CN1597858A - Process for deep desulfating of diesel oil fractional oil - Google Patents
Process for deep desulfating of diesel oil fractional oil Download PDFInfo
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- CN1597858A CN1597858A CN 03134000 CN03134000A CN1597858A CN 1597858 A CN1597858 A CN 1597858A CN 03134000 CN03134000 CN 03134000 CN 03134000 A CN03134000 A CN 03134000A CN 1597858 A CN1597858 A CN 1597858A
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Abstract
The invention discloses a method for drastically desulfating the fractionated oil of diesel oil, and the raw material of diesel oil and the hydrogen gas contact the hydrofining catalyst in the first catalyst bed to react under the conditions: hydrogen fractional pressure 2.0 MPa-8.0 MPa, temperature 320 deg.C-420 deg.C, liquid space-time speed 2 h-1-10 h-1, and hydrogen-diesel oil ratio 200-700, the effluent is not separated but directly enters in the second catalyst bed to contact hydrogen gas and hydrofining catalyst react under the conditions of: hydrogen fractional pressure 2.0 MPa-8.0MPa, 300 deg.C-390 deg.C, and liquid space-time speed 1.0 h-1-7.0h-1, the corresponding effluent is cooled and then enters in a high-pressure separator, and the separated liquid resultant enters in a fractionating system, and the hydrogen-containing gas circulates back to the reactor.
Description
Technical field
The invention belongs to the method that obtains the fuel for cleaning vehicle refined diesel oil under a kind of hydro condition, more particularly, is the method that a kind of diesel oil fraction hydrogenating deep desulfuration is produced ultra-low-sulphur diesel.
Background technology
Along with the reinforcement of environmental consciousness, for reducing vehicle exhaust to atmospheric pollution, people are to the increasingly stringent that requires of foreign matter content such as sulphur, nitrogen in the diesel oil distillate.Just diesel oil sulphur content index has been dropped to the sulfur specifications diesel oil index that is not more than 350 μ g/g in 2000 as Europe, will drop to again to sulphur content specification in 2005 and be not more than 50 μ g/g.California, USA resource management office (CARB) and U.S. environment management association (EMA) have also proposed the low-sulfur diesel-oil index of oneself.At home, metropolitan diesel oil specification also resembles the content of impurity such as further restriction sulphur Europe, the U.S., nitrogen, and the sulphur content that requires diesel product is less than 500 μ g/g.For this reason, each oil refining enterprise all will face the problem of improving diesel quality.
Adopt conventional hydrofinishing process or highly active Hydrobon catalyst, though also can reach the purpose of desulfurization, along with the intensification of the hydrogenation degree of depth, it is more and more harsher that operational conditions such as the air speed of hydrogenation unit become, to each oil refining enterprise, all be disadvantageous economically.So a main difficult point of research is how to solve the operating severity that reduces device when reducing the hydrogenated products sulphur content at present.
Existing hydrogen addition technology mostly is to adopt two reactors, remove the sulphur that more easily removes at first reactor after, try every possible means to improve the reaction environment of second reactor then, remove the sulphur content that difficulty is taken off part, reach the purpose of deep desulfuration.As increase separation system, and promptly between two reactors, increase a high-pressure separator, remove the hydrogen sulfide in first reactor product, the hydrogen purity that enters second reactor is improved, reach the purpose of deep desulfuration with this.At USP5, just introduced a kind of method of this hydrogenating desulfurization in 114,562.At least adopt two reaction zones in this method, load non-precious metal catalyst in first reaction zone, second reaction zone generally loads noble metal catalyst, and the hydrogen dividing potential drop is than the high 500kPa of first reaction zone, and temperature of reaction is lower than first reaction zone.A high temperature stripper plant is arranged, to remove the hydrogen sulfide in first reaction zone product between two reactors.Though this method can obtain the diesel product of low-sulfur, low aromatic hydrocarbons, owing to the process cost of the pressure of two reaction zones interpolation different and stripping apparatus having increased device.
Chinese patent CN 1355273A has proposed a kind of method of deeply desulfurizing fractional oil of low hydrogen consumption, and diesel raw material and hydrogen are at hydrogen dividing potential drop 2.0～8.0MPa, 320 ℃～440 ℃ of temperature, liquid hourly space velocity 2h
-1～7h
-1,, contact with Hydrobon catalyst under the condition of hydrogen to oil volume ratio 200～700, reaction effluent is 200～290 ℃, liquid hourly space velocity 4h without separation in temperature of reaction
-1～10h
-1Condition under contact with Hydrobon catalyst, the separating reaction effluent, wherein product liquid enters fractionating system, rich hydrogenous hydrogen recycle is returned reactor.The chemical hydrogen consumption of this method is low, and the sulphur content of diesel product can be reduced to below the 300 μ g/g.But if produce ultra-low-sulphur diesel (＜30 μ g/g), the desulfurization depth deficiency of this technology with it.
Summary of the invention
The objective of the invention is provides a kind of diesel fraction deep desulfurization method on the basis of existing hydrogen addition technology, with the diesel product of production super low sulfur.
Method provided by the invention is: diesel raw material contacts with Hydrobon catalyst in first beds with hydrogen, and reaction conditions is: hydrogen dividing potential drop 2.0～8.0MPa, best 3.0～6.5MPa; 320 ℃～420 ℃ of temperature, best 350 ℃～400 ℃; Liquid hourly space velocity 2h
-1～10h
-1, best 3h
-1～8h
-1Hydrogen to oil volume ratio 200～700, best 300～500.The effluent of first beds directly enters second beds without separating, and continues to contact to carry out catalyzed reaction with hydrogen and Hydrobon catalyst.Reaction conditions is: hydrogen dividing potential drop 2.0～8.0MPa, best 3.0～6.5MPa; Temperature of reaction is 300～390 ℃, best 320～360 ℃, liquid hourly space velocity 1.0h
-1～7.0h
-1, best 1.5h
-1～6.0h
-1Reaction effluent enters high-pressure separator through cooling, and isolated product liquid enters fractionating system, and hydrogen-containing gas loops back reactor after purifying.
The series connection of 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 the temperature height, air speed is big.In this bed, easily remove sulphur (being the sulphur of the more performance hydrogenolysis of reaction mechanism characteristic) by hydrogenation and removing significantly in the diesel raw material as thioether, thiophene etc.; Temperature is low, air speed is little and the reaction conditions of second bed shows as.In this bed, the difficulty in the diesel raw material removes sulphur (being the sulphur of the more performance hydrogenation of reaction mechanism characteristic, as dibenzothiophene) quilt hydrogenation and removing significantly.The temperature of reaction of two beds can adopt cold hydrogen or cold oil to circulate and control, and respectively at two reactors, also available heat exchange is controlled as if two beds.
The used Hydrobon catalyst of first beds and second beds is different, also can be identical.The catalyzer of first beds filling is a loaded catalyst, loaded metal is VIB and group VIII non-precious metal catalyst, as Co, Mo, Ni and W etc., it generally is the combination between them, preferred Co, Mo combination, metal content (in oxide compound) is at 5.0wt%～45.0wt%, preferred 15.0wt%～35.0wt%; Preferred carrier is silicon oxide, aluminum oxide, silica-alumina, silica-alumina phosphoric acid salt, titanium oxide, zirconium white, vanadium oxide and other III-th family, IV family, VA family and VI family oxide compound, and one or more the mixture in the Y zeolite.This kind catalyzer should have stronger hydrogenolysis active centre.
The catalyzer of second beds filling also is a loaded catalyst, loaded metal is VIB and group VIII non-precious metal catalyst, as Co, Mo, Ni and W etc., it generally is the combination between them, preferred Ni, Mo, W three metallic combinations, metal content (in oxide compound) is at 5.0wt%～55.0wt%, preferred 15.0wt%～45.0wt%; Preferred carrier has silicon oxide, aluminum oxide, silica-alumina, silica-alumina phosphoric acid salt, titanium oxide, zirconium white, vanadium oxide and other III-th family, IV family, VA family and VI family oxide compound, and Y zeolite equimolecular sieve, or the mixture of two or more carrier wherein.This kind catalyzer should have stronger hydrogenation sites.
When carbon residue in the diesel raw material or metal content are higher; for preventing that the beds coking from causing bed pressure drop too fast; can add a certain amount of hydrogenation protecting agent or the used hydrogenation catalyst of second beds at the Hydrobon catalyst top of first bed; also can be with being similar to the used highly active hydrogenation catalyst of second beds; its add-on is generally the 1v%～20v% of the-beds hydrogenation catalyst; normally bring into play with the catalyst activity performance that guarantees two beds, and prolong operating period.The hydrogenation protecting agent is made up of the gamma-aluminium oxide carrier with diplopore distribution of 1.0～5.0wt% nickel oxide, 5.5～10.0wt% molybdenum oxide and surplus, preferably the FZC-10 of Fushun Petrochemical Research Institute series residual hydrogenation protective material.
The invention has the advantages that: the present invention is the single hop flow process, has bigger flexibility of operation, can adjust operating parameters according to product requirement, produce the product of different sulphur content specifications, especially be used for producing ultra-low-sulphur diesel (sulphur content＜30 μ g/g), utilize existing apparatus to carry out appropriate reconstruction and can implement; And working pressure is relatively low, thereby has reduced plant investment, has reduced process cost.
The inventive method can be used for various straight-run diesel oils, catalytic cracking diesel oil, coker gas oil or its mixture.The boiling range scope of diesel raw material is 140 ℃～390 ℃, is preferably 170 ℃～370 ℃, and sulphur content is 0.1～3.0wt%.
Embodiment
Following embodiment further specifies of the present invention, and it does not limit use range of the present invention.
Embodiment 1～6
Hydrogenating desulfurization effect of the present invention is mainly investigated in test below.With the coker gas oil of middle-eastern crude and the hydrogenating desulfurization of catalytic cracking diesel oil mixing oil (weight ratio of coker gas oil and catalytic cracking diesel oil is 25: 75) is example.The raw material oil properties sees Table 1 in this test, and the catalyst system therefor physico-chemical property sees Table 2.Hydrogenation reaction is all carried out in this test on the long run test device, its processing condition and test-results see Table 3.
Table 1 stock oil main character
| Density, kg/m 3 | ????0.8692 |
| ??S，μg/g | ????10200 |
| ??N，μg/g | ????747 |
| Aromatic hydrocarbons, wt% | ????45.7 |
| Boiling range, ℃ IBP～EBP | ????156～366 |
Table 2 catalyzer physico-chemical property
| Numbering | First beds | Second beds |
| Catalytic active component | Co、Mo | ????Mo、Ni、W |
| Shape | Trifolium | Trifolium |
| Diameter, mm | 1.6 | ????1.6 |
| Specific surface area, m 2/g | 275 | ????268 |
| Pore volume, ml/g | 0.38 | ????0.35 |
| Metal component (oxide compound), wt% CoO MoO 3??NiO ??WO 3 | ? 5.3 18.6 - - | ? ????- ????20.47 ????2.07 ????7.20 |
| Carrier | Gama-alumina+5wt%USY molecular sieve | Gama-alumina+12wt% silicon oxide |
The processing condition of each embodiment of table 3 and experimental result thereof
| Embodiment | ????1 | ????2 | ????3 | ????4 | ????5 | ????6 |
| Processing condition hydrogen dividing potential drop, the MPa temperature of reaction, ℃ first bed, the second bed liquid hourly space velocity, h -1First bed, the second bed hydrogen to oil volume ratio | ? ????3.2 ? ????350 ????320 ? ????3.0 ????2.0 ????300 | ? ????3.2 ? ????360 ????320 ? ????3.0 ????2.0 ????300 | ? ????3.2 ? ????370 ????320 ? ????3.0 ????2.0 ????300 | ? ????3.2 ? ????390 ????320 ? ????4.0 ????4.0 ????300 | ? ????6.4 ? ????370 ????340 ? ????6.7 ????2.9 ????500 | ? ????6.4 ? ????370 ????340 ? ????5.0 ????2.1 ????500 |
| First bed generates oily S content, μ g/g | ????487.3 | ? ????398.9 | ? ????325.4 | ? ????383.1 | ? ????568.5 | ? ????435.7 |
| Product property S, μ g/g | ? ????38.5 | ? ????16.8 | ? ????6.5 | ? ????28.3 | ? ????43.1 | ? ????21.5 |
By experimental result as seen, the present invention is optimizing and revising under the situation of operational condition, can be used for producing ultra-low-sulphur diesel fully, can be oil refining enterprise and obtains bigger economic benefit.
Claims (12)
1, a kind of method of diesel oil distillate oil deep desulfuration is characterized in that diesel raw material contacts with Hydrobon catalyst in first beds with hydrogen, and reaction conditions is: hydrogen dividing potential drop 2.0MPa～8.0MPa, 320 ℃～420 ℃ of temperature, liquid hourly space velocity 2h
-1～10h
-1, hydrogen to oil volume ratio 200～700; The effluent of first beds directly enters second beds without separating, contact with Hydrobon catalyst with hydrogen and to carry out catalyzed reaction, reaction conditions is: hydrogen dividing potential drop 2.0MPa～8.0MPa, temperature of reaction is 300 ℃～390 ℃, liquid hourly space velocity 1.0h
-1～7.0h
-1, reaction effluent enters high-pressure separator through cooling, and isolated product liquid enters fractionating system, and hydrogen-containing gas loops back reactor after purifying.
2, in accordance with the method for claim 1, the reaction conditions that it is characterized in that first beds is: hydrogen dividing potential drop 3.0～6.5MPa; 350 ℃～400 ℃ of temperature; Liquid hourly space velocity 3h
-1～8h
-1Hydrogen to oil volume ratio 300～500.
3, in accordance with the method for claim 1, the reaction conditions that it is characterized in that second beds is: hydrogen dividing potential drop 3.0～6.5MPa; 320 ℃～360 ℃ of temperature; Liquid hourly space velocity 1.5h
-1～6.0h
-1
4, in accordance with the method for claim 1, it is characterized in that the catalyzer of first beds filling is a loaded catalyst, loaded metal is VIB and group VIII base metal, in metal oxide, accounts for 5.0%～45.0% of catalyst weight; Carrier is one or more the mixture in silicon oxide, aluminum oxide, silica-alumina, silica-alumina phosphoric acid salt, titanium oxide, zirconium white, vanadium oxide and other III-th family, IV family, VA family and VI family oxide compound and the Y zeolite.
5, in accordance with the method for claim 4, the metal that it is characterized in that load on the catalyzer of first beds filling is Co and Mo.
6, according to claim 4 or 5 described methods, it is characterized in that the non-noble metal weight of load on the catalyzer of first beds filling, in metal oxide, account for 15.0%～35.0% of catalyst weight.
7, in accordance with the method for claim 1, it is characterized in that the catalyzer of second beds filling is a loaded catalyst, loaded metal is VIB and group VIII base metal, in metal oxide, accounts for 5.0%～55.0% of catalyst weight; Carrier is one or more the mixture in silicon oxide, aluminum oxide, silica-alumina, silica-alumina phosphoric acid salt, titanium oxide, zirconium white, vanadium oxide and other III-th family, IV family, VA family and VI family oxide compound and the Y zeolite.
8, in accordance with the method for claim 7, it is characterized in that loaded metal is Ni, Mo and W on the catalyzer of second beds filling.
9, according to claim 7 or 8 described methods, it is characterized in that the amount of metal of load on the catalyzer of second beds filling, count 15.0wt%～45.0wt% with oxide compound.
10, in accordance with the method for claim 1; its feature adds hydrogenation protecting agent or the used hydrogenation catalyst of second beds at the Hydrobon catalyst top of first bed, and its add-on is the 1v%～20v% of the first beds Hydrobon catalyst.
11, in accordance with the method for claim 10, it is characterized in that the hydrogenation protecting agent is made up of the gamma-aluminium oxide carrier that diplopore distributes that has of 1.0wt%～5.0wt% nickel oxide, 5.5wt%～10.0wt% molybdenum oxide and surplus.
12, in accordance with the method for claim 1, it is characterized in that diesel raw material is straight-run diesel oil, catalytic cracking diesel oil, coker gas oil or its mixture.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB031340008A CN1313573C (en) | 2003-09-15 | 2003-09-15 | Process for deep desulfating of diesel oil fractional oil |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB031340008A CN1313573C (en) | 2003-09-15 | 2003-09-15 | Process for deep desulfating of diesel oil fractional oil |
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| Publication Number | Publication Date |
|---|---|
| CN1597858A true CN1597858A (en) | 2005-03-23 |
| CN1313573C CN1313573C (en) | 2007-05-02 |
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|---|---|---|---|
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100448951C (en) * | 2005-08-09 | 2009-01-07 | 中国石油化工股份有限公司 | Method of producing catalytic reforming raw material |
| CN101942330A (en) * | 2009-07-09 | 2011-01-12 | 中国石油化工股份有限公司抚顺石油化工研究院 | Method for deep hydrogenation, sulfur removal and aromatics removal of diesel oil |
| CN102041063A (en) * | 2009-10-21 | 2011-05-04 | 中国石油化工股份有限公司 | Method for carrying out deep hydrogenation and desulfurization on diesel |
| CN101092573B (en) * | 2006-06-22 | 2011-08-10 | 中国石油化工股份有限公司 | A hydrogenation method for producing diesel oil in low sulphur |
| CN103215069A (en) * | 2013-03-29 | 2013-07-24 | 中国海洋石油总公司 | Method for producing clean diesel by hydro-upgrading inferior distillate oil |
| CN105542850A (en) * | 2014-10-28 | 2016-05-04 | 中国石油化工股份有限公司 | Method for producing ultra low sulfur diesel oil through hydrorefining |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5114562A (en) * | 1990-08-03 | 1992-05-19 | Uop | Two-stage hydrodesulfurization and hydrogenation process for distillate hydrocarbons |
| FR2757532B1 (en) * | 1996-12-20 | 1999-02-19 | Inst Francais Du Petrole | PROCESS FOR THE CONVERSION OF A GAS CUT TO PRODUCE FUEL WITH A HIGH INDEX OF CETANE, DESAROMATISED AND DESULPHURIZED |
| US6582590B1 (en) * | 1997-07-15 | 2003-06-24 | Exxonmobil Research And Engineering Company | Multistage hydroprocessing using bulk multimetallic catalyst |
| CN1119395C (en) * | 1999-03-19 | 2003-08-27 | 中国石油化工集团公司 | Two-stage fraction oil hydrogenating and arene eliminating process |
| CN1115387C (en) * | 2000-11-28 | 2003-07-23 | 中国石油化工股份有限公司 | Process for deeply desulfurizing fractional oil with low hydrogen consumption |
| US6447673B1 (en) * | 2001-03-12 | 2002-09-10 | Fina Technology, Inc. | Hydrofining process |
| CN1173012C (en) * | 2001-10-30 | 2004-10-27 | 中国石油化工股份有限公司 | Method of desulfurizing and dearomatizing diesel oil deeply |
-
2003
- 2003-09-15 CN CNB031340008A patent/CN1313573C/en not_active Expired - Lifetime
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100448951C (en) * | 2005-08-09 | 2009-01-07 | 中国石油化工股份有限公司 | Method of producing catalytic reforming raw material |
| CN101092573B (en) * | 2006-06-22 | 2011-08-10 | 中国石油化工股份有限公司 | A hydrogenation method for producing diesel oil in low sulphur |
| CN101942330A (en) * | 2009-07-09 | 2011-01-12 | 中国石油化工股份有限公司抚顺石油化工研究院 | Method for deep hydrogenation, sulfur removal and aromatics removal of diesel oil |
| CN101942330B (en) * | 2009-07-09 | 2013-06-19 | 中国石油化工股份有限公司 | Method for deep hydrogenation, sulfur removal and aromatics removal of diesel oil |
| CN102041063A (en) * | 2009-10-21 | 2011-05-04 | 中国石油化工股份有限公司 | Method for carrying out deep hydrogenation and desulfurization on diesel |
| CN102041063B (en) * | 2009-10-21 | 2015-12-09 | 中国石油化工股份有限公司 | The method of deep hydrodesulfurizationof of diesel oil |
| CN103215069A (en) * | 2013-03-29 | 2013-07-24 | 中国海洋石油总公司 | Method for producing clean diesel by hydro-upgrading inferior distillate oil |
| CN105542850A (en) * | 2014-10-28 | 2016-05-04 | 中国石油化工股份有限公司 | Method for producing ultra low sulfur diesel oil through hydrorefining |
| CN105542850B (en) * | 2014-10-28 | 2017-05-24 | 中国石油化工股份有限公司 | Method for producing ultra low sulfur diesel oil through hydrorefining |
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| CN1313573C (en) | 2007-05-02 |
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