CN103773450B - A kind of method for hydrogen cracking processing inferior raw material - Google Patents
A kind of method for hydrogen cracking processing inferior raw material Download PDFInfo
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Abstract
The invention discloses a kind of method for hydrogen cracking processing inferior raw material.The method comprises: (1) inferior feedstock oil carries out hydrofining reaction; (2) hydrofining effluent carries out gas-liquid separation, obtains liquid and carries out fractionation; (3) fractionation gained tail oil enters 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 and inferior raw material are mixed into hydrotreatment reaction zone.In the inventive method, upstream catalyst I in cracking reaction district 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, downstream 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, specifically a kind of method for hydrogen cracking processing inferior raw material acquisition high-quality rocket engine fuel and ultra-low-sulphur diesel.
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.
US Patent No. 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, jet fuel yield reduction, 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 1272524A 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 the method for hydrogen cracking of a kind of inverted sequence series connection, 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 can, middle distillates oil selectivity strong to adaptability to raw material at maintenance inverted sequence serial hydrocracking method high while, improve object quality product further.
A kind of method for hydrogen cracking processing inferior raw material 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; Hydrogen-rich gas can recycle through circulating hydrogen compressor, and liquid product enters separation column to carry out fractionation and obtain gas, petroleum naphtha, rocket engine fuel, diesel oil and tail oil fraction;
(3) step (2) gained hydrogenation tail oil enters hydrocracking reaction district, carries out hydrocracking reaction;
(4) the hydrocracking reaction effluent that obtains of step (3), enters hydrotreatment reaction zone with inferior feedstock oil after mixing.
According to method for hydrogen cracking of the present invention, the inferior feedstock oil described in step (1) is Hydrocracking Raw Oil conventional in this area.The boiling range of described inferior feedstock oil is generally 350 ~ 620 DEG C, and nitrogen content is generally at more than 0.2wt%, and be preferably 0.2 ~ 0.3 wt%, 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 high nitrogen low sulfur 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, can also be shale oil and the coal tar fraction with corresponding boiling range.
In described step (3), in hydrocracking reaction district, comprise 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 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 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 simultaneously containing some auxiliary agents as one or more in the elements such as phosphorus, titanium, zirconium.General industry generally uses the hydrocracking catalyst containing modified Y molecular sieve and/or amorphous silicon aluminium.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 ~ 35wt%.
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 ~ <2.435 nm).
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 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 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, 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 for hydrogen cracking that the present invention discloses, described hydrocracking reaction district should comprise at least 2 beds, generally includes 3 ~ 5 beds.Wherein said 2 or multiple beds can be arranged in a reactor, or can be arranged at respectively in two or more reactor.Wherein 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: reaction pressure 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, the operational condition in described hydrocracking reaction district is generally, reaction pressure 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 preferred hydrocracking catalyst II wants high 3 ~ 20 DEG C, most preferably high 5 ~ 15 DEG C compared with the average reaction temperature of hydrocracking catalyst I.
Compared with prior art, the inventive method has following characteristics:
1, in the inventive method, adopt the technical process of inverted sequence serial hydrocracking, widen the scope of stock oil, improve the yield of intermediate oil, reduce the impurity such as the ammonia generated in preprocessing process to greatest extent to the impact of hydrocracking catalyst, farthest can play the performance of hydrocracking catalyst, improve quality product, the ultra-low-sulphur diesel that sulphur content is less than 10ppm can be obtained.
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 enough according to a certain volume example load.The hydrocracking catalyst I of upstream has higher 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 be distributed in heavy naphtha fraction and jet fuel fraction; 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 improve the smoke point of jet fuel fraction.
3, in prior art, hydrocracking adopts traditional catalyst loading method, and when only using 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, and by the filling of reasonable arrangement catalyzer order, can also scientific utilization upper bed layer exothermic heat of reaction, can not liquid hydrogen injection between bed, or few liquid hydrogen injection.Thus quenching hydrogen consumption and the cold hydrogen reserve level of hydroeracking unit accident (generally can reduce 30 ~ 70%) of cracking case can be greatly reduced, play 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, the present invention is a kind of, and to process the technical process of the method for hydrogen cracking of inferior raw material as follows: inferior feedstock oil 1 mixes with hydrogen 2, and after process furnace 3 heats, parallel feeding 4 enters hydrotreatment reaction zone 5 and carries out hydrofining reaction.Refining reaction device effluent 6 enters separator 7 and carries out gas-liquid separation, and described separator 7 generally includes high-pressure separator and light pressure separator.Separator 7 obtains recycling through circulating hydrogen compressor 9 after gas 8 purifies, and the liquid 10 obtained enters separation column 11, and fractionation obtains gas 12, petroleum naphtha 13, rocket engine fuel 14, diesel oil 15 and hydrogenation tail oil 16; Hydrogenation tail oil 16 enters hydrocracking reaction district 17, respectively with hydrocracking catalyst I 18 and hydrocracking catalyst II 19 contact reacts, hydrocracking effluent 20 enters hydrotreatment reaction zone 5 and reacts together with parallel feeding 4, obtains corresponding product.
Next by specific embodiment, a kind of method for hydrogen cracking processing inferior raw material of the present invention is further described.
Embodiment 1 ~ 3
Adopt process flow sheet shown in Fig. 1.Hydrotreating reactor selects FF-46 pretreating catalyst by hydrocracking, and hydrocracking reactor adopts the catalyst system being equipped with the hydrocracking catalyst I/hydrocracking catalyst II of different volumes ratio grating.Catalyzer I and catalyst II all with amorphous aluminum silicide and modified Y molecular sieve for carrier.In embodiment 1-3, 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, with embodiment 1-3, selects the catalyst system of FF-46 pretreating catalyst by hydrocracking and hydrocracking catalyst I.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.
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 hydrocracking technological condition.
| Embodiment 1 | Embodiment 2 | Embodiment 3 | Comparative example | |
| Catalyzer | FF-46/ catalyzer I/catalyst II | FF-46/ catalyzer I catalyst II | FF-46/ catalyzer I/catalyst II | FF-46/ catalyzer I |
| Reaction pressure, MPa | 15 | 15 | 15 | 15 |
| Temperature of reaction/DEG C | 383/382/390 | 383/384/392 | 383/386/394 | 389/386 |
| 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 |
* 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, % | 35.0 | 36.52 | 37.22 | 38.03 |
| Density (20 DEG C)/gcm -3 | 0.7456 | 0.7468 | 0.7500 | 0.7439 |
| Boiling range scope/DEG C | 77～181 | 79～186 | 79～187 | 80～179 |
| Virtue is dived, % | 50.40 | 54.00 | 52.72 | 47.29 |
| Rocket engine fuel | ||||
| Yield, % | 29.47 | 28.07 | 27.84 | 27.01 |
| Density (20 DEG C)/gcm -3 | 0.8065 | 0.8047 | 0.8054 | 0.8082 |
| Boiling range scope/DEG C | 183～256 | 181～257 | 183～257 | 182～258 |
| Freezing point/DEG C | <-60 | <-60 | <-60 | <-60 |
| Smoke point/mm | 24 | 25 | 26 | 20 |
| Aromatic hydrocarbons, v% | 9.9 | 8.1 | 7.1 | 12.7 |
| Naphthalene system hydrocarbon, v% | 0.13 | 0.10 | 0.12 | 0.15 |
| Diesel oil | ||||
| Yield, % | 19.75 | 20.11 | 20.22 | 19.55 |
| Density (20 DEG C)/gcm -3 | 0.8156 | 0.8137 | 0.8135 | 0.8172 |
| Boiling range scope/DEG C | 268～355 | 269～352 | 270～356 | 271～358 |
| Condensation point/DEG C | -10 | -8 | -7 | -17 |
| Sulphur/μ gg -1 | <10 | <10 | <10 | 18 |
| Cetane index | 74.8 | 77.0 | 78.2 | 70.3 |
Claims (9)
1. process a method for hydrogen cracking for inferior raw material, comprise 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; Hydrogen-rich gas recycles through circulating hydrogen compressor, and liquid product enters separation column to carry out fractionation and obtain gas, petroleum naphtha, rocket engine fuel, diesel oil and tail oil fraction;
(3) step (2) gained hydrogenation tail oil 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 loaded upstream hydrocracking catalyst I in hydrocracking reaction district, downstream filling hydrocracking catalyst II, 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 its relative crystallinity is 90 ~ 130%; In hydrocracking catalyst II, the lattice constant of modified Y molecular sieve is the SiO of 2.425 ~ 2.435 nm, modified Y molecular sieve
2/ Al
2o
3mol ratio is 5 ~ 50, and relative crystallinity is 90 ~ 120%;
(4) the hydrocracking effluent that obtains of step (3), enters hydrotreatment reaction zone with inferior feedstock oil after mixing.
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, the nitrogen content of described inferior feedstock oil is 0.2wt%, and sulphur content is unrestricted; Or described inferior feedstock oil 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 comprises at least two beds, and at least two described beds are arranged in a reactor, or can be arranged at respectively in plural reactor.
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 the method for hydrogen cracking described in claim 1 or 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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| CN105733674B (en) * | 2014-12-07 | 2017-10-27 | 中国石油化工股份有限公司 | A kind of method that inverted sequence is hydrocracked |
| CN107304373B (en) * | 2016-04-22 | 2019-03-19 | 中国石油化工股份有限公司 | A kind of catalytic diesel oil hydroconversion process |
| CN109777510B (en) * | 2017-11-14 | 2021-05-04 | 中国石油化工股份有限公司 | Hydrocracking method for improving jet fuel yield |
| CN109988623B (en) * | 2017-12-29 | 2021-06-04 | 中国石油化工股份有限公司 | Flexible reverse hydrocracking process |
| CN109988606B (en) * | 2017-12-29 | 2021-06-04 | 中国石油化工股份有限公司 | Flexible reverse hydrocracking process |
| CN114437786B (en) * | 2020-10-19 | 2023-07-04 | 中国石油化工股份有限公司 | Hydrocracking method of inferior raw oil |
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