CN1597863A - Process for hydrogenating modifying faulty gasoline - Google Patents
Process for hydrogenating modifying faulty gasoline Download PDFInfo
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- CN1597863A CN1597863A CN 03133990 CN03133990A CN1597863A CN 1597863 A CN1597863 A CN 1597863A CN 03133990 CN03133990 CN 03133990 CN 03133990 A CN03133990 A CN 03133990A CN 1597863 A CN1597863 A CN 1597863A
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Abstract
The invention discloses a bad gasoline hydrogenated-modifying method, and the hydrogenation includes two catalyst beds, firstly separating the bad gasoline fraction into light and heavy components, where the heavy component and the hydrogen gas contact with the hydrofining catalyst in the first catalyst bed to make hydrodesulfation reaction, and the effluent is not separated and then mixes with the light component to directly enter in the second catalyst bed, so as to contact with the hydrogenated-modifying catalyst to make hydrogenation reaction, and the corresponding effluent enters in a high-pressure separator to make gas-liquid separation, the liquid phase acts as gasoline product and the hydrogen-rich gas is purified and then returns to the reacting system.
Description
Technical field
The present invention relates to a kind of hydrotreating process for light hydrocarbons, relate to the hydrogenation modification method 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.
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 hydrogenation modifying process, the degree that this technology can make the inferior patrol desulfurization, fall alkene is higher, and does not reduce the gasoline fraction octane value.
In the inventive method, hydrotreatment comprises two beds, and its step is as follows:
A, the inferior patrol cut is divided into light constituent and heavy constituent;
B, isolated gasoline reform divide to contact with Hydrobon catalyst in first beds with hydrogen and carry out hydrodesulfurization reaction;
The effluent of C, first beds does not separate, and directly enters second beds again with after isolated light constituent mixes, and contacts with catalyst for hydro-upgrading and carries out hydrogenation reaction;
The effluent of D, second beds enters high-pressure separator and carries out gas-liquid separation, and liquid phase is directly done gasoline products, and hydrogen-rich gas is Returning reacting system after purifying then.
In the steps A, the cut point of light constituent and heavy constituent is generally by the content decision of the alkene of stock oil and sulphur, and the temperature that 95% of general isolated light constituent boiling range distillates a little is 95 ℃～135 ℃.
The first beds hydrodesulfurization process described in the step B can adopt conventional hydrofining, preferably adopts Mo-Co or Mo-Ni/ aluminium oxide catalyst, and operates under the conventional hydrofining technology condition.Reaction conditions is preferably: reaction pressure 1.0MPa～4.0MPa, 240 ℃～360 ℃ of temperature of reaction, liquid hourly space velocity 1.0h
-1～10.0h
-1With hydrogen to oil volume ratio 100～500.
The catalyst for hydro-upgrading of second beds described in the step C, its carrier are Al
2O
3, halogen-containing Al
2O
3, one or more in SAPO-11, ZSM-12, ZSM-35, MCM-22, MCM-41, ZSM-5 molecular sieve, ZSM-5 molecular sieve with small crystal grains, HBeta zeolite, the y-type zeolite; So-called fine grain ZSM-5 type molecular sieve 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 transiting state metals such as Co, Mo, Ni and W, also can be in the precious metals such as Pt, Re, Ir one or more, perhaps while carried noble metal and base metal.Loading for transiting state metals such as Co, Mo, Ni and W is generally 0.5wt%～20.0wt% by oxide compound, preferred 1.0wt%～15.0wt%.This kind catalyzer should have stronger isomery, cyclisation (comprising aromizing) function.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.
First beds and second beds can be in same fixed-bed reactor, also can be in two different fixed-bed reactor.First beds mainly is the desulfurization of carrying out gasoline stocks, and second beds mainly is to guarantee not reducing of octane value.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.
The present invention is applicable to the various types of gasoline fractions 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.
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 method of hydrotreating of the present invention of this test.With gasoline desulfur, alkene falls, octane value recovering is an example.Raw materials used oil nature 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, and embodiment sees Table 3.
Table 1 stock oil main character
| Cut | Full cut | Light constituent | |||
| Light constituent cut point/T95/ ℃ | ????95 | ????110 | ????120 | ????135 | |
| Density, g/cm 3 | ????0.732 | ????0.67 | ????0.6712 | ????0.675 | ????0.681 |
| ??S，μg/g | ????1635 | ????260 | ????280 | ????301 | ????453 |
| Alkene, v% | ????52.9 | ????74.0 | ????64.9 | ????52.3 | ????40.9 |
| ??RON | ????93.8 | ????95.6 | ????95.3 | ????94.8 | ????94.3 |
| Boiling range, ℃ 5%～95% | ????52～185 | ||||
Table 2 catalyzer physico-chemical property
| Heterogeneous catalyst | Hydrobon catalyst | |
| Catalytic active component | ????Ni | ??Mo、Co |
| Shape | Stripe shape | Bar shaped |
| Diameter, mm | ????2.15 | ??1.9 |
| Specific surface area, m 2/g | ????454.4 | ??198 |
| Pore volume, ml/g | ????0.383 | ??0.38 |
| 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 |
| Light constituent cut point/T95/ ℃ | ????120 | ????120 | ????120 |
| Full distillate oil character S, μ g/g alkene, v% RON loss | ? ????94 ????27.1 ????-0.9 | ? ????52 ????23.5 ????-1.5 | ? ????30 ????19.7 ????-2.1 |
Continuous table-2 embodiment experimental results
| Embodiment | ????4 | ????5 | ????6 |
| Operational condition reaction pressure/MPa temperature of reaction/℃ first beds, second beds air speed/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 | ? ????4.3 ????14.5 ????0.2 | ? ????35 ????21.3 ????-1.7 | ? ????29 ????27.6 ????-1.9 |
Claims (10)
1, a kind of inferior patrol hydrogenation modification method, wherein hydrotreatment comprises two beds, step is as follows:
A, the inferior patrol cut is divided into light constituent and heavy constituent;
Isolated gasoline reform is divided to contact with Hydrobon catalyst in first beds with hydrogen and is carried out hydrodesulfurization reaction in B, the steps A;
The effluent of C, first beds does not separate, and directly enters second beds again with after isolated light constituent mixes, and contacts with catalyst for hydro-upgrading and reacts;
The reacted effluent of D, step C enters high-pressure separator and carries out gas-liquid separation, and liquid phase is made gasoline products, and hydrogen-rich gas is Returning reacting system after purifying then.
2, in accordance with the method for claim 1, it is characterized in that separating of light constituent described in the steps A and heavy constituent, the temperature that 95% of isolated light constituent boiling range distillates a little is 95 ℃～135 ℃.
3, in accordance with the method for claim 1, it is characterized in that the used Hydrobon catalyst of first beds described in the step B is Mo-Co/ aluminum oxide, Mo-Ni/ aluminum oxide or W-Mo-Ni/ aluminum oxide.
4, in accordance with the method for claim 1, it is characterized in that the hydrofining technology condition described in the step B is: reaction pressure 1.0MPa～4.0MPa, 240 ℃～360 ℃ of temperature of reaction, liquid hourly space velocity 1.0h
-1～10.0h
-1With hydrogen to oil volume ratio 100～500.
5, in accordance with the method for claim 1, it is characterized in that the catalyst for hydro-upgrading of second beds described in the step C, its carrier is Al
2O
3, halogen-containing Al
2O
3, in SAPO-11, ZSM-12, ZSM-35, MCM-22, MCM-41, ZSM-5 molecular sieve, ZSM-5 molecular sieve with small crystal grains, HBeta zeolite and the y-type zeolite one or more; Loaded metal is one or more among Co, Mo, Ni, W, Pt, Re and the Ir.
6, in accordance with the method for claim 1, the catalyst for hydro-upgrading that it is characterized in that second beds described in the step C, loaded metal is one or more among Co, Mo, Ni and the W, and by the metal oxide compound, its total content is 0.5wt%～20.0wt%.
7,, it is characterized in that the catalyst for hydro-upgrading of described second beds can add TiO according to claim 5 or 6 described methods
2, SiO
2, ZrO
2, Al
2O
3With in the rare-earth oxide one or more.
8, in accordance with the method for claim 1, the reaction conditions that it is characterized in that second beds described in the step C is: hydrogen dividing potential drop 0.5～5.0MPa; 320 ℃～450 ℃ of temperature; Liquid hourly space velocity 1.0h
-1～15.0h
-1Hydrogen-oil ratio 100～800.
9, in accordance with the method for claim 1, it is characterized in that the reaction conditions of second beds described in the step C is: hydrogen dividing potential drop 1.0～4.0MPa, 350 ℃～435 ℃ of temperature, liquid hourly space velocity 1.0h
-1～10.0h
-1, hydrogen to oil volume ratio 300～800.
10, in accordance with the method for claim 1, it is characterized in that inferior patrol is straight-run spirit, catalytically cracked gasoline, coker gasoline or their mixture.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB031339905A CN1313575C (en) | 2003-09-15 | 2003-09-15 | Process for hydrogenating modifying faulty gasoline |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB031339905A CN1313575C (en) | 2003-09-15 | 2003-09-15 | Process for hydrogenating modifying faulty gasoline |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1597863A true CN1597863A (en) | 2005-03-23 |
| CN1313575C CN1313575C (en) | 2007-05-02 |
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ID=34658935
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB031339905A Expired - Lifetime CN1313575C (en) | 2003-09-15 | 2003-09-15 | Process for hydrogenating modifying faulty gasoline |
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|---|---|
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN101376827B (en) * | 2007-08-27 | 2012-04-04 | 中国石油化工股份有限公司 | Mixed hydrogenation technological process for coker gasoline and once run kerosene |
| CN104560164A (en) * | 2013-10-29 | 2015-04-29 | 中国石油化工股份有限公司 | Hydro-upgrading method for producing high-octane gasoline component or BTX raw material |
| CN106929099B (en) * | 2015-12-30 | 2018-10-16 | 中国石油天然气股份有限公司 | A kind of method of inferior patrol hydro-upgrading |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2476118B1 (en) * | 1980-02-19 | 1987-03-20 | Inst Francais Du Petrole | PROCESS FOR DESULFURIZING A CATALYTIC CRACKING OR STEAM CRACKING EFFLUENT |
| US6656329B1 (en) * | 1996-08-28 | 2003-12-02 | Premark Rwp Holdings, Inc. | Coated pressing surfaces for abrasion resistant laminate and making laminates therefrom |
| US6083378A (en) * | 1998-09-10 | 2000-07-04 | Catalytic Distillation Technologies | Process for the simultaneous treatment and fractionation of light naphtha hydrocarbon streams |
| FR2785908B1 (en) * | 1998-11-18 | 2005-12-16 | Inst Francais Du Petrole | PROCESS FOR PRODUCING LOW SULFUR CONTENT |
| FR2790000B1 (en) * | 1999-02-24 | 2001-04-13 | Inst Francais Du Petrole | PROCESS FOR PRODUCING LOW SULFUR ESSENCE |
-
2003
- 2003-09-15 CN CNB031339905A patent/CN1313575C/en not_active Expired - Lifetime
Cited By (5)
| 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 technological process for coker gasoline and once 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 |
| CN104560164A (en) * | 2013-10-29 | 2015-04-29 | 中国石油化工股份有限公司 | Hydro-upgrading method for producing high-octane gasoline component or BTX raw material |
| CN104560164B (en) * | 2013-10-29 | 2016-10-19 | 中国石油化工股份有限公司 | A kind of hydrogenation modification method producing high octane gasoline component or BTX raw material |
| CN106929099B (en) * | 2015-12-30 | 2018-10-16 | 中国石油天然气股份有限公司 | A kind of method of inferior patrol hydro-upgrading |
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| Publication number | Publication date |
|---|---|
| CN1313575C (en) | 2007-05-02 |
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