) 2005-06-29

Similar Documents

Publication Publication Date Title
CN1224679C (en) Method for producing low sulfur gasoline
CN101368111B (en) Hydrogenation modification method for catalytically cracked gasoline
CN101492608A (en) Method for deep desulfurization olefin hydrocarbon reduction of inferior gasoline
CN1604956A (en) Process for sulfur reduction in naphtha streams
CN102311795A (en) Hydrogenation method for producing high-octane gasoline components by diesel oil raw material
CN101492609A (en) Method for deep desulfurization olefin hydrocarbon reduction of gasoline
CN102337153B (en) Hydrotreatment method of gasoline distillate oil
CN1208436C (en) Method of heavily desulfurating and reducing olefinic hydrocarbon for gasoline
CN103305269B (en) Method for producing gasoline and diesel by directly hydrogenating medium and low temperature coal tar
CN1171976C (en) Combined hydrogenation method of producing diesel oil with high cetane number and low solidifying point
CN100344733C (en) Method for simultanesusly reducing sulfur and olefine content in gasoline
CN1912063A (en) Method of producing catalytic reforming raw material
CN102399585B (en) Method for producing sweet gasoline
CN1643113A (en) Process for catalytically reforming a hydrocarbonaceous feedstock
CN1224675C (en) Method for producing sweet gasoline
RU2652982C2 (en) Process for hydrodesulphurisation of hydrocarbon cuts
CN101492610B (en) Method for deep desulfurization olefin hydrocarbon reduction of gasoline
CN1234815C (en) Method of gasoline desulfurization
CN102199448A (en) Process method for reducing olefins by hydrogen desulfurization of catalytic gasoline
CN1958740A (en) Hydrogenization method for deep desulfurization of gasoline, and lowering olefin
CN101314734B (en) Selective hydrogenation desulfurization method for gasoline
CN1727448A (en) Method for rectifying qualities of fractions of diesel oil
CN1313575C (en) Process for hydrogenating modifying faulty gasoline
CN1542103A (en) Medium pressure hydrogenation method for maximumly producing high quality diesel fuel
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
CX01 Expiry of patent term

Granted publication date: 20050629

CX01 Expiry of patent term