CN1313576C - Process for hydrogenating treatment of foulty gasoline - Google Patents
Process for hydrogenating treatment of foulty gasoline Download PDFInfo
- Publication number
- CN1313576C CN1313576C CNB031340105A CN03134010A CN1313576C CN 1313576 C CN1313576 C CN 1313576C CN B031340105 A CNB031340105 A CN B031340105A CN 03134010 A CN03134010 A CN 03134010A CN 1313576 C CN1313576 C CN 1313576C
- Authority
- CN
- China
- Prior art keywords
- gasoline
- catalyst bed
- catalyst
- hydrogen
- hydrogenation
- 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.)
- Expired - Lifetime
Links
- 238000000034 method Methods 0.000 title claims abstract description 24
- 230000008569 process Effects 0.000 title claims description 11
- 239000003054 catalyst Substances 0.000 claims abstract description 34
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 23
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 20
- 239000001257 hydrogen Substances 0.000 claims abstract description 20
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 18
- 238000006243 chemical reaction Methods 0.000 claims abstract description 17
- 230000003197 catalytic effect Effects 0.000 claims abstract description 6
- 238000012545 processing Methods 0.000 claims abstract description 6
- 239000002994 raw material Substances 0.000 claims abstract description 3
- 239000007788 liquid Substances 0.000 claims description 5
- 229910052751 metal Inorganic materials 0.000 claims description 5
- 239000002184 metal Substances 0.000 claims description 5
- 239000002808 molecular sieve Substances 0.000 claims description 5
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 5
- 229910021536 Zeolite Inorganic materials 0.000 claims description 4
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 4
- 229910052750 molybdenum Inorganic materials 0.000 claims description 4
- 229910052759 nickel Inorganic materials 0.000 claims description 4
- 229910052721 tungsten Inorganic materials 0.000 claims description 4
- 239000010457 zeolite Substances 0.000 claims description 4
- 229910017318 Mo—Ni Inorganic materials 0.000 claims description 3
- 229910017313 Mo—Co Inorganic materials 0.000 claims description 2
- 229910004298 SiO 2 Inorganic materials 0.000 claims description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 2
- 229910010413 TiO 2 Inorganic materials 0.000 claims description 2
- GEIAQOFPUVMAGM-UHFFFAOYSA-N ZrO Inorganic materials [Zr]=O GEIAQOFPUVMAGM-UHFFFAOYSA-N 0.000 claims description 2
- 238000001816 cooling Methods 0.000 claims description 2
- 229910052736 halogen Inorganic materials 0.000 claims description 2
- 150000002367 halogens Chemical class 0.000 claims description 2
- 229910052741 iridium Inorganic materials 0.000 claims description 2
- 229910044991 metal oxide Inorganic materials 0.000 claims description 2
- 150000002739 metals Chemical class 0.000 claims description 2
- 229910052697 platinum Inorganic materials 0.000 claims description 2
- 229910001404 rare earth metal oxide Inorganic materials 0.000 claims description 2
- 229910052702 rhenium Inorganic materials 0.000 claims description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims 3
- 229910018072 Al 2 O 3 Inorganic materials 0.000 claims 2
- 238000004821 distillation Methods 0.000 claims 2
- 239000002671 adjuvant Substances 0.000 claims 1
- 239000007809 chemical reaction catalyst Substances 0.000 claims 1
- 150000004706 metal oxides Chemical class 0.000 claims 1
- 239000000203 mixture Substances 0.000 claims 1
- 150000001336 alkenes Chemical class 0.000 abstract description 30
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 16
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 abstract description 14
- 238000005516 engineering process Methods 0.000 abstract description 13
- 229910052717 sulfur Inorganic materials 0.000 abstract description 7
- 239000011593 sulfur Substances 0.000 abstract description 7
- 239000005864 Sulphur Substances 0.000 description 12
- 239000000470 constituent Substances 0.000 description 11
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 9
- 238000006477 desulfuration reaction Methods 0.000 description 6
- 230000023556 desulfurization Effects 0.000 description 5
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 4
- 238000012360 testing method Methods 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 238000009835 boiling Methods 0.000 description 3
- 229920006395 saturated elastomer Polymers 0.000 description 3
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 2
- 239000010953 base metal Substances 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 238000006317 isomerization reaction Methods 0.000 description 2
- 239000010970 precious metal Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 239000012752 auxiliary agent Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 238000010523 cascade reaction Methods 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 239000003518 caustics Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 239000002638 heterogeneous catalyst Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- -1 metal oxide compound Chemical class 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 239000010913 used oil Substances 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
本发明公开了一种劣质汽油的加氢处理方法，其中加氢处理包括两个催化剂床层。劣质汽油原料与氢气在第一催化剂床层中与加氢改质催化剂接触，第一催化剂床层的流出物分离成轻重两个组分，其中的重组分进入第二催化剂床层，与氢气和加氢精制催化剂接触进行催化加氢脱硫反应，其流出物经冷却后与第一催化剂床层分离出的轻组分混合构成汽油产品全馏分。与现有加氢技术相比，本发明更适合于加工高硫、高烯烃的劣质汽油，它不但可以真正实现降烯不降辛烷值，而且还会实现未来对汽油硫含量更苛刻的要求。The invention discloses a method for hydrogenation treatment of inferior gasoline, wherein the hydrogenation treatment comprises two catalyst beds. Inferior gasoline raw material and hydrogen are in contact with the hydro-upgrading catalyst in the first catalyst bed, the effluent of the first catalyst bed is separated into light and heavy components, and the heavy component enters the second catalyst bed to be mixed with hydrogen and The hydrorefining catalyst is contacted to carry out the catalytic hydrodesulfurization reaction, and the effluent is cooled and mixed with the light components separated from the first catalyst bed to form the whole fraction of gasoline products. Compared with the existing hydrogenation technology, the present invention is more suitable for processing low-quality gasoline with high sulfur and high olefins. It can not only truly reduce olefins without reducing octane number, but also realize more stringent requirements for gasoline sulfur content in the future .
Description
Technical field
The present invention relates to a kind of hydrotreating process for light hydrocarbons, relate to the hydroprocessing process of high-sulfur inferior patrol specifically.
Background technology
Because sulphur in the gasoline and olefin(e) centent can increase CO, NO in the vehicle exhaust
XWith emission of harmful substances such as particulate matter, cause serious environmental to pollute.Therefore, the gasoline needs that meet new environmental regulation are controlled the concentration that olefin(e) centent also reduces aromatic hydrocarbons (particularly benzene) and sulphur as far as possible.But along with the change day by day of world petroleum resource is heavy, the main source of gasoline is a pressure gasoline, this type of gasoline is the olefin(e) centent height not only, and the sulphur of gasoline products almost 90% also derives from this, so each oil refinery company of the world all falls alkene in research and development, falls the Technology of sulphur, successful is hydrogenation technique at present.But when using this technology, also produced new problem, though that is exactly the sulfide in the hydrodesulfurization energy effective elimination gasoline, alkene that simultaneously also can octane value in the gasoline is higher exceedingly hydrogenation is saturated to low-octane alkane, cause the gasoline octane rating loss to become substandard product too much, as generally speaking, the gasoline desulfur rate reaches at 90% o'clock, and RON can lose 7～10 units, has also increased the hydrogen consumption simultaneously.Therefore, in order to overcome the shortcoming of above-mentioned technology, each company of great oil refining of the world all is fit to fall alkene, desulfurization and gasoline processing technology that octane value does not reduce in exploitation competitively.
Experimental study shows that alkene mainly concentrates in the lighter fraction in pressure gasoline, and sulfide mainly concentrates in the last running.In order to reduce the loss of octane number that causes because of hydrogenation of olefins is saturated, both economical, rational way is earlier the catalytic gasoline fractionation to be light, last running, and then carries out post-treatment respectively.At above-mentioned conclusion, patent US4397739 has proposed at first gasoline rectifying to be become light constituent and heavy constituent before hydrotreatment, heavy constituent is carried out the method for specific hydrogenating desulfurization again.The give chapter and verse difference of gasoline boiling point of patent US4131537 becomes several fractions with gasoline rectifying, three kinds of cuts preferably, and then under different condition, carry out desulfurization respectively.Above-mentioned technology can be by lighter fraction caustic wash desulfuration and heavy fractioning hydrogenation desulfurization, the purpose of reach and fall alkene, falling sulphur can avoid again that the light olefin hydrogenation is saturated to cause too much loss of octane number.Also there is deficiency in above-mentioned technology, and that is exactly to reduce more for a long time at product requirement alkene, still can not avoid the too much loss of octane value, generates substandard product, and the hydrogenation saturation of olefins also can increase the hydrogen consumption greatly.
CN 1316485A has proposed a kind of technology of gasoline being carried out modification by isomerizing hydrogenation, and this technology comprises two sections cascade reactions, and first section is carried out olefin isomerization, carries out hydrogenation reaction at second section then.First section dress be olefin isomerization catalyst, second section dress be olefin hydrogenation catalyst, this two-stage catalytic agent can be respectively charged into two reactors, or in the same reactor of packing into.The present invention can guarantee under the constant situation of gasoline octane rating, the content of alkene is reduced.But also there is the bigger shortcoming of hydrogen consumption in it.
Summary of the invention
In order more effectively to handle the gasoline fraction that contains alkene, sulfur-bearing with hydrogen addition technology, remedy above-mentioned the deficiencies in the prior art, the present invention proposes a kind of novel inferior patrol hydroprocessing process, this method can make inferior patrol desulfurization, to fall the alkene degree higher, and do not reduce the gasoline fraction octane value.
The hydroprocessing process of inferior patrol of the present invention, wherein hydrotreatment comprises two beds, its step is as follows:
A, bad gasoline contact with catalyst for hydro-upgrading in first beds with hydrogen, and reaction conditions is: hydrogen dividing potential drop 0.5～5.0MPa, best 1.0～4.0MPa; 320 ℃～450 ℃ of temperature, best 350 ℃～435 ℃; Liquid hourly space velocity 1.0h
-1～15.0h
-1, best 1.0h
-1～10.0h
-1Hydrogen-oil ratio 100～800, best 300～800;
B, the effluent of first beds is isolated light constituent and heavy constituent;
The heavy constituent of telling among C, the step B (being the higher part of sulphur content) enter second beds, contact with Hydrobon catalyst with hydrogen and carry out the catalytic desulfurhydrogenation reaction;
The effluent of D, second beds mixes with the isolated light constituent of first beds after cooling off and constitutes the full cut of gasoline products.
The catalyzer of first beds filling described in the above-mentioned steps A is a catalyst for hydro-upgrading, and carrier is Al
2O
3, halogen-containing Al
2O
3, one or more in SAPO-11, ZSM-12, ZSM-35, MCM-22, MCM-41, conventional ZSM-5 molecular sieve, ZSM-5 molecular sieve with small crystal grains, HBeta zeolite and the y-type zeolite etc.; So-called ZSM-5 molecular sieve with small crystal grains is meant that its size is less than 1 μ m.Auxiliary agent is TiO
2, SiO
2, ZrO
2, Al
2O
3, rare-earth oxide is (as La
2O
3) in waiting one or more.Loaded metal is a kind of or its various combination in the transition state base metals such as Co, Mo, Ni and W, also can be in the precious metals such as Pt, Re, Ir one or more, or while load base metal and precious metal.Loading for transiting state metals such as Co, Mo, Ni and W by the metal oxide compound, is generally 0.5wt%～20.0wt%, preferred 1.0wt%～15.0wt%.This kind catalyzer should have stronger hydrocracking, isomery, cyclisation functions such as (comprising aromizing).
Among the above-mentioned steps B, the product index that the effluent of first beds will satisfy according to its sulphur content carries out the separation of weight component.The isolating cut point of weight component is decided by sulphur, alkene equal size (just gasoline products sulphur, alkene equal size index) in the isolated light constituent, and the temperature that 95% of general isolated light constituent boiling range distillates a little is 95 ℃～135 ℃.
The second beds hydrodesulfurization process among the step C can adopt conventional Hydrobon catalyst, preferably adopts Mo-Co/ aluminum oxide, Mo-Ni/ aluminum oxide or W-Mo-Ni/ aluminum oxide; Adopt conventional hydrofining technology condition, reaction conditions is preferably: reaction pressure 1.0MPa～4.0MPa, 240 ℃～360 ℃ of temperature of reaction, volume space velocity 1.0h
-1～10.0h
-1With hydrogen to oil volume ratio 100～500.
First beds and second beds can be in same fixed-bed reactor, also can be in two different fixed-bed reactor.The reaction conditions of first beds shows as temperature height, operational condition harshness.In this bed, realize that mainly gasoline stocks falls alkene and do not fall octane value, and will easily remove the sulphur hydrogenation and take off; And the reaction conditions of second bed shows as that temperature is low, air speed is little, and operational condition relaxes.Mainly be that the difficulty in the gasoline stocks is removed sulphur (i.e. first beds fail to remove sulphur) hydrogenation and removing in this bed.
Reduction or rising situation according to the full cut octane value of gasoline products, determine whether the effluent of the second catalysts bed is necessary that part loops back first beds and processes, promptly when the reduction amplitude of the full cut octane value of gasoline products is big, then the effluent of the second catalysts bed is necessary that part loops back first beds and processes, otherwise then needn't.
The present invention is applicable to the various types of gasoline of processing, as straight-run spirit, catalytically cracked gasoline, coker gasoline etc., is particularly useful for processing the inferior patrol of high-sulfur, high olefin.
Compare with existing hydrogen addition technology, the present invention more helps processing the inferior patrol of high-sulfur, high olefin, and it not only can really be realized falling alkene and not fall octane value, but also can realize following harsher to content of sulfur in gasoline requirement.
Embodiment
Following embodiment further specifies of the present invention, and it does not limit use range of the present invention.
Embodiment 1～6
The main hydrogenation effect of investigating hydrogenation technique of the present invention of this test.With gasoline desulfur, alkene falls, octane value recovering is an example.Raw materials used oil properties sees Table 1 in this test.Hydrogenation reaction is all carried out in this test on the long run test device.Required catalyzer sees Table 2.The stock oil feeding temperature is 160 ℃, and operational condition and the test-results thereof of each embodiment see Table 3.
Table 1 stock oil main character
| Density, g/cm 3 | 0.732 |
| S，μg/g | 1635 |
| Alkene, v% | 52.9 |
| RON | 93.8 |
| Boiling range, ℃ 5%～95% | 52～185 |
Table 2 catalyzer physico-chemical property
| Heterogeneous catalyst | Hydrobon catalyst | |
| Catalytic active component | Ni | Mo、Co |
| Shape | Bar shaped | Bar shaped |
| Diameter, mm | 2.15 | 1.9 |
| Specific surface area, m 2/g | 454.4 | 198 |
| Pore volume, ml/g | 0.383 | 0.380 |
| Metal component (oxide compound meter), wt% NiO MoO 3 CoO | 3.5 - - | - 18.6 5.3 |
| Carrier | HBeta | Aluminum oxide |
The operational condition of each embodiment of table 3 and experimental result thereof
| Embodiment | 1 | 2 | 3 |
| Operational condition reaction pressure/MPa temperature of reaction/℃ first beds, second beds liquid hourly space velocity/h -1First beds, the second beds hydrogen to oil volume ratio, first beds, second beds | 1.0 370 320 4.0 4.0 300 200 | 2.0 390 320 4.0 5.0 300 200 | 3.0 420 320 6.0 6.0 300 300 |
| The light constituent cut point, T95/ ℃ | 120 | 120 | 120 |
| Full distillate oil character S, μ g/g alkene, v% RON loss | 90 28.1 -0.7 | 58 23.0 -1.3 | 32 19.0 -1.9 |
Operational condition and the experimental result thereof of continuous each embodiment of table 3
| Embodiment | 4 | 5 | 6 |
| Operational condition reaction pressure/MPa temperature of reaction/℃ first beds, second beds liquid hourly space velocity/h -1First beds, the second beds hydrogen to oil volume ratio, first beds, second beds | 2.5 390 340 6.0 4.0 300 200 | 2.5 390 340 6.0 4.0 300 200 | 2.5 390 340 6.0 4.0 300 200 |
| Light constituent cut point/T95/ ℃ | 95 | 110 | 135 |
| Full distillate oil character S, μ g/g alkene, v% RON loss | 5.6 14.1 0.7 | 45 21.0 -1.5 | 26 28.3 -1.8 |
Claims (9)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB031340105A CN1313576C (en) | 2003-09-15 | 2003-09-15 | Process for hydrogenating treatment of foulty gasoline |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB031340105A CN1313576C (en) | 2003-09-15 | 2003-09-15 | Process for hydrogenating treatment of foulty gasoline |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1597864A CN1597864A (en) | 2005-03-23 |
| CN1313576C true CN1313576C (en) | 2007-05-02 |
Family
ID=34658955
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB031340105A Expired - Lifetime CN1313576C (en) | 2003-09-15 | 2003-09-15 | Process for hydrogenating treatment of foulty gasoline |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1313576C (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101376827B (en) * | 2007-08-27 | 2012-04-04 | 中国石油化工股份有限公司 | Mixed hydrogenation process method for coker gasoline and straight-run kerosene |
| CN101434851B (en) * | 2007-11-15 | 2012-02-29 | 中国石油化工股份有限公司 | Mixed hydrogenation process for coker gasoline and coking kerosene |
| CN103102970B (en) * | 2011-11-10 | 2015-02-18 | 中国石油化工股份有限公司 | Inferior gasoline fraction hydrotreating method |
| CN106929098B (en) * | 2015-12-30 | 2018-10-16 | 中国石油天然气股份有限公司 | A method for hydrogenation upgrading of inferior catalytic gasoline |
| CN106929099B (en) * | 2015-12-30 | 2018-10-16 | 中国石油天然气股份有限公司 | A method for hydrogenation and upgrading of low-quality gasoline |
| CN119951569A (en) * | 2024-12-20 | 2025-05-09 | 中国科学院青岛生物能源与过程研究所 | A ZMQ-1 molecular sieve catalytic cracking catalyst with less carbon deposits and long service life |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4397739A (en) * | 1980-02-19 | 1983-08-09 | Institut Francais Du Petrole | Process for desulfurizing a catalytic cracking or steam cracking effluent |
| CN1253993A (en) * | 1998-11-18 | 2000-05-24 | 法国石油公司 | Production method of low-sulfur gasoline |
| EP1031622A1 (en) * | 1999-02-24 | 2000-08-30 | Institut Francais Du Petrole | Process for the production of low sulphur gasolines |
| JP2001009856A (en) * | 1999-06-22 | 2001-01-16 | Premark Rwp Holdings Inc | Coated press surface for wear-resistant laminated body and manufacture of laminated body using same |
| CN1316914A (en) * | 1998-09-10 | 2001-10-10 | 催化蒸馏技术公司 | Process for simultaneous treatment and fractionation of light naphtha hydrocarbon streams |
| US6495029B1 (en) * | 1997-08-22 | 2002-12-17 | Exxon Research And Engineering Company | Countercurrent desulfurization process for refractory organosulfur heterocycles |
-
2003
- 2003-09-15 CN CNB031340105A patent/CN1313576C/en not_active Expired - Lifetime
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4397739A (en) * | 1980-02-19 | 1983-08-09 | Institut Francais Du Petrole | Process for desulfurizing a catalytic cracking or steam cracking effluent |
| US6495029B1 (en) * | 1997-08-22 | 2002-12-17 | Exxon Research And Engineering Company | Countercurrent desulfurization process for refractory organosulfur heterocycles |
| CN1316914A (en) * | 1998-09-10 | 2001-10-10 | 催化蒸馏技术公司 | Process for simultaneous treatment and fractionation of light naphtha hydrocarbon streams |
| CN1253993A (en) * | 1998-11-18 | 2000-05-24 | 法国石油公司 | Production method of low-sulfur gasoline |
| US6334948B1 (en) * | 1998-11-18 | 2002-01-01 | Institut Francais Du Petrole | Process for producing gasoline with a low sulphur content |
| EP1031622A1 (en) * | 1999-02-24 | 2000-08-30 | Institut Francais Du Petrole | Process for the production of low sulphur gasolines |
| JP2001009856A (en) * | 1999-06-22 | 2001-01-16 | Premark Rwp Holdings Inc | Coated press surface for wear-resistant laminated body and manufacture of laminated body using same |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1597864A (en) | 2005-03-23 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US5403469A (en) | Process for producing FCC feed and middle distillate | |
| US6190533B1 (en) | Integrated hydrotreating steam cracking process for the production of olefins | |
| JP3871449B2 (en) | Hydrodesulfurization method of light oil | |
| CN101845322B (en) | A production method for reducing sulfur and olefin content in gasoline | |
| CN1325611C (en) | Process for reducing sulfur in naphtha streams | |
| US5868921A (en) | Single stage, stacked bed hydrotreating process utilizing a noble metal catalyst in the upstream bed | |
| US5364514A (en) | Hydrocarbon conversion process | |
| US7090767B2 (en) | Hydrodesulfurization of gasoline fractions | |
| CN1294240C (en) | Depth hydrogenation treatment method of faulty gasoline | |
| EP1506270B1 (en) | Multi-stage hydrodesulfurization of cracked naphtha streams with a stacked bed reactor | |
| EP0725126B1 (en) | Process for desulfurizing catalytically cracked gasoline | |
| JPH10505127A (en) | Gasoline reforming method | |
| CN101343562B (en) | Hydrodesulphurization, olefin reduction method for gasoline | |
| CN1331991C (en) | Hydrogenation and quality improvement method for reducing sulfur and olefin content of inferior gasoline | |
| JP3859235B2 (en) | Method for hydrogenating thiophene sulfur-containing hydrocarbon feedstock | |
| CN1282735C (en) | Light hydrocarbon hydrogenation method | |
| CN1313576C (en) | Process for hydrogenating treatment of foulty gasoline | |
| US20050029162A1 (en) | Producing low sulfur naphtha products through improved olefin isomerization | |
| CN1782034A (en) | Method for simultanesusly reducing sulfur and olefine content in gasoline | |
| US3420768A (en) | Middle distillate hydrogen treating processes | |
| JP6181378B2 (en) | Hydrotreating method | |
| KR100813775B1 (en) | Method for producing petrol having a low sulphur content | |
| CA2206309A1 (en) | Integrated process for the production of reformate having reduced benzene content | |
| CN1313575C (en) | Process for hydrogenating modifying faulty gasoline | |
| CN103059964B (en) | Method for producing ultra-low sulfur 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 | ||
| CX01 | Expiry of patent term |
Granted publication date: 20070502 |