CN103773463B - A kind of two-segment hydrocracking method - Google Patents
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Abstract
The invention discloses a kind of two-segment hydrocracking method.The method comprises: carry out hydrofining reaction after (1) inferior feedstock oil and hydrogen mixing; (2) hydrofining effluent carries out gas-liquid separation, obtains gas and liquid; (3) liquid enters hydrocracking reaction district and carries out hydrocracking reaction, and hydrocracking reaction district comprises hydrocracking catalyst I and II that two kinds have differing molecular sieve content; (4) hydrocracking effluent is through being separated and fractionation, obtains the product needed.In the inventive method, cracking catalyst I has stronger aromatic conversion ability, aromatic conversion in Raw material recombination can being divided is more small molecules, and be distributed in petroleum naphtha and jet fuel fraction, cracking catalyst II has stronger alkane cracking capability, two kinds of catalyzer synergies, significantly improve the quality of hydrocracked product, in particular improve the smoke point of jet fuel fraction.
Description
Technical field
The present invention relates to a kind of method for hydrogen cracking, particularly relate to a kind of can the two-segment hydrocracking method of production high-quality rocket engine fuel.
Background technology
Along with the continuous increase of distillate demand between city's field alignment, need refinery to produce more intermediate oil, the index of new fuel standard to vapour, diesel oil proposes stricter requirement.Obviously, time processing means and FCC technique can not meet the index request of market to clean fuel.Hydrocracking process is not only the secondary processing means of heavy feed stock lighting, obtains a kind of important means of high-quality rocket engine fuel and clean diesel especially from inferior raw material.
In recent years, along with the in poor quality day by day of the in short supply of worldwide crude resources and oil property, the character that hydroeracking unit processes raw material also heaviness and in poor quality day by day, relative oil density, sulphur content and nitrogen content constantly rise.At present, the nitrogen content that domestic hydroeracking unit processes raw material generally lower than 0.2%, but the processing of high-nitrogen stock inferior become each oil refining enterprise must in the face of and need solve problem.In addition, also there is the raw material that some are special, there is nitrogen content medium, but the feature that sulphur content is very low, processes these raw materials, conventional method for hydrogen cracking generally can not be used, need to make necessarily special improvement, comprise the raising of catalyst performance and the optimization etc. of processing condition.
Hydroeracking unit one-time investment is larger, and process cost is also higher.Therefore, countries in the world Ge great research company all carries out large quantifier elimination at the positive cost for reduction hydrocracking, makes great progress.In catalyzer: each large patent business in the world is all using the emphasis of the update of catalyzer as oneself technical development, in recent years, constantly at the material of catalyzer, activity, life-span, the stability of catalyzer and reduce the aspects such as catalyzer cost and done a large amount of work.At process aspect: distillate hydrocracking technology is quite ripe, and each major oil companies, while optimizing hydrocracking operation further, are placed on innovative point on the combination process relevant to hydrocracking, are reduced costs by optimum combination technique; In addition, by the further investigation to hydrocracking, seek the inner link between catalyst performance and feedstock property and object quality product, set up the emphasis that suitable catalyst grade part system is also this area research current.
United States Patent (USP) (US 4940503) discloses a kind of two sections of hydrocarbon conversion techniques and catalyzer, remove the impurity such as sulphur and nitrogen in the first paragraph, and through stripping, liquid after stripping enters second segment and carries out hydrocracking, the method needs stripping tower, and do not make full use of the space of reactor, Gradation Optimization is not carried out to hydrocracking catalyst, do not play the effect of catalyzer to greatest extent.
US Patent No. 4172815 discloses a kind of single hop circulation method for hydrogen cracking simultaneously producing rocket engine fuel and diesel oil, its technical process is: heavy raw oil is after hydrocracking, its product, through fractionation, obtains jet fuel fraction, diesel oil distillate and tail oil; Jet fuel fraction is all or part of to be mixed with tail oil, sends hydrocracking reactor back to.The obvious shortcoming of this technical process is that rocket engine fuel carries out hydrocracking again, although improve the quality of rocket engine fuel, the reduction of its jet fuel yield, total hydrogen consumption and investment increase more.
US Patent No. 5026472, discloses a kind of hydrocracking and product cut oil repeated hydrogenation refines the method for combination producing high-quality rocket engine fuel.Its technical process can simply be described as: out product is by after twice high pressure hot separator separation for cracking case, and the kerosene(oil)fraction obtained repeated hydrogenation in refining reaction device is refined, and wherein used catalyst is noble metal catalyst; The heavy distillate of refining reaction device out product and cracking case is mixed into separation column.The method technical characterstic is only to refine kerosene(oil)fraction, reaches the object of producing rocket engine fuel.But the method needs to increase more equipment, and hydrofining catalyzer used is noble metal catalyst, and cost is comparatively large, and can not obtain high-quality hydrogenation tail oil.
Chinese patent CN 1272524 discloses the technical process of a kind of middle pressure hydrocracking and the combination of kerosene Deep Hydrotreating.This flow process be by higher in a lower pressure, hydrogen purity for the kerosene(oil)fraction of the higher aromaticity content obtained in middle pressure hydrocracking process oil, compared with the condition of low reaction temperatures under carry out aromatic saturation, used catalyst is the catalyzer containing Pt or Ni as-reduced metal.This patent can process the kerosene(oil)fraction of higher aromaticity content well, obtains qualified rocket engine fuel.But the method needs to increase more equipment, and the internal circulating load of kerosene(oil)fraction is comparatively large, adds plant investment, and operation is more complicated.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of two-segment hydrocracking method, cracking zone is by the layering filling in the reactor of two kinds of dissimilar hydrocracking catalysts, to give full play to the feature of two kinds of dissimilar hydrocracking catalysts, the inventive method while maintenance two-segment hydrocracking method is strong to adaptability to raw material, can improve object quality product further.
A kind of two-segment hydrocracking method producing high-quality rocket engine fuel of the present invention comprises following content:
(1) enter hydrotreatment reaction zone after inferior feedstock oil and hydrogen mixing, contact with Hydrobon catalyst, carry out hydrofining reaction;
(2) hydrofining reaction resultant enters separator and carries out gas-liquid separation, after being separated, obtain hydrogen-rich gas and liquid product;
(3) step (2) obtains liquid product and enters hydrocracking reaction district, carries out hydrocracking reaction; Hydrogen-rich gas can recycle through circulating hydrogen compressor;
(4) the hydrocracking reaction effluent that obtains of step (3), carries out gas-liquid separation, and gas circulation uses, and liquid enters fractionating system, obtains hydrocracked product.
According to method for hydrogen cracking of the present invention, the inferior feedstock oil described in step (1) is the conventional hydrocracking raw material of this area.The boiling range of inferior feedstock oil is generally 350 ~ 620 DEG C, and nitrogen content, generally at more than 0.2wt%, is generally 0.2 ~ 0.3 wt%, and sulphur content is substantially unrestricted; Also can be nitrogen content at 0.08 more than wt%, be generally 0.1 ~ 0.2 wt%, sulphur content, at below 0.1wt%, is generally the low-sulfur high-nitrogen stock oil of 0.01 ~ 0.08 wt%.Described inferior feedstock oil is generally selected from the various coker gas oils (CGO) that processing middle-eastern crude obtains, as one or several in Iranian CGO, Saudi Arabia CGO etc., also can be the various coker gas oils (CGO) that processing Changqing Crude Oil obtains, also can be shale oil and the coal tar of corresponding cut.
In described step (3), in hydrocracking reaction district, comprise at least two kinds of hydrocracking catalysts, i.e. hydrocracking catalyst I and hydrocracking catalyst II.According to the engagement sequence with reaction mass, the upstream catalyst bed filling hydrocracking catalyst I in hydrocracking reaction district, downstream catalyst bed filling hydrocracking catalyst II; Described hydrocracking catalyst I with VI B race and/or VIII race's metal for active metal component, in catalyzer, the content of modified Y molecular sieve is 15 ~ 50wt%, be preferably 30 ~ 40wt%, described hydrocracking catalyst II equally with VI B race and/or VIII race's metal for active metal component, in catalyzer, the content of modified Y molecular sieve is 3 ~ 30wt%, be preferably 15 ~ 25wt%, wherein in hydrocracking catalyst I the content of modified Y molecular sieve compared with the high 10 ~ 25wt% of modified Y molecular sieve content in hydrocracking catalyst II.
Hydrocracking catalyst recited above all with modified Y molecular sieve and aluminum oxide for carrier, or with modified Y molecular sieve, amorphous aluminum silicide and aluminum oxide for carrier, with VI B race (as tungsten, molybdenum) and/or VIII race (as nickel, cobalt) metal for active metal component, in catalyzer can simultaneously containing some auxiliary agents as one or more in the elements such as phosphorus, titanium, zirconium.With the weight of catalyzer for benchmark, in hydrocracking catalyst, the content of VI B race and/or VIII race's active metal component is generally 15 ~ 35 wt% with oxide basis.
According to the method for hydrogen cracking that the present invention discloses, in some embodiment, in hydrocracking catalyst I, the lattice constant of modified Y molecular sieve is generally 2.435 ~ 2.445 nm, in hydrocracking catalyst II, the lattice constant of modified Y molecular sieve is generally 2.425 ~ 2.435 nm, is preferably 2.425 to being less than 2.435 nm(2.425 ~ <2.435nm).
In described hydrocracking catalyst I, the SiO of modified Y molecular sieve
2/ Al
2o
3mol ratio is generally 5 ~ 70, and its relative crystallinity is generally 90 ~ 130%; In described hydrocracking catalyst II, the SiO of modified Y molecular sieve
2/ Al
2o
3mol ratio is generally 5 ~ 50, and relative crystallinity is generally 90 ~ 120%.
Satisfactory hydrocracking catalyst I and hydrocracking catalyst II can select the commercial catalysts in this area.As hydrocracking catalyst I can be Fushun Petrochemical Research Institute's development and production 3824,3903,3971,3976, catalyzer or its mixture such as FC-12, FC-32, FC-36 or FC-46, or catalyzer or its mixture such as HC-16, HC-26, HC-43, HC-53, HC-140LT and HC-150 of Uop Inc.'s development and production.Also as required, satisfactory hydrocracking catalyst I can be prepared voluntarily according to method well known in the art.Described hydrocracking catalyst II can be Fushun Petrochemical Research Institute's development and production 3901,3973,3974, catalyzer or its mixture such as FC-16, FC-26, FC-40, FC-50, catalyzer or its mixtures such as DHC-8, DHC-32, HC-115, HC-215, HC-110, HC-120LT of Uop Inc.'s development and production.Also as required, the satisfactory hydrocracking catalyst II of molecular sieve content can be prepared voluntarily according to well known method.
According to the method that the present invention discloses, described hydrocracking reaction district should comprise at least two beds, generally includes 3 ~ 5 beds.Hydrocracking catalyst I and hydrocracking catalyst II is seated at least two beds respectively.Wherein said two or more beds can be arranged in a reactor, or can be arranged at respectively in two or more reactor.Wherein said hydrocracking catalyst I is generally 1:5 ~ 5:1, preferred 1:3 ~ 3:1 with the admission space ratio of hydrocracking catalyst II.
In method for hydrogen cracking of the present invention, the condition of the hydrofining reaction described in step (1) is generally: reactive hydrogen dividing potential drop 5.0 ~ 20.0MPa, average reaction temperature 280 ~ 427 DEG C, volume space velocity 0.1 ~ 10.0h
-1, hydrogen to oil volume ratio 300 ~ 3000.
In method for hydrogen cracking of the present invention, described in step (3), the operational condition in hydrocracking reaction district is generally, reactive hydrogen dividing potential drop 5.0 ~ 20.0MPa, average reaction temperature 280 ~ 427 DEG C, volume space velocity 0.1 ~ 10.0h
-1, hydrogen to oil volume ratio 300 ~ 3000.The average reaction temperature of usual hydrocracking catalyst II wants high 3 ~ 20 DEG C compared with the average reaction temperature of hydrocracking catalyst I, preferably 5 ~ 15 DEG C.
Compared with prior art, method for hydrogen cracking of the present invention has following characteristics:
1, in the inventive method, adopt two-stage hydrocracking technical process, widen the scope of stock oil, reduce the impurity such as the ammonia generated in inferior feedstock oil preprocessing process to greatest extent to the impact of hydrocracking catalyst, improve the hydrogen dividing potential drop in hydrocracking reaction district, farthest can play the performance of hydrocracking catalyst.
2, in the inventive method, modified Y molecular sieve that two kinds of hydrocracking catalysts that hydrocracking reaction district selects contain different content, that particularly have different lattice constant is as cracking active component, and two kinds of catalyzer according to a certain volume example load.The hydrocracking catalyst I of upstream is owing to containing higher Y molecular sieve content, and it has stronger aromatic conversion ability, can be less molecule by the aromatic conversion in heavy constituent in raw material, and is distributed in heavy naphtha fraction and boat coal cut; The hydrocracking catalyst II in downstream has stronger alkane cracking capability simultaneously, and the hydrocracking catalyst synergy of two kinds of differing molecular sieve content, significantly improves the quality of hydrocracked product, in particular improves the smoke point of boat coal cut.
3, in prior art, hydrocracking reaction district adopts traditional catalyst loading method, when only making a kind of hydrocracking catalyst, exothermic heat of reaction amount is comparatively large, when hydroeracking unit operates, needs the reaction temperature rising taking 24 ~ 40 DEG C with cold hydrogen away, and adopt method of the present invention, by the filling of reasonable arrangement catalyzer order, except can significantly improve except quality product, can also the exothermic heat of reaction of scientific utilization upper bed layer, can not liquid hydrogen injection between bed, or few liquid hydrogen injection.Quenching hydrogen consumption and the cold hydrogen reserve level of hydroeracking unit accident (generally can reduce 30 ~ 70%) of cracking case can being greatly reduced, playing the well energy-conservation effect with reducing operating cost.
4, in method for hydrogen cracking of the present invention, due to whole cracking case temperature of reaction show an ascending trend distribution, reactor outlet temperature is relatively high, thus improves the temperature of interchanger thermal source, energy obtains rational comprehensive utilization, decreases the load of process furnace.
Accompanying drawing explanation
Fig. 1 is a kind of principle process flow diagram of the inventive method.
Embodiment
Below in conjunction with accompanying drawing, method of the present invention is described in detail.
As shown in Figure 1, a kind of technical process of producing the two-segment hydrocracking method of high-quality rocket engine fuel of the present invention is as follows: inferior feedstock oil 1 is mixed into hydrotreatment reaction zone 2 with hydrogen 5 and hydrogen make-up and carries out hydrofining reaction.Refining reaction resultant 3 enters separator 4 and carries out gas-liquid separation, and separator 4 generally includes high-pressure separator and light pressure separator.Separator 4 obtains gas 5 and purifies Posterior circle use, the liquid 6 obtained enters hydrocracking reaction district 7, successively with hydrocracking catalyst I 8 and hydrocracking catalyst II 9 contact reacts, hydrocracking reaction effluent 10 enters separator 11, and separator 11 generally includes high-pressure separator and light pressure separator.Separator 11 obtains hydrogen-rich gas 12 and purifies Posterior circle use, obtains liquid hydrocarbon 14 and enters separation column 15 fractionation acquisition corresponding product: gas 16, petroleum naphtha 17, rocket engine fuel 18, diesel oil 19 and hydrogenation tail oil 20.
Next by specific embodiment, a kind of two-segment hydrocracking method producing high-quality rocket engine fuel of the present invention is further described.
Embodiment 1-3
Adopt the process flow sheet shown in Fig. 1.Hydrotreating reactor selects FF-46 pretreating catalyst by hydrocracking, and hydrocracking reactor adopts the catalyst system of the hydrocracking catalyst I/ hydrocracking catalyst II of different volumes ratio grating.In embodiment 1-3, in hydrocracking reactor, the volume ratio of hydrocracking catalyst I/ hydrocracking catalyst II is respectively 2:1,1:1 and 1:2, and stock oil character is in table 1.
At reaction pressure 15.0MPa, refining stage and cracking zone hydrogen to oil volume ratio are respectively 900:1 and 1100:1, and refining stage and cracking zone volume space velocity are respectively 1.0h
-1and 1.2h
-1condition under, carried out the technological test that > 350 DEG C of transformation efficiencys are about 80wt%, investigated the quality product of each cut.
Comparative example 1
Technical process is with embodiment 1-3, and stock oil is with embodiment 1-3.Select the catalyst system of FF-46 pretreating catalyst by hydrocracking and hydrocracking catalyst I.At reaction pressure 15.0 MPa, refining stage and cracking zone hydrogen to oil volume ratio are respectively 900:1 and 1100:1, and refining stage and cracking zone volume space velocity are respectively 1.0h
-1and 1.2h
-1, carried out the technological test that > 350 DEG C of transformation efficiencys are about 80wt%, investigated the quality product of each cut.
table 1 stock oil main character.
| Source | Wax oil |
| Density (20 DEG C)/gcm -3 | 0.8904 |
| Boiling range scope/DEG C | 250～580 |
| Sulphur/μ gg -1 | 1500 |
| Nitrogen/μ gg -1 | 2100 |
table 2 catalyzer main character.
| Catalyzer | FF-46 | Hydrocracking catalyst I | Hydrocracking catalyst II |
| Face shaping | Trifolium bar | Cylindrical bars | Cylindrical bars |
| Particle diameter, mm | 1.1~1.3 | 1.5～1.7 | 1.5～1.7 |
| Bar is long, mm | 3~8 | 3~8 | 3~8 |
| Modified Y molecular sieve content, wt% | — | 35 | 20 |
| Lattice constant, nm | — | 2.437 | 2.428 |
| SiO 2/Al 2O 3Mol ratio | — | 14 | 31 |
| Relative crystallinity * | — | 105 | 105 |
| Chemical constitution, wt%: | |||
| NiO | 4.0 | 6.5 | 7.2 |
| MoO 3 | 24.0 | — | — |
| WO 3 | — | 19.0 | 24.0 |
* relative crystallinity: Xc=Wc (Wc+Wa), in formula, Wc and Wa is respectively the weight percentage shared by crystallising part and non-crystallized part.
table 3 technological condition.
| Embodiment 1 | Embodiment 2 | Embodiment 3 | Comparative example | |
| Catalyzer | FF-46/ catalyst I/catalyst I I | FF-46/ catalyst I/catalyst I I | FF-46/ catalyst I/catalyst I I | FF-46/ catalyst I |
| Reaction stagnation pressure, MPa | 15 | 15 | 15 | 15 |
| Temperature of reaction/DEG C | 381/381/389 | 381/382/390 | 381/384/392 | 381/381 |
| Volume space velocity, h -1 | 1.0/1.2* | 1.0/1.2* | 1.0/1.2* | 1.0/1.2 |
| Hydrogen to oil volume ratio, v/v | 900:1/1100:1 | 900:1/1100:1 | 900:1/1100:1 | 900:1/1100:1 |
| > 350 DEG C of transformation efficiencys, wt% | ~80 | ~80 | ~80 | ~80 |
* to the cumulative volume air speed of hydrocracking catalyst.
the distribution of table 4 hydrocracked product and main products quality
| Embodiment 1 | Embodiment 2 | Embodiment 3 | Comparative example | |
| Heavy naphtha | ||||
| Yield, % | 31.67 | 31.58 | 32.42 | 32.01 |
| Density (20 DEG C)/gcm -3 | 0.7454 | 0.7466 | 0.7498 | 0.7438 |
| Boiling range/DEG C | ||||
| IBP/10% | 77/98 | 78/99 | 78/100 | 78/97 |
| 30%/50% | 108/120 | 110/123 | 110/126 | 106/117 |
| 70%/90% | 132/150 | 137/154 | 139/156 | 128/147 |
| 95%/EBP | 160/179 | 161/184 | 162/187 | 158/174 |
| Virtue is dived, % | 54.40 | 57.15 | 55.72 | 50.69 |
| Boat coal | ||||
| Yield, % | 23.17 | 23.02 | 22.91 | 23.15 |
| Density (20 DEG C)/gcm -3 | 0.8065 | 0.8047 | 0.8054 | 0.8082 |
| Boiling range/DEG C | ||||
| IBP/10% | 183/197 | 182/195 | 182/196 | 181/194 |
| 30%/50% | 202/210 | 203/212 | 204/213 | 200/207 |
| 70%/90% | 221/233 | 226/233 | 224/231 | 216/232 |
| 95%/EBP | 240/254 | 240/255 | 241/255 | 239/252 |
| Freezing point/DEG C | <-70 | <-70 | <-70 | <-60 |
| Smoke point/mm | 25 | 26 | 27 | 24 |
| Aromatic hydrocarbons, v% | 8.9 | 7.1 | 6.9 | 10.7 |
| Naphthalene system hydrocarbon, v% | 0.13 | 0.10 | 0.12 | 0.15 |
| Diesel oil | ||||
| Yield, % | 15.9 | 16.03 | 16.24 | 15.55 |
| Density (20 DEG C)/gcm -3 | 0.8155 | 0.8136 | 0.8134 | 0.8172 |
| Boiling range/DEG C | ||||
| IBP/10% | 267/286 | 268/285 | 268/285 | 269/286 |
| 30%/50% | 296/305 | 295/304 | 294/305 | 297/306 |
| 70%/90% | 318/334 | 316/333 | 318/334 | 320/335 |
| 95%/EBP | 343/350 | 342/349 | 342/350 | 343/350 |
| Condensation point/DEG C | -9 | -6 | -5 | -14 |
| Cetane index | 73.5 | 78.1 | 78.9 | 72.3 |
| Tail oil | ||||
| Yield, % | 20.6 | 20.58 | 20.73 | 20.31 |
| Density (20 DEG C)/gcm -3 | 0.8259 | 0.8253 | 0.8261 | 0.8263 |
| Boiling range/DEG C | ||||
| IBP/10% | 359/370 | 352/367 | 352/367 | 365/372 |
| 30%/50% | 389/399 | 385/402 | 385/402 | 392/394 |
| 70%/90% | 418/454 | 426/461 | 426/461 | 409/449 |
| 95%/EBP | 477/508 | 480/512 | 480/512 | 473/502 |
| Condensation point/DEG C | 33 | 33 | 33 | 34 |
| BMCI value | 8.2 | 7.5 | 7.3 | 9.2 |
Claims (9)
1. a two-segment hydrocracking method, comprises following content:
(1) enter hydrotreatment reaction zone after inferior feedstock oil and hydrogen mixing, contact with Hydrobon catalyst, carry out hydrofining reaction;
(2) hydrofining reaction resultant enters separator and carries out gas-liquid separation, after being separated, obtain hydrogen-rich gas and liquid product;
(3) step (2) obtains liquid product and enters hydrocracking reaction district, carries out hydrocracking reaction; Wherein comprise two kinds of hydrocracking catalysts in hydrocracking reaction district, according to the engagement sequence with reaction mass, the upstream catalyst bed filling hydrocracking catalyst I in hydrocracking reaction district, in hydrocracking catalyst I, the content of modified Y molecular sieve is 15 ~ 50wt%, in hydrocracking catalyst II, the content of modified Y molecular sieve is 3 ~ 30wt%, wherein in hydrocracking catalyst I the content of modified Y molecular sieve compared with the high 10 ~ 25wt% of modified Y molecular sieve content in hydrocracking catalyst II;
In described hydrocracking catalyst I, the lattice constant of modified Y molecular sieve is 2.435 ~ 2.445 nm, SiO
2/ Al
2o
3mol ratio is 5 ~ 70, and relative crystallinity is 90 ~ 130 %; In hydrocracking catalyst II, the lattice constant of modified Y molecular sieve is 2.425 ~ 2.435 nm, SiO
2/ Al
2o
3mol ratio is 5 ~ 50, and relative crystallinity is 90 ~ 120 %;
(4) the hydrocracking reaction effluent that obtains of step (3), carry out gas-liquid separation, liquid enters fractionating system, obtains hydrocracked product.
2. according to method for hydrogen cracking according to claim 1, it is characterized in that, in described hydrocracking catalyst I, the content of modified Y molecular sieve is 30 ~ 40wt%, and in described hydrocracking catalyst II, the content of modified Y molecular sieve is 15 ~ 25wt%.
3. according to method for hydrogen cracking according to claim 1, it is characterized in that, described hydrocracking catalyst I and hydrocracking catalyst II all with VI B race and/or VIII race's metal for active metal component, with the weight of catalyzer for benchmark, the content of active metal component is 15 ~ 35 wt% with oxide basis.
4. according to method for hydrogen cracking according to claim 1, it is characterized in that, in described hydrocracking catalyst II, the lattice constant of modified Y molecular sieve is 2.425 to being less than 2.435 nm.
5., according to method for hydrogen cracking according to claim 1, it is characterized in that, described inferior feedstock oil be nitrogen content at more than 0.2wt%, the unconfined high-nitrogen raw oil of sulphur content; Or be nitrogen content at 0.08 more than wt%, sulphur content is at the low-sulfur high-nitrogen stock oil of below 0.1wt%.
6. according to method for hydrogen cracking according to claim 1, it is characterized in that, described hydrocracking reaction district should comprise at least two beds, and hydrocracking catalyst I and hydrocracking catalyst II is seated at least two beds respectively.
7. according to method for hydrogen cracking according to claim 1, it is characterized in that, described hydrocracking catalyst I is 1:5 ~ 5:1 with the admission space ratio of hydrocracking catalyst II.
8. according to method for hydrogen cracking according to claim 1, it is characterized in that, the condition of described hydrofining reaction is: reactive hydrogen dividing potential drop 5.0 ~ 20.0MPa, average reaction temperature 280 ~ 427 DEG C, volume space velocity 0.1 ~ 10.0h
-1, hydrogen to oil volume ratio 300 ~ 3000; The operational condition in described hydrocracking reaction district is, reactive hydrogen dividing potential drop 5.0 ~ 20.0MPa, average reaction temperature 280 ~ 427 DEG C, volume space velocity 0.1 ~ 10.0h
-1, hydrogen to oil volume ratio 300 ~ 3000.
9. according to method for hydrogen cracking according to claim 8, it is characterized in that, the average reaction temperature of described hydrocracking catalyst II is high compared with the average reaction temperature of hydrocracking catalyst I 3 ~ 20 DEG C.
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