CN101928599B - Method for producing jet fuel or jet fuel blending component - Google Patents
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- CN101928599B CN101928599B CN200910148609.2A CN200910148609A CN101928599B CN 101928599 B CN101928599 B CN 101928599B CN 200910148609 A CN200910148609 A CN 200910148609A CN 101928599 B CN101928599 B CN 101928599B
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Abstract
The invention discloses a method for producing a jet fuel or a jet fuel blending component. A mixed oil is obtained by mixing a Fischer-Tropsch synthesis fuel and a direct coal liquefaction oil; and the jet fuel or jet fuel blending component is obtained by hydrorefining, hydrocracking, isocracking and fractionating the mixed oil. According to the method provided by the invention, two prepared coal oils can be converted into the high-quality jet fuel or jet fuel blending component. Compared with hydro-upgrading of the direct coal liquefaction oil, the method has the advantages of mild reaction conditions, low device investment cost and low operation cost.
Description
Technical field
The present invention relates to a kind of method that oil produced by coal produces jet fuel or Jet fuel blend component.More particularly, be by coal direct liquefaction oil and ICL for Indirect Coal Liquefaction oil in the presence of hydrogen gas, produce the method for jet fuel or Jet fuel blend component.
Background technology
The demand of high speed development to the energy of Chinese national economy continues vigorous, since 1993 Nian Qi China become net import of oil state, oil insufficiency of supply-demand expands year by year, crude oil external dependence degree raises year by year, within 2006, crude oil external dependence degree is 43%, within 2007, more than 46%, estimate that the year two thousand twenty will reach 60%.The fluctuation of international petroleum market and change will directly affect the safety of China's economy and even politics and stablize.Solve liquid fuel supply and demand problem by Non oil-based route synthetic liquid fuel, not only meet the requirement of national energy strategic security, and to national economy sustainable development steady in a long-term, there is important facilitation.
In numerous alternative energy source technology, F-T synthesis technology becomes the focus of various countries, the technological development of each major oil companies.The raw material sources of F-T synthesis are extensive, and coal, natural gas, associated gas, refinery's lighter hydrocarbons, poor residuum etc. all can as the raw materials for production of synthesis gas.Fischer-Tropsch synthesis is different according to object product, has high temperature method and low temperature process two technology paths.High temperature method mainly produces gasoline and various high valuable chemicals, and low temperature process mainly produces heavy hydrocarbon.The liquid fuel combustion performance adopting F-T synthesis technology to produce is good, and exhaust emission is little, is called as clean energy resource.ICL for Indirect Coal Liquefaction technology adapts to the advantages such as strong and oil quality is good owing to having raw material, has the successful example of commercial operation abroad: Sasol company has three factories of annual output about 7,400,000 tons synthetic oils in South Africa; Shell company has the factory of annual output about 540,000 tons synthetic oils in Malaysia.Such as ExxonMobil, Chevron, Topsoe, IFP etc. all research and develop energetically in F-T synthesis technical field in other oil companies.
US5766274 discloses a kind of method of being produced jet fuel by Fischer-Tropsch synthesis oil.In the method, artificial oil is divided into light oil, intermediate distillates, heavy distillate, intermediate distillates and the cracking of heavy distillate mixing back end hydrogenation, the light oil of gained kerosene distillate and non-hydrogenation is mixed to get jet fuel.
US5888376 discloses the method for producing jet fuel, first boiling range is that the Fischer-Tropsch synthetic of 40 ~ 260 DEG C carries out hydrotreatment by the method, under Raney nickel effect, with hydrogen and stream carries out hydrotreatment reaction, product is under noble metal catalyst effect, with hydrogen adverse current generation hygrogenating isomerization reaction, obtain the jet fuel with excellent low temperature flowability.
Germany just started the research that liquid hydrocarbon product technology is produced in DCL/Direct coal liquefaction as far back as 1913, and will manufacture the technology commercialization of gasoline with brown coal direct liquefaction in nineteen twenty-seven.Since within 1973, first time world oil crisis occurs, direct coal liquefaction technology is subject to the attention of developed country, in succession develops many direct coal liquefaction process.
CN1896189A discloses a kind of method that coal direct liquefaction oil produces large proportion boat coal.Coal direct liquefaction oil, by hydrofinishing and hydro-upgrading, can be produced proportion and be greater than 0.84g/cm
3boat coal.
Fischer-Tropsch synthesis oil upgrading gained kerosene distillate has the advantages that density is low, smoke point is high, and density is generally lower than 0.76g/cm
3, smoke point is higher than 40mm, although smoke point is high, density cannot meet jet fuel density and be greater than 0.775g/cm
3requirement; Coal direct liquefaction oil upgrading gained diesel oil has the advantages that density is high, smoke point is low, and density is generally higher than 0.84g/cm
3although density meets jet fuel requirement, smoke point, generally lower than 20mm, cannot meet the requirement that jet fuel is greater than 25mm.The upgrading kerosene of the two all cannot meet jet fuel standard-required.
Summary of the invention
The object of the invention is to provide a kind of coal to produce the method for oil production jet fuel or Jet fuel blend component on the basis of existing technology.
Method provided by the invention comprises the following steps:
(1) mix Fischer-Tropsch synthesis oil and coal direct liquefaction oil, obtain miscella;
(2) enter hydrofining reaction district after miscella and hydrogen mixing, contact with Hydrobon catalyst under Hydrofinishing conditions, obtain hydrofined oil; Fractionation hydrofined oil, obtains the cut comprising kerosene distillate I, diesel oil distillate I and tail oil fraction I;
(3) tail oil fraction I enters hydroisomerizing cracking reaction district, contacts, obtain hydrocrackates under hydroisomerizing cracking conditions with hydroisomerizing Cracking catalyst; Fractionation hydrocrackates, obtains the cut comprising kerosene distillate II, diesel oil distillate II and tail oil fraction II;
(4) the tail oil fraction II of step (3) gained loops back hydroisomerizing cracking reaction district and carries out hydroisomerizing cracking reaction;
(5) Mixture Density Networks oil distillate I and kerosene distillate II obtains jet fuel or Jet fuel blend component.
Described Fischer-Tropsch synthesis oil and the mixed proportion of coal direct liquefaction oil are 5: 95 (weight ratio) ~ 95: 5 (weight ratio).Preferred mixed proportion is 30: 70 (weight ratio) ~ 70: 30 (weight ratio).
Coal direct liquefaction oil is by coal and the solvent product oil that obtains of hydrogenation at reaction conditions.Described DCL/Direct coal liquefaction reaction condition is reaction temperature 250 ~ 550 DEG C, hydrogen dividing potential drop 15 ~ 40MPa.The boiling range of coal direct liquefaction oil of the present invention is 50 ~ 500 DEG C.
Described Fischer-Tropsch synthesis oil is Low Temperature Fischer Tropsch artificial oil, and boiling range is 20 ~ 680 DEG C.Low Temperature Fischer Tropsch artificial oil is the liquid hydrocarbon obtained after being contacted with fischer-tropsch synthetic catalyst under Low Temperature Fischer Tropsch synthesis condition with carbon monoxide by hydrogen.Described Low Temperature Fischer Tropsch synthesis condition is reaction temperature 160 ~ 250 DEG C, pressure 1.5 ~ 4.0MPa, air speed 300 ~ 3000h
-1, hydrogen/carbon monoxide mole ratios 1.5 ~ 2.5.Described fischer-tropsch synthetic catalyst is Co based Fischer-Tropsch synthesis catalyst.
Miscella removes most of alkene, oxygen, colloid in hydrofining reactor, polycyclic aromatic hydrocarbon fractional saturation.Described Hydrofinishing conditions is hydrogen dividing potential drop 2.0 ~ 15.0MPa, reaction temperature 250 ~ 400 DEG C, hydrogen to oil volume ratio 100 ~ 1000v/v, volume space velocity 0.5 ~ 10.0h
-1.
Described Hydrobon catalyst is a kind of metal load type catalyst, and carrier is unformed aluminium oxide, metal component be VIB or/and VIII base metal, wherein group vib metal be Mo or/and W, group VIII metal is that Co is or/and Ni.
The reactant in described hydrofining reaction district flows through the laggard row gas-liquid separation of cooling, and separating obtained hydrogen-rich gas capable of circulation time reaction zone, separating obtained liquid stream enters fractionating column.Fractionating column cutting obtains naphtha cut I, kerosene distillate I, diesel oil distillate I and tail oil fraction I, cut point wherein between naphtha cut I and kerosene distillate I is 100 DEG C ~ 150 DEG C, cut point between kerosene distillate I and diesel oil distillate I is 200 DEG C ~ 300 DEG C, and the cut point between diesel oil distillate I and tail oil fraction I is 300 DEG C ~ 360 DEG C.
The tail oil fraction I of gained enters isomery and/or cracking reaction that hydroisomerizing cracking reaction district carries out hydro carbons.In another preferred embodiment, the diesel oil distillate I of 20 ~ 80 described heavy % or 20 ~ 80 heavy % diesel oil distillate II enters hydroisomerizing cracking reaction district and carries out hydroisomerizing cracking reaction.Described hydroisomerizing cracking conditions is hydrogen dividing potential drop 2.0 ~ 15.0MPa, reaction temperature 300 ~ 450 DEG C, hydrogen to oil volume ratio 100 ~ 1500v/v, volume space velocity 0.5 ~ 5.0h
-1.
Described hydroisomerizing Cracking catalyst is noble metal catalyst or the non-precious metal catalyst of amorphous silicon aluminium load, the metal component of non-precious metal catalyst is that VIB is or/and VIII base metal, wherein group vib metal be Mo or/and W, group VIII metal is that Co is or/and Ni; The metal component of noble metal catalyst is that Pt is or/and Pd.
The reactant in described hydroisomerizing cracking reaction district flows through the laggard row gas-liquid separation of cooling, and separating obtained hydrogen-rich gas capable of circulation time reaction zone, separating obtained liquid stream enters fractionating column.Fractionating column cutting obtains naphtha cut II, kerosene distillate II, diesel oil distillate II and tail oil fraction II, cut point wherein between naphtha cut II and kerosene distillate II is 100 DEG C ~ 150 DEG C, cut point between kerosene distillate II and diesel oil distillate II is 200 DEG C ~ 300 DEG C, and the cut point between diesel oil distillate II and tail oil fraction II is 310 DEG C ~ 370 DEG C.
Advantage of the present invention:
(1) Fischer-Tropsch synthesis oil upgrading gained kerosene distillate has the advantages that density is low, smoke point is high, and density is generally lower than 0.76g/cm
3, smoke point is higher than 40mm, although smoke point is high, density cannot meet jet fuel density and be greater than 0.775g/cm
3requirement; Coal direct liquefaction oil upgrading gained diesel oil has the advantages that density is high, smoke point is low, and density is generally higher than 0.84g/cm
3although density meets jet fuel requirement, smoke point, generally lower than 20mm, cannot meet the requirement that jet fuel is greater than 25mm.The upgrading kerosene of the two all cannot meet jet fuel standard-required.By method provided by the invention, Fischer-Tropsch synthesis oil and coal direct liquefaction oil are by mixed hydrogenation upgrading, and its kerosene distillate can directly use as commodity jet fuel.
(2) relative to the hydro-upgrading of coal direct liquefaction oil, the reaction condition of Fischer-Tropsch synthesis oil and coal direct liquefaction oil mixed hydrogenation upgrading comparatively relaxes, and reduces device operating cost.
Accompanying drawing explanation
Accompanying drawing is the schematic flow sheet of the method for production jet fuel provided by the invention or Jet fuel blend component.
Detailed description of the invention
Below in conjunction with accompanying drawing, method provided by the present invention is further described, but the present invention is not therefore subject to any restriction.
Technological principle schematic flow sheet of the present invention is shown in accompanying drawing.Flow process is described below: the mixing logistics 1 of miscella and hydrogen enters hydrofining reactor A and reacts, and the effluent 2 of hydrofining reactor A enters hydrotreatment fractionating column B to carry out fractionation and be cut into naphtha cut 3, kerosene distillate 4, diesel oil distillate 5 and tail matter cut 6; Enter hydroisomerizing cracker C as logistics 7 after tail matter cut 6 mixes with the unconverted tail oil fraction 12 from fractionating column D, fill into hydrogen 13 to regulate the hydrogen-oil ratio in hydroisomerizing cracking reaction district at hydroisomerizing cracker entrance.Hydrocracking reaction is there is under the effect of hydroisomerizing Cracking catalyst, product and logistics 8 enter fractionating column D cutting and obtain naphtha cut 9, kerosene distillate 10, diesel oil distillate 11 and tail oil fraction 12, tail oil fraction 12 i.e. unconverted heavy end loops back cracker C and proceeds cracking, finally realizes the full conversion of heavy end.
The following examples will be further described method provided by the invention, but not thereby limiting the invention.
Test the character of Fischer-Tropsch synthesis oil used and coal direct liquefaction oil in table 1, the two obtains miscella after mixing according to a certain percentage.
The trade names testing Hydrobon catalyst used are RTF-1, and the trade names of hydroisomerizing Cracking catalyst are RCF-1.Be catalyst branch company of China Petrochemical Industry Chang Ling catalyst plant to produce.
Adopt fixed bed hydrogenation reactor, double-reactor operates, and wherein one instead loads Hydrobon catalyst RTF-1, catalyst loading amount 100ml; Two instead load hydroisomerizing Cracking catalyst RCF-1, catalyst loading amount 60ml.
Embodiment 1
Fischer-Tropsch synthesis oil and coal direct liquefaction oil according to 30: 70 ratio mixing, obtain feedstock oil A, its character, in table 2, carries out the hydro-upgrading of miscella according to previous process flow process, and the inlet amount of miscella is 123g/h.
Hydrofining reaction district operating condition is: temperature 320 DEG C, hydrogen dividing potential drop 11.0MPa, hydrogen to oil volume ratio 450.
Hydroisomerizing cracking reaction district operating condition is: temperature 365 DEG C, hydrogen dividing potential drop 11.0MPa, hydrogen to oil volume ratio 800.
The temperature range that fractionating column B cuts distillate is: naphtha cut I is < 120 DEG C, kerosene distillate I is 120 ~ 230 DEG C, and diesel oil distillate I is 230 ~ 350 DEG C, and tail oil fraction I is > 350 DEG C.
The temperature range that fractionating column D cuts distillate is: naphtha cut II is < 120 DEG C, kerosene distillate II is 120 ~ 230 DEG C, and diesel oil distillate II is 230 ~ 350 DEG C, and tail oil fraction II is > 350 DEG C.
The kerosene distillate I of mixing fractionating column B and fractionating column D and kerosene distillate II, the character of the kerosene 1 obtained is in table 3.
Embodiment 2
Fischer-Tropsch synthesis oil and coal direct liquefaction oil according to 50: 50 ratio mixing, obtain feedstock oil B, its character, in table 2, carries out the hydro-upgrading of miscella according to previous process flow process, and the inlet amount of miscella is 138g/h.
Hydrofining reaction district operating condition is: temperature 315 DEG C, hydrogen dividing potential drop 9.5MPa, hydrogen to oil volume ratio 400.
Hydroisomerizing cracking reaction district operating condition is: temperature 365 DEG C, hydrogen dividing potential drop 9.5MPa, hydrogen to oil volume ratio 800.
The temperature range that fractionating column B cuts distillate is: naphtha cut I is < 120 DEG C, kerosene distillate I is 120 ~ 230 DEG C, and diesel oil distillate I is 230 ~ 350 DEG C, and tail oil fraction I is > 350 DEG C.
The temperature range that fractionating column D cuts distillate is: naphtha cut II is < 120 DEG C, kerosene distillate II is 120 ~ 230 DEG C, and diesel oil distillate II is 230 ~ 350 DEG C, and tail oil fraction II is > 350 DEG C.
The kerosene distillate I of mixing fractionating column B and fractionating column D and kerosene distillate II, the character of the kerosene 2 obtained is in table 3.
Embodiment 3
Fischer-Tropsch synthesis oil and coal direct liquefaction oil according to 80: 20 ratio mixing, obtain feedstock oil C, its character, in table 2, carries out the hydro-upgrading of miscella according to previous process flow process, and the inlet amount of miscella is 150g/h.
Hydrofining reaction district operating condition is: temperature 310 DEG C, hydrogen dividing potential drop 9.0MPa, hydrogen to oil volume ratio 400.
Hydroisomerizing cracking reaction district operating condition is: temperature 365 DEG C, hydrogen dividing potential drop 9.0MPa, hydrogen to oil volume ratio 800.
The temperature range that fractionating column B cuts distillate is: naphtha cut I is < 140 DEG C, kerosene distillate I is 140 ~ 260 DEG C, and diesel oil distillate I is 260 ~ 350 DEG C, and tail oil fraction I is > 350 DEG C.
The temperature range that fractionating column D cuts distillate is: naphtha cut II is < 140 DEG C, kerosene distillate II is 140 ~ 260 DEG C, and diesel oil distillate II is 260 ~ 350 DEG C, and tail oil fraction II is > 350 DEG C.
Mixing fractionating column B and fractionating column D kerosene distillate I and kerosene distillate II, the character of the kerosene 3 obtained is in table 3.
Embodiment 4
On the technological process basis of embodiment 3, the diesel oil distillate II of fractionated out by fractionating column D 30 % by weight loops back hydroisomerizing cracker C.The operating condition of fractionating column B and D is with embodiment 3.
Hydrofining reaction district operating condition is: temperature 315 DEG C, hydrogen dividing potential drop 9.0MPa, hydrogen to oil volume ratio 400.
Hydroisomerizing cracking reaction district operating condition is: temperature 368 DEG C, hydrogen dividing potential drop 9.0MPa, hydrogen to oil volume ratio 850.
Mixing fractionating column B and fractionating column D kerosene distillate I and kerosene distillate II, the character of the kerosene 4 obtained is in table 4.
As can be seen from the data of the embodiment 1 of table 3, the kerosene 1 obtained by the method for the invention, its index meets No. 1 jet fuel standard-required, can use, also can use as its blending component as No. 1 jet fuel.As can be seen from the data of embodiment 2, the kerosene 2 obtained by the method for the invention, its index meets No. 2 jet fuel standard-requireds, can use, also can use as its blending component as No. 2 jet fuels.As can be seen from the data of embodiment 3, by changing product cut point, kerosene 3 index meets No. 3 jet fuel standard-requireds, can use, also can use as its blending component as No. 3 jet fuels.As can be seen from the data of embodiment 4, part diesel oil distillate and tail oil fraction are looped back hydroisomerizing cracker jointly, also can produce the fuel meeting jet fuel standard.
Table 1 Fischer-Tropsch synthesis oil and DCL/Direct coal liquefaction oil nature
| Fischer-Tropsch synthesis oil | Coal direct liquefaction oil | |
| Density (20 DEG C), g/cm 3 | 0.7910 | 0.9869 |
| Viscosity (20 DEG C), mm 2/s | 42.21 | |
| Condensation point, DEG C | 12 | |
| Carbon residue, w% | 13.2 | |
| Bromine valency, gBr/100g | 11.3 | 20.8 |
| Aromatic hydrocarbons, w% | 0 | 82.6 |
| Oxygen content, w% | 1.01 | 1.29 |
| Boiling range, DEG C | ||
| 5％ | 101 | 248 |
| 50％ | 372 | 326 |
| 90％ | 555 | 420 |
| 95％ | 616 | 453 |
Table 2 miscella character
| Miscella A | Miscella B | Miscella C | |
| Density (20 DEG C), g/cm 3 | 0.9282 | 0.8890 | 0.8301 |
| Carbon residue, w% | 9.36 | 6.82 | 2.70 |
| Bromine valency, gBr/100g | 18.63 | 16.38 | 13.25 |
| Aromatic hydrocarbons, w% | 57.8 | 41.3 | 16.5 |
| Oxygen content, w% | 1.21 | 1.15 | 1.07 |
| Boiling range, DEG C | |||
| 5％ | 195 | 169 | 135 |
| 50％ | 341 | 351 | 365 |
| 90％ | 480 | 489 | 516 |
| 95％ | 532 | 543 | 597 |
Table 3 kerosene distillate character
| Kerosene 1 | Kerosene 2 | Kerosene 3 | Kerosene 4 | No. 1 jet fuel | No. 2 jet fuels | No. 3 jet fuels | |
| Density (20 DEG C), g/cm 3 | 0.812 | 0.793 | 0.781 | 0.789 | Be not less than 0.775 | Be not less than 0.775 | 0.775～ 0.830 |
| Crystalline temperature, DEG C | ＜-60 | -59 | -51 | -53 | Not higher than-60 | Not higher than-50 | Not higher than-47 |
| Close flash point, DEG C | 33 | 32 | 45 | 45 | Be not less than 28 | Be not less than 28 | Be not less than 38 |
| Aromatic hydrocarbons, % by weight | 3.56 | 2.68 | 2.13 | 2.10 | Not higher than 20 | Not higher than 20 | Not higher than 20 |
| Smoke point, mm | 29 | 35 | 44 | 43 | Be not less than 25 | Be not less than 25 | Be not less than 25 |
| Boiling range, DEG C | |||||||
| IBP | 126 | 127 | 149 | 149 | Not higher than 150 | Not higher than 150 | / |
| 10％ | 172 | 172 | 192 | 191 | Not higher than 165 | Not higher than 165 | Not higher than 205 |
| 50％ | 187 | 189 | 211 | 212 | Not higher than 195 | Not higher than 195 | Not higher than 232 |
| 90％ | 205 | 210 | 237 | 238 | Not higher than 230 | Not higher than 230 | / |
| 98％ | 227 | 233 | 272 | 274 | Not higher than 250 | Not higher than 250 | / |
| FBP | 230 | 236 | 275 | 278 | / | / | Not higher than 300 |
Claims (9)
1. produce a method for jet fuel or Jet fuel blend component, comprising:
(1) mix Fischer-Tropsch synthesis oil and coal direct liquefaction oil, obtain miscella; Described Fischer-Tropsch synthesis oil is Low Temperature Fischer Tropsch artificial oil, and boiling range is 20 ~ 680 DEG C, and the Mixing ratio by weight example of described Fischer-Tropsch synthesis oil and coal direct liquefaction oil is 5: 95 ~ 95: 5,
(2) enter hydrofining reaction district after miscella and hydrogen mixing, contact with Hydrobon catalyst under Hydrofinishing conditions, obtain hydrofined oil; Fractionation hydrofined oil, obtains the cut comprising kerosene distillate I, diesel oil distillate I and tail oil fraction I;
(3) tail oil fraction I enters hydroisomerizing cracking reaction district, contacts, obtain hydrocrackates under hydroisomerizing cracking conditions with hydroisomerizing Cracking catalyst; Fractionation hydrocrackates, obtains the cut comprising kerosene distillate II, diesel oil distillate II and tail oil fraction II;
(4) the tail oil fraction II of step (3) gained loops back hydroisomerizing cracking reaction district and carries out hydroisomerizing cracking reaction;
(5) Mixture Density Networks oil distillate I and kerosene distillate II obtains jet fuel or Jet fuel blend component.
2. in accordance with the method for claim 1, it is characterized in that the Mixing ratio by weight example of described Fischer-Tropsch synthesis oil and coal direct liquefaction oil is 30: 70 ~ 70: 30.
3. in accordance with the method for claim 1, it is characterized in that the boiling range of described coal direct liquefaction oil is 50 ~ 500 DEG C.
4. in accordance with the method for claim 1, it is characterized in that, the diesel oil distillate I of described 20 ~ 80 heavy % or 20 ~ 80 heavy % diesel oil distillate II enters hydroisomerizing cracking reaction district and carries out hydroisomerizing cracking reaction.
5. in accordance with the method for claim 1, it is characterized in that described Hydrofinishing conditions is hydrogen dividing potential drop 2.0 ~ 15.0MPa, reaction temperature 250 ~ 400 DEG C, hydrogen to oil volume ratio 100 ~ 1000v/v, volume space velocity 0.5 ~ 10.0h
-1.
6. in accordance with the method for claim 1, it is characterized in that described hydroisomerizing cracking conditions is hydrogen dividing potential drop 2.0 ~ 15.0MPa, reaction temperature 300 ~ 450 DEG C, hydrogen to oil volume ratio 100 ~ 1500v/v, volume space velocity 0.5 ~ 5.0h
-1.
7. in accordance with the method for claim 1, it is characterized in that described Hydrobon catalyst is a kind of metal load type catalyst, carrier is unformed aluminium oxide, and metal component is that VIB is or/and VIII base metal, wherein group vib metal be Mo or/and W, group VIII metal is that Co is or/and Ni.
8. in accordance with the method for claim 1, it is characterized in that described hydroisomerizing Cracking catalyst is noble metal catalyst or the non-precious metal catalyst of amorphous silicon aluminium load, the metal component of non-precious metal catalyst is that VIB is or/and VIII base metal, wherein group vib metal be Mo or/and W, group VIII metal is that Co is or/and Ni; The metal component of noble metal catalyst is that Pt is or/and Pd.
9. in accordance with the method for claim 1, it is characterized in that the cut point between kerosene distillate I in described step (2) and diesel oil distillate I is 200 DEG C ~ 300 DEG C; Cut point between kerosene distillate II in described step (3) and diesel oil distillate II is 200 DEG C ~ 300 DEG C.
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| EP2797998A1 (en) * | 2011-12-29 | 2014-11-05 | 3M Innovative Properties Company | Curable polysiloxane composition |
| US20140097123A1 (en) * | 2012-10-09 | 2014-04-10 | George ARMISTEAD | Integrated hydroprocessing |
| CN103773462B (en) * | 2012-10-24 | 2015-08-12 | 中国石油化工股份有限公司 | A kind of two-segment hydrocracking method producing high-quality industrial chemicals |
| CN103773463B (en) * | 2012-10-24 | 2015-09-02 | 中国石油化工股份有限公司 | A kind of two-segment hydrocracking method |
| CN103773452B (en) * | 2012-10-24 | 2015-09-30 | 中国石油化工股份有限公司 | A kind of method for hydrogen cracking of high-output qulified industrial chemicals |
| CN103773450B (en) * | 2012-10-24 | 2015-08-12 | 中国石油化工股份有限公司 | A kind of method for hydrogen cracking processing inferior raw material |
| CN103773473B (en) * | 2012-10-24 | 2015-09-02 | 中国石油化工股份有限公司 | A kind of two-segment hydrocracking method producing high-quality rocket engine fuel |
| CN103773461B (en) * | 2012-10-24 | 2015-08-12 | 中国石油化工股份有限公司 | A kind of method for hydrogen cracking producing high-quality rocket engine fuel |
| CN107345164B (en) * | 2016-05-05 | 2018-10-12 | 中国石油化工股份有限公司 | A kind of method that straight-run diesel oil is hydrocracked production jet fuel |
| CN109988617B (en) * | 2017-12-29 | 2021-07-09 | 中国石油化工股份有限公司 | Flexible two-stage hydrocracking process |
| CN112708485B (en) * | 2020-12-27 | 2023-04-11 | 陕西延长石油（集团）有限责任公司 | Method for preparing high-calorific-value high-density jet fuel from kerosene mixed raw material |
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| CN1162516C (en) * | 2002-02-07 | 2004-08-18 | 中国石油化工股份有限公司 | Process for greatly preparing hihg-quality diesel oil or jet fuel from liquefied coil oil |
| CN100389181C (en) * | 2005-04-29 | 2008-05-21 | 中国石油化工股份有限公司 | Production of intermediate fractional oil from Fischer-Tropsch synthetic oil |
| CN101177623A (en) * | 2007-03-26 | 2008-05-14 | 中科合成油技术有限公司 | Hydro-cracking method for Fisher-Tropsch synthesis fuels |
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