CN103059978B - Single-stage series diesel oil hydrofining method - Google Patents
Single-stage series diesel oil hydrofining method Download PDFInfo
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- CN103059978B CN103059978B CN201110321333.0A CN201110321333A CN103059978B CN 103059978 B CN103059978 B CN 103059978B CN 201110321333 A CN201110321333 A CN 201110321333A CN 103059978 B CN103059978 B CN 103059978B
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Abstract
The invention discloses a hydrofining method. The method consists of: mixing diesel oil with hydrogen, introducing the mixed gas into a first reactor, leaving the mixed gas and a hydrofining catalyst to undergo a contact reaction under a low temperature and a high space velocity, with the catalyst taking metal Mo and Co as active components, and having an average pore size of 20-40 angstroms and a total acid amount of 0.2-1.0mmol/g; and leaving the effluent of a first reactor to enter a second reactor, letting the effluent and a hydrofining catalyst to undergo a contact reaction under a high temperature and a low space velocity, with the catalyst taking metal W and/or Mo and Ni as active components, and having an average pore size of 40-70 angstroms and a total acid amount of 1.0-3.0mmol/g. The method employs appropriate catalysts according to different reaction types, and is in favor of lowering the catalyst cost without influencing reaction activity. The method provided in the invention can be used for producing diesel oil with a sulfur content of less than 50 micrograms/g.
Description
Technical field
The present invention relates to a kind of hydrocarbon hdyrotreating method, specifically a kind of single hop series connection diesel oil hydrofining method being applicable to production ultra-low-sulphur diesel.
Background technology
Along with the raising of people's environmental consciousness and the increasingly stringent of environmental regulation, produce and use fuel for cleaning vehicle more and more to become a kind of development trend.The exploitation of deep hydrodesulfurizationof of diesel oil technology then becomes the focus of research at present.At present, most Diesel Oil Hydrofining Unit operating process is that stock oil is by same refined diesel oil, reaction product heat exchange, and be heated to enter hydrofining reactor after reaction requires temperature through process furnace, this is a kind of hydrogenation flow process of routine, its advantage is easy to operate, but ultra-low-sulphur diesel is produced, its temperature of reactor and Hydrogen distribution are very unreasonable, because industrial diesel oil hydrogenator belongs to adiabatic reactor, reactor catalyst bed also exists larger axial temperature difference (the deep hydrodesulfurizationof reactor bed temperature difference is larger), often entrance feeding temperature is lower, and need to inject cold hydrogen in reactor to control reactor outlet temperature.Remove dibenzothiophene due to ultra-low-sulphur diesel need of production and contain sterically hindered dibenzothiophene class sulfide, as 4, 6-DMDBT, and this part sulfide reacts hardly under temperature of reaction is lower than 320 DEG C of conditions, therefore, cryogenic reaction zone is for 4, removing of 6-DMDBT is inoperative, and for simple sulfide as mercaptan, thioether, thiophene and simple dibenzothiophene, can remove rapidly under lower temperature of reaction and higher volume space velocity, but dependence reaction heat just enters high temperature reaction zone after naturally heating up and needing to arrive reactor middle and lower part in traditional single reactor bed, low temperature reaction conversion zone is long, simple sulfide in cold zone is removed completely and cannot proceed 4, 6-DMDBT removes, reduce the service efficiency of cryogenic reaction zone catalyzer.Therefore, under the condition that cumulative volume air speed is certain, be equivalent to increase high temperature section volume space velocity, be unfavorable for the performance of monolith performance.Simultaneously a large amount of cold hydrogen uses and too increases device hydrogen consumption, energy consumption.
Summary of the invention
For the deficiency of existing diesel oil hydrofining reaction process, the invention provides a kind of single hop series connection diesel hydrogenation process.The investment of this process unit is little, and energy consumption reduces, and may be used for producing ultra-low-sulphur diesel.
Bavin hydrogenation method of the present invention comprises following content:
(1) diesel raw material and hydrogen in the first hydrogenator with Hydrobon catalyst contact reacts, to remove the simple impurity such as sulphur, nitrogen in diesel oil distillate; Reaction conditions is: temperature of reaction 220 DEG C ~ 320 DEG C, reaction pressure 3.0MPa ~ 10.0MPa, volume space velocity 1.0h during liquid
-1~ 10.0h
-1, hydrogen to oil volume ratio 100 ~ 1000; Wherein said Hydrobon catalyst is with metal M o and Co for active ingredient, and catalyzer mean pore size is 20 ~ 40 dusts, and total acid content is 0.2 ~ 1.0mmol/g;
(2) first hydrofining reactor effluents enter the second hydrogenator without separation, contact with hydrogen, Hydrobon catalyst; Reaction conditions is, temperature of reaction 330 DEG C ~ 400 DEG C, reaction pressure 3.0MPa ~ 10.0MPa, volume space velocity 0.5h during liquid
-1~ 6.0h
-1, hydrogen to oil volume ratio 200 ~ 2000; Described Hydrobon catalyst with metal W and/or Mo and Ni for active ingredient, mean pore size 40 ~ 70 dust, total acid content 1.0 ~ 3.0mmol/g;
(3) second hydrofining reactor effluents enter cold high pressure separator after cooling, and isolated product liquid enters fractionating system, and gas is through purifying, and hydrogen-rich gas loops back reactor.
According to single hop of the present invention series connection diesel oil hydrofining method, in step (2) the first hydrofining reactor effluent before entering the second hydrofining reactor first through process furnace.In step (3), the second hydrofining reactor effluent is after realizing cooling with the mixture heat exchange of diesel raw material or diesel raw material and hydrogen, then enters cold high pressure separator.
In diesel oil hydrofining method of the present invention, participate in the different of compound of reaction for the first hydrofining reactor from the second hydrofining reactor, in the first hydrofining reactor and the second hydrofining reactor, load dissimilar catalyzer.Because in the first hydrofining reactor, reaction conditions comparatively relaxes, mainly carry out simple sulphur, nitrogen compound hydrogenation and removing reaction and olefin saturation, complicated macromole sulphur, nitrogen compound are difficult to react, therefore, the catalyzer of the suitable small molecules turnover reaction using aperture less in the first hydrofining reactor targetedly, this reduces the complicated sulphur of macromole, nitrogen compound invalid stop on a catalyst, improve the service efficiency of the first catalyst in reactor.Meanwhile, higher for reactant reaction activity in the first reactor, use active relatively low Hydrobon catalyst at the first hydrofining reactor.The chemical reaction mainly carried out in second reactor is the reaction of complicated sulphur, the hydrofining reaction of nitrogen compound and aromatic saturation, consider complicated sulphur, nitrogen compound especially 4, removing of 6 dibenzothiophene class sulfide containing substituent steric hindrance of having living space requires higher to catalyst hydrogenation activity and isomerism ability, therefore, the body phase method catalyzer of the Mo-Ni type Hydrobon catalyst that the second reactor use hydrogenation activity is higher or high metal content, suitably can improve the acidity of support of the catalyst simultaneously.So both being conducive to reaction to carry out, simultaneously because an anti-Effect of Pretreatment reduces the easily coking material such as alkene, diolefine in raw material, because this reducing the coking soot level of two anti-peracidity catalyzer, extending catalyzer work-ing life.
The consumption of the first reactor and the second reactor catalyst can require according to raw material oil properties and quality product and catalyst property is specifically determined.Usual first reactor catalyst consumption is less than the second reactor catalyst consumption, and general volume ratio is 1: 2 ~ 1: 10, and preferably 1: 4 ~ 1: 8.
First hydrofining reactor generally reacts under low temperature, high-speed, and the second hydrofining reactor then reacts under high temperature, low-speed.High temperature described herein, low temperature and high-speed and low-speed are relative.In the present invention, the liquid hourly space velocity of the second hydrofining reactor will lower than the first hydrofining reactor, and the temperature of reaction of the second hydrofining reactor is then higher than the first hydrofining reactor.The operational condition of general first reactor is as follows: temperature of reaction 220 DEG C ~ 320 DEG C, preferably 240 DEG C ~ 300 DEG C, reaction pressure 3.0MPa ~ 10.0MPa, preferred 4.0MPa ~ 8.0MPa, volume space velocity 1.0h during liquid
-1~ 10.0h
-1, preferred 4h
-1~ 8.0h
-1, hydrogen to oil volume ratio 100 ~ 1000, preferably 200 ~ 800.
The operational condition of the second reactor is as follows: temperature of reaction 330 DEG C ~ 400 DEG C, preferably 340 DEG C ~ 380 DEG C, reaction pressure 3.0MPa ~ 10.0MPa, preferred 4.0MPa ~ 8.0MPa, volume space velocity 0.5h during liquid
-1~ 6.0h
-1, preferred 1.0h
-1~ 3.0h
-1, hydrogen to oil volume ratio 200 ~ 2000, preferably 400 ~ 1000.
In diesel oil hydrofining method of the present invention, the diesel raw material described in step (1) can be straight-run diesel oil, secondary processing diesel oil or their parallel feeding, the mixing oil of preferred secondary processing diesel oil or secondary processing diesel oil and straight-run diesel oil.
Larger problem is there is in conventional diesel hydrofining single hop single reactor technique when carrying out ultra-low-sulphur diesel and producing.When reactor inlet temperature arranges too low, due in reactor without external heat source heat supply, rely on separately exothermic heat of reaction to heat up, in reactor, cold zone scope is excessive, remove completely at simple sulfide, reaction is still in cold zone, cannot complete removing of complicated sulfide further.Therefore, the cold zone catalyzer of this part surplus is difficult to play its effect.And when reactor inlet temperature arranges too high, adding plant energy consumption on the one hand, the design of single hop single reactor makes diesel oil hydrogenation exothermic heat of reaction all concentrate in a reactor on the other hand, makes temperature out too high, is unfavorable for device long-term operation.Therefore, often in the middle of the bed liquid hydrogen injection to reduce temperature out.At this moment, compared with single hop tandem process, the heat release of simple sulfide reaction serves negative effect, and device hydrogen consumption, energy consumption are higher.
In diesel oil hydrofining method of the present invention, in low-temp reaction device, diesel oil reacts under high-speed, low temperature, mainly removes the simple sulfide of structure, nitride.Because temperature of reaction is lower, therefore, without the need to process furnace heating, the entrance temperature of reaction that can reach the requirement of low-temp reaction device with the second hydrofining reactor effluent heat exchange is only needed; Simultaneously, the feed volume air speed in low-temp reaction device can be designed according to feedstock property, make low-temp reaction device meet remove the prerequisite of simple sulfide and nitride under, the catalyst volume taken minimizes, and takes full advantage of simple sulfide, feature that nitride can react under low temperature, high-speed.Low-temp reaction device reaction effluent enters high-temperature reactor after mixing with circulating hydrogen and new hydrogen after process furnace heating and carries out deep desulfuration, denitrification reaction.The Heat of Formation of simple sulfide in low-temp reaction device, nitride reaction can be made full use of after high-temperature reactor being positioned over low-temp reaction device, reduce process furnace load, according to two anti-reaction depth requirement and feedstock properties, the second reactor reaction temperature can also be adjusted flexibly after process furnace is placed on low-temp reaction device.Simultaneously, low-temp reaction heat is separated with high-temperature reaction heat, while utilizing low-temp reaction heat, avoid low-temp reaction heat and high-temperature reaction heat superposing in same reactor, and bed temperature rise also comparatively single reactor bed overall temperature rise decline in high-temperature reactor, the even inactive cold hydrogen of usage quantity of cold hydrogen can be reduced, reduce hydrogen consumption, energy consumption.
Compared with conventional diesel hydrofining single reactor technique, single hop serial hydrogenation technique of the present invention has carried out rational distribution to reaction Heat of Formation, reactive system heat, temperature distribution are more reasonable, energy consumption, hydrogen consumption is lower, catalyst activity is played more fully, and under the same terms, the hydrofining degree of depth is darker.
In addition, according to difference that is anti-, two anti-reaction types, have for the catalyzer that adapts of constituency more can play the speciality of different characteristics catalyzer, good grating result of use can be obtained, simultaneously, high and low metals content catalysts collocation is conducive to reducing catalyzer cost while being used in and not affecting reactive behavior.
Accompanying drawing explanation
Fig. 1 is the principle process schematic diagram of diesel hydrogenation process of the present invention.
Embodiment
Below in conjunction with Fig. 1, diesel hydrogenation method of the present invention is described in detail.
As shown in Figure 1, fresh diesel feed and reactor 6 effluent are after interchanger 7 place's heat exchange, after pipeline 1 mixes with the recycle hydrogen introduced through pipeline 16, enter hydrofining reactor 3 carry out hydrofining reaction and remove simple sulfide, reactor 3 effluent enters in high-temperature reactor 6 and carries out deep hydrofinishing reaction after process furnace 4 heats after pipeline 5 mixes with the hydrogen introduced through pipeline 15, high-temperature reactor 6 effluent with enter through pipeline 8 after raw material heat exchange that gas-liquid separator 9 carries out gas, liquid is separated.After being separated, vapor phase stream effluent enters through pipeline 11 and mixes a part through pipeline 13 with the new hydrogen introduced through pipeline 14 after de-hydrogen sulfide column 12 removes hydrogen sulfide and enter high-temperature reactor 6, and another part enters reactor 3.Liquid phase part goes out device as hydrogenated products through pipeline 10.
In diesel hydrogenation process of the present invention, the Hydrobon catalyst of employing can be the non-noble metal hydrogenation catalyst with hydrogenating desulfurization, hydrodenitrification and aromatic saturation function, and the function of catalyzer can stress some aspect.This non-precious metal catalyst generally exists with oxidation states, needs before use to carry out prevulcanized, makes non-noble metal oxide be converted into sulfide and just have reactive behavior.Therefore, non-precious metal catalyst in use will keep sulphided state.
Catalyzer wherein in the first reactor with metal M o and Co for active ingredient, with aluminum oxide or silicon-containing alumina for carrier.With the weight of catalyzer for benchmark, molybdenum take oxide basis as 8wt% ~ 17wt%, and cobalt take oxide basis as 2wt% ~ 7wt%.Total acid content 0.2 ~ 1.0 mmol/g of catalyzer, strong acid content 0.02 ~ 0.08mmol/g; Its physical properties is generally as follows: specific surface area is 100 ~ 650 m
2/ g, pore volume is 0.15 ~ 0.8 mL/g, mean pore size 20 ~ 40 dust.
The catalyzer selected of second reactor with metal W and/or Mo and Ni for active ingredient, with aluminum oxide or silicon-containing alumina for carrier.With the weight of catalyzer for benchmark, W and/or Mo take oxide basis as 20wt% ~ 30wt%, Ni take oxide basis as 4wt% ~ 8wt%; Total acid content 1.0 ~ 3.0mmol/g, strong acid content 0.1 ~ 0.5mmol/g; Its physical properties is generally as follows: specific surface area is 100 ~ 650m
2/ g, pore volume is 0.15 ~ 0.8mL/g, mean pore size 40 ~ 70 dust.
The present invention one anti-low temperature hydrogenation refining reaction device hydrogenation catalyst used adopts and is suitable for the small-bore of simple sulphur, nitrogen compound and olefin removal reaction, the desulphurizing activated stronger Mo-Co type diesel oil hydrofining catalyst of direct hydrogenolysis of low-metal content.What two anti-high-temperature reactors adopted the comparatively strong and heterogeneous activity of high hydrogenation activity has stronger catalyzer, and the acid amount of this kind of catalyzer is higher, and active metal selects Mo-Ni type, W-Ni type or W-Mo-Ni type, while catalyzer metal content also higher.
Below by specific embodiment and comparative example, technical scheme of the present invention and effect are described.
embodiment 1 ~ 4
Embodiment 1 ~ 4 adopts the flow process shown in Fig. 1 of the present invention.Use the composition of catalyzer and character in table 1 in following examples.Feedstock property used is in table 2, and embodiment 1 ~ 4 processing condition used list in table 3.The evaluation result of embodiment 1 ~ 4 is in table 5.
The composition of table 1 embodiment used catalyst and main character
| Project | One anti-finishing agent | Two anti-finishing agents |
| Chemical constitution, quality % | ||
| MoO 3 | 14.2 | 6.2 |
| NiO | — | 20.3 |
| CoO | 3.5 | — |
| Carrier | Silicon-containing alumina | Silicon-containing alumina |
| Physical properties | ||
| Mean pore size, dust | 36 | 55 |
| Acid amount, mmol/g | 0.8 | 1.5 |
| Strong acid content, mmol/g | 0.04 | 0.18 |
Table 2 stock oil character
| Project | Stock oil |
| Density (20 DEG C), g/cm 3 | 0.8632 |
| Boiling range, DEG C | 199～375 |
| Sulphur content, μ g/g | 12000 |
| Nitrogen content, μ g/g | 406 |
comparative example 1 ~ 2
Comparative example 1 ~ 2 adopts old process: fresh feed is heated through process furnace after mixing hydrogen, then, enter hydrofining reactor and carry out hydrofining reaction, reaction effluent carries out gas, liquid is separated, use as recycle hydrogen after gas phase depriving hydrogen sulphide after being separated, liquid phase goes out device as diesel product.
Stock oil is identical with embodiment, and Hydrobon catalyst selects two anticatalyzers in embodiment.The operational condition of comparative example 1 and 2 is respectively with embodiment 1 and 2, and list in table 4, experimental result is listed in table 5.
Table 3 embodiment operational condition
| Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | |
| Low-temp reaction device | ||||
| Temperature of reaction, DEG C | 260 | 280 | 260 | 280 |
| Reaction pressure, MPa | 6.0 | 6.0 | 8.0 | 8.0 |
| Volume space velocity, h -1 | 6.0 | 6.0 | 5.0 | 5.0 |
| Hydrogen to oil volume ratio | 200 | 200 | 100 | 100 |
| High-temperature reactor | ||||
| Temperature of reaction, DEG C | 360 | 360 | 350 | 350 |
| Reaction pressure, MPa | 6.0 | 6.0 | 8.0 | 8.0 |
| Volume space velocity, h -1 | 2.0 | 1.5 | 2.0 | 1.5 |
| Hydrogen to oil volume ratio | 500 | 500 | 400 | 400 |
Table 4 comparative example operational condition
| Comparative example 1 | Comparative example 2 | |
| Temperature of reaction, DEG C | 335 | 344 |
| Reaction pressure, MPa | 6.0 | 6.0 |
| Volume space velocity, h -1 | 1.5 | 1.2 |
| Hydrogen to oil volume ratio | 500 | 500 |
Note: the temperature of reaction in comparative example 1 and 2 is average reaction temperature, and identical with the average reaction temperature of 2 with embodiment 1.Comparative example 1 is identical with the average-volume air speed in embodiment 1 and 2 respectively with the feed volume air speed of 2.
Table 5 evaluation result
| Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | Comparative example 1 | Comparative example 2 | |
| Sulphur content, μ g/g | 45 | 8 | 52 | 12 | 55 | 18 |
| Nitrogen content, μ g/g | 5 | <1 | 7 | <1 | 12 | 4 |
As can be seen from Table 5, comparative example 1 and 2 is under employing and embodiment 1 and 2 same reaction charging and same reaction conditions, during the high metals content catalysts selecting embodiment high-temperature reactor used, comparative example 1,2 generates oily sulphur, nitrogen content still higher than embodiment 1 and 2.This illustrates while reduction hydrogen consumption, energy consumption, diesel oil hydrogenation technical process of the present invention is by reasonably allotment temperature of reactor distribution, simultaneously, for the difference of reaction type in different zones, select applicable catalyzer targetedly, the better like this activity playing Hydrobon catalyst, reaction effect is better.And embodiment catalyzer cost will be invested lower than the catalyzer of the whole high metal content of comparative example in investment.
Claims (10)
1. a single hop series connection diesel hydrogenation process, comprises following content:
(1) diesel raw material and hydrogen in the first hydrogenator with Hydrobon catalyst contact reacts, reaction conditions is: temperature of reaction 220 DEG C ~ 320 DEG C, reaction pressure 3.0MPa ~ 10.0MPa, volume space velocity 1.0h during liquid
-1~ 10.0h
-1, hydrogen to oil volume ratio 100 ~ 1000; Wherein said Hydrobon catalyst is with metal M o and Co for active ingredient, and catalyzer mean pore size is 20 ~ 40 dusts, and total acid content is 0.2 ~ 1.0mmol/g;
(2) first hydrogenator effluents enter the second hydrogenator without separation, contact with hydrogen, Hydrobon catalyst; Reaction conditions is, temperature of reaction 330 DEG C ~ 400 DEG C, reaction pressure 3.0MPa ~ 10.0MPa, volume space velocity 0.5h during liquid
-1~ 6.0h
-1, hydrogen to oil volume ratio 200 ~ 2000; Described Hydrobon catalyst with metal W and/or Mo and Ni for active ingredient, mean pore size 40 ~ 70 dust, total acid content 1.0 ~ 3.0mmol/g;
(3) second hydrofining reactor effluents enter cold high pressure separator after cooling, and isolated product liquid enters fractionating system, and gas is through purifying, and hydrogen-rich gas loops back reactor.
2. in accordance with the method for claim 1, it is characterized in that, in step (2), the first hydrogenator effluent first heated through process furnace before entering the second hydrofining reactor.
3. in accordance with the method for claim 1, it is characterized in that, in step (3), the second hydrogenator effluent is after realizing cooling with the mixture heat exchange of diesel raw material or diesel raw material and hydrogen, then enters cold high pressure separator.
4. in accordance with the method for claim 1, it is characterized in that, the first hydrogenator catalyst levels and the second reactor catalyst consumption volume ratio are 1: 2 ~ 1: 10.
5. in accordance with the method for claim 1, it is characterized in that, the operational condition of the first hydrogenator is: temperature of reaction 240 DEG C ~ 300 DEG C, reaction pressure 4.0MPa ~ 8.0MPa, volume space velocity 4h during liquid
-1~ 8.0h
-1, hydrogen to oil volume ratio 200 ~ 800; The operational condition of the second reactor hydrogenation is as follows: temperature of reaction 340 DEG C ~ 380 DEG C, reaction pressure 4.0MPa ~ 8.0MPa, volume space velocity 1.0h during liquid
-1~ 3.0h
-1, hydrogen to oil volume ratio 400 ~ 1000.
6. in accordance with the method for claim 1, it is characterized in that, described diesel raw material is straight-run diesel oil, secondary processing diesel oil or their parallel feeding.
7. in accordance with the method for claim 1, it is characterized in that, with the weight of catalyzer for benchmark, the catalyzer in the first reactor take oxide basis as 8wt% ~ 17wt% containing molybdenum, is 2wt% ~ 7wt% containing cobalt with oxide basis.
8. in accordance with the method for claim 1, it is characterized in that, with the weight of catalyzer for benchmark, the catalyzer in the second hydrogenator take oxide basis as 20wt% ~ 30wt% containing W and/or Mo, is 4wt% ~ 8wt% containing Ni with oxide basis.
9. in accordance with the method for claim 7, it is characterized in that, the strong acid content of described catalyzer is 0.02 ~ 0.08mmol/g; Its physical properties is as follows: specific surface area is 100 ~ 650 m
2/ g, pore volume is 0.15 ~ 0.8 mL/g.
10. in accordance with the method for claim 8, it is characterized in that, the strong acid content of described catalyzer is 0.1 ~ 0.5mmol/g; Its physical properties is as follows: specific surface area is 100 ~ 650m
2/ g, pore volume is 0.15 ~ 0.8mL/g.
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1769390A (en) * | 2004-10-29 | 2006-05-10 | 中国石油化工股份有限公司 | Method for producing high grade low condensation diesel oil from distillate oil |
| CN101590417A (en) * | 2008-05-29 | 2009-12-02 | 北京三聚环保新材料股份有限公司 | Hydrobon Catalyst And Its Preparation Method |
| CN101618347A (en) * | 2008-07-04 | 2010-01-06 | 中国石油化工股份有限公司 | Y-type molecular sieve-containing hydrocracking catalyst carrier and preparation method thereof |
| CN102041089A (en) * | 2009-10-21 | 2011-05-04 | 中国石油化工股份有限公司 | Hydrotreating method for producing low-sulphur and ultra-low sulphur 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 |
| FR2953740A1 (en) * | 2009-12-16 | 2011-06-17 | Inst Francais Du Petrole | New catalyst comprising amorphous support made of alumina, phosphorus, at dialkyl succinate, acetic acid and hydro-dehydrogenating function containing e.g. element of group VIB, useful for the hydrotreatment of hydrocarbon feedstocks |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8252709B2 (en) * | 2006-09-14 | 2012-08-28 | Cosmo Oil Co., Ltd. | Catalyst for hydrodesulfurization/dewaxing of hydrocarbon oil, process for producing the same, and method of hydrotreating hydrocarbon oil with the catalyst |
-
2011
- 2011-10-21 CN CN201110321333.0A patent/CN103059978B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1769390A (en) * | 2004-10-29 | 2006-05-10 | 中国石油化工股份有限公司 | Method for producing high grade low condensation diesel oil from distillate oil |
| CN101590417A (en) * | 2008-05-29 | 2009-12-02 | 北京三聚环保新材料股份有限公司 | Hydrobon Catalyst And Its Preparation Method |
| CN101618347A (en) * | 2008-07-04 | 2010-01-06 | 中国石油化工股份有限公司 | Y-type molecular sieve-containing hydrocracking catalyst carrier and preparation method thereof |
| CN102041089A (en) * | 2009-10-21 | 2011-05-04 | 中国石油化工股份有限公司 | Hydrotreating method for producing low-sulphur and ultra-low sulphur 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 |
| FR2953740A1 (en) * | 2009-12-16 | 2011-06-17 | Inst Francais Du Petrole | New catalyst comprising amorphous support made of alumina, phosphorus, at dialkyl succinate, acetic acid and hydro-dehydrogenating function containing e.g. element of group VIB, useful for the hydrotreatment of hydrocarbon feedstocks |
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