CN105018137B - Hydrocracking method of low-energy-consumption, productive and high-quality jet fuel - Google Patents
Hydrocracking method of low-energy-consumption, productive and high-quality jet fuel Download PDFInfo
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- CN105018137B CN105018137B CN201410164890.XA CN201410164890A CN105018137B CN 105018137 B CN105018137 B CN 105018137B CN 201410164890 A CN201410164890 A CN 201410164890A CN 105018137 B CN105018137 B CN 105018137B
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Abstract
The invention discloses a hydrocracking method of low-energy-consumption, productive and high-quality jet fuel. The hydrocracking method comprises the steps that after being mixed with hydrogen, raw oil undergoes heat exchange twice, passes through hydrofining and first cracking reaction zones in sequence after passing through a heating furnace and is separated to obtain middle distillate, and the middle distillate enters a second cracking reaction zone to be cracked, wherein the first cracking reaction zone at least comprises two cracking catalysts, namely an upstream filling catalyst I and a downstream filling catalyst II; the catalyst I contains 15-50wt% of modified Y molecular sieve; the catalyst II contains 3-30wt% of modified Y molecular sieve; the content of the modified Y molecular sieve in the catalyst I is higher than the content of the modified Y molecular sieve in the catalyst II by 10-25%. The hydrocracking method has the advantages that the high temperature and high pressure countercurrent heat transfer technology and the hydrocracking catalyst grading technology are organically combined and the hydrocracking reaction heat is comprehensively utilized, thus improving the quality of the target product and reducing the project investment and the operation energy consumption while maintaining the selectivity of the catalysts.
Description
Technical field
The present invention relates to a kind of method for hydrogen cracking, specifically a kind of low energy consumption is hydrogenated with using different type simultaneously to be split
Change the method for hydrogen cracking of catalyst greatly preparing hihg-quality jet fuel.
Background technology
As distillate demand is continuously increased between city's field alignment, refinery is needed to produce more intermediate oils, newly
Fuel standard tightened up requirement is proposed to the index of vapour, diesel oil.Obviously, time processing means and FCC techniques is not
Index request of the market to clean fuel can be met.Hydrocracking process is not only the secondary operations handss of heavy charge lighting
Section, even more obtains a kind of important means of high-quality jet fuel and cleaning diesel oil from inferior raw material.
Hydrocracking unit one-time investment is than larger, and operating cost is also higher.Therefore, each big research in countries in the world is public
Department all carries out substantial amounts of research positive to reduce the cost being hydrocracked, and makes great progress.In terms of catalyst：
The emphasis that each big patent business in the world is all developed the update of catalyst as oneself technology, in recent years, constantly in catalysis
The material of agent, the activity of catalyst, life-span, stability and reduces the aspects such as catalyst cost and has done substantial amounts of work.In work
Skill aspect：Distillate hydrocracking technology is quite ripe, and each major oil companies are same further optimization hydrocracking operation
When, innovative point is placed on and is hydrocracked on related group technology, by optimum organization technique come reduces cost；In addition, logical
The further investigation to being hydrocracked is crossed, the inherent connection between catalyst performance and feedstock property and purpose product quality is sought
System, sets up the emphasis that suitable catalyst grade is also the current area research with system.
United States Patent (USP)（US 4172815）Disclose a kind of while the single hop circulation hydrogenation for producing jet fuel and diesel oil splits
Change method, its technological process is：Heavy raw oil after being hydrocracked, its product through fractional distillation, obtain jet fuel fraction,
Diesel oil distillate and tail oil；Jet fuel fraction completely or partially mixes with tail oil, sends hydrocracking reactor back to.This technological process
Although significantly having the disadvantage that jet fuel is hydrocracked again is improve quality, its yield reduces more, hydrogen consumption to be increased, and
Investment also increases more.
United States Patent (USP)（US 5026472）, disclose one kind and be hydrocracked and the refined Joint Production of product cut oil repeated hydrogenation
The method of high-quality jet fuel.Its technological process can be briefly described for：Out product is divided cracker by thermal high twice
After separating from device, the kerosene distillate for obtaining repeated hydrogenation in finishing reactor is refined, and wherein used catalyst is precious metal catalyst
Agent；Out product is mixed into fractionating column to finishing reactor with the heavy distillate of cracker.The method technical characterstic is
Only kerosene distillate is refined, the purpose of production jet fuel is reached.But the method needs to increase more equipment, and is hydrogenated with
It is noble metal catalyst to refine catalyst used, and cost is larger, and can not obtain high-quality hydrogenation tail oil.
Chinese patent（CN 1272524）Disclose the work of a kind of middle pressure hydrocracking and the combination of kerosene Deep Hydrotreating
Skill flow process.The flow process be the higher arene content that will be obtained during middle pressure hydrocracking kerosene distillate oil at one compared with low pressure
Power, hydrogen purity be higher, compared with aromatic hydrocarbons saturation is carried out under conditions of low reaction temperatures, used catalyst is containing Pt or Ni reduction-states gold
The catalyst of category.The patent can be processed the kerosene distillate of higher arene content well, obtain qualified jet combustion
Material.But the method needs to increase more equipment, and the circulating load of kerosene distillate is larger, plant investment is increased, and operated
It is increasingly complex.
The content of the invention
For the deficiency of existing processing technique, the present invention provides a kind of method for hydrogen cracking of high-output qulified jet fuel.
High Temperature High Pressure countercurrent heat-transfer technology and hydrocracking catalyst level with organically combining, are comprehensively utilized hydrocracking reaction by the method
Heat, so as to reduce construction investment and operation energy consumption.The present invention is by two kinds of different type hydrocracking catalysts in reactor
In layering filling, the characteristics of give full play to two kinds of different type hydrocracking catalysts, can be with the spray of greatly preparing hihg-quality
Gas fuel, it is also possible to according to the market demand, and produce part high-quality hydrogenation tail oil.
A kind of method for hydrogen cracking of the high-output qulified jet fuel of low energy consumption that the present invention is provided, including following content：
（1）After heavy raw oil and hydrogen mixing, through hot high score gas/cold mixing feed exchanger, reaction effluent/heat
Mixed feeding heat exchanger, twice heat exchange heats up, then rises to reaction temperature with or without reaction heating furnace, anti-into hydrotreating
Answer area to contact with Hydrobon catalyst, carry out hydrofining reaction；
（2）Hydrofining reaction product enters the first hydrocracking reaction area, carries out hydrocracking reaction；
（3）Step（2）Gained reaction effluent carries out gas-liquid separation into separator, it is separated after obtain hydrogen-rich gas and
Fluid product；Hydrogen-rich gas Jing circulating hydrogen compressors are recycled, and fluid product carries out fractional distillation and obtains gas, stone into fractionating column
Cerebrol, jet fuel and tail oil；
（4）Step（3）Resulting tail oil can be whole, it is also possible to second is partly mixed into hydrogen and is hydrocracked instead
Area is answered, is further hydrocracked, raw material of the remainder hydrogenation tail oil as next machining cell；
（5）Step（4）The reaction product return to step for obtaining（3）, the reaction obtained with the first hydrocracking reaction area
After effluent mixing, gas-liquid separation and fractional distillation are carried out, obtain gas, Petroleum and the jet fuel of quantity increase.
According to method for hydrogen cracking of the present invention, wherein it is described the step of（2）In, in the first hydrocracking reaction area
Including at least two hydrocracking catalysts, according to the engagement sequence with raw material, respectively hydrocracking catalyst I and hydrogenation splits
Change catalyst II.Described hydrocracking catalyst I with VI B races and/or VIII race's metal as active metal component, by weight,
The content containing modified Y molecular sieve is 15~50wt% in catalyst I, is preferably 30~40wt%, the hydrocracking catalyst
II is same with VI B races and/or VIII race's metal as active metal component, and by weight, the content of modified Y molecular sieve is in catalyst
The content of modified Y molecular sieve is compared with hydrocracking catalyst in 3~30wt%, preferably 15~25wt%, wherein hydrocracking catalyst I
High 10~25 percent of modified Y molecular sieve content in agent II.
Wherein in the first hydrocracking reaction area, the filling body of hydrocracking catalyst I and hydrocracking catalyst II
Product ratio generally 1:5~5:1, preferably 1:3~3:1.
Conventional hydrocracking catalyst can be loaded in the second described hydrocracking reaction area.Such as can individually load
Hydrocracking catalyst I or hydrocracking catalyst II, or level is with using hydrocracking catalyst I and hydrocracking catalyst
II, for circulating cracking and hydrogenation tail oil.It is described when level is with using hydrocracking catalyst I and hydrocracking catalyst II
The volume ratio of hydrocracking catalyst I and hydrocracking catalyst II be generally 1:5~5:1, preferably 1:3~3:1.
Hydrocracking catalyst recited above I and hydrocracking catalyst II are with modified Y molecular sieve and aluminium oxide to carry
Body, or with modified Y molecular sieve, amorphous silica-alumina and aluminium oxide as carrier, with the B races of the periodic table of elements VI（Such as tungsten, molybdenum）And/or VIII
Race（Such as nickel, cobalt）Metal is active component, while some auxiliary agents such as phosphorus, titanium, zirconium etc. can be added.Commonly use on general industry
It is containing molecular sieve and/or unformed hydrocracking catalyst.On the basis of the weight of catalyst, in hydrocracking catalyst I or
The content of VI B races and/or VIII race's metal active constituent is generally 15% ~ 35% in II.
According to the method for present disclosure, in some specific embodiments, be modified Y molecules in hydrocracking catalyst I
The lattice constant of sieve is generally 2.435~2.445nm；The lattice constant of modified Y molecular sieve is general in hydrocracking catalyst II
For 2.425~2.435nm, preferably 2.425 to less than 2.435nm（2.425~<2.435nm）.
In preferred some embodiments, the SiO of modified Y molecular sieve in hydrocracking catalyst I2/Al2O3Mol ratio
Generally 5.0~70.0, its relative crystallinity is 90~130%；The SiO of modified Y molecular sieve in hydrocracking catalyst II2/
Al2O3Mol ratio is generally 5.0~50.0, and relative crystallinity is 90~120%.
Satisfactory hydrocracking catalyst I and hydrocracking catalyst II can select the commercial catalyst in this area
Agent.Satisfactory hydrocracking catalyst can also voluntarily be prepared according to method well known in the art as needed.
According to the method for present disclosure, described hydrotreating reaction area includes at least one Hydrobon catalyst bed
Layer, generally includes 2 ~ 3 hydrogenation catalyst beds.Described the first hydrocracking reaction area and the second hydrocracking reaction is distinguished
Not Bao Kuo at least 2 beds, generally respectively include 3~5 beds.2 wherein described or multiple catalysis
Agent bed can be arranged in a reactor, or can be respectively arranged in plural reactor.
In method for hydrogen cracking of the present invention, two big reaction zones can be included, the first reaction zone is by being hydrogenated with
Reason reaction zone and the first hydrocracking reaction area are constituted, generally using a reactor or two reactors in series operations, according to
With the engagement sequence of reaction mass, Hydrobon catalyst, hydrocracking catalyst I and hydrocracking catalyst II are loaded respectively
（Or combination loading Hydrobon catalyst, hydrocracking catalyst I and hydrocracking catalyst II）.Second reaction zone（I.e.
Two hydrocracking reaction areas）It is arranged in an independent little reactor, can individually loads hydrocracking catalyst I or hydrogenation splits
Change catalyst II, it is also possible to grading loading hydrocracking catalyst I and hydrocracking catalyst II, behaviour in parallel with the first reaction zone
Make, for circulating cracking and hydrogenation tail oil；Two sections of shared high-low pressure separators and fractionating column and hydrogen gas system.
In method for hydrogen cracking of the present invention, described Hydrobon catalyst generally comprises carrier and hydrogenation active metals.
On the basis of the weight of catalyst, metal component of group VIB in the periodic table of elements is generally included, such as tungsten and/or molybdenum are with oxide
It is calculated as 10%~35%, preferably 15%~30%；Group VIII metal such as nickel and/or cobalt are calculated as 1%~7% with oxide, preferably
1.5%~6%.Carrier is inorganic refractory oxide, is selected generally from aluminium oxide, amorphous silicon aluminium, silicon dioxide or titanium oxide etc..Can
To select existing various commercial catalysts, such as Fushun Petrochemical Research Institute（FRIPP）FF-14, FF- of development
24th, 3936, the 3996, Hydrobon catalyst such as FF-16, FF-26, FF-36, FF-46；HC-K, HC-P of Uop Inc.'s production is urged
Agent；TK-555, TK-565 catalyst of Topsoe companies production, it is also possible to as needed by the general knowledge system of this area
It is standby.
According to method for hydrogen cracking of the present invention, wherein step（3）Described in tail oil initial boiling point be generally 270~
385℃。
Heavy raw oil of the present invention can include the suitable hydrocarbon feed of various boiling ranges.Typical hydrocracking raw material
Including any heavy oil or synthesis oil distillate, this kind of raw material include straight-run gas oil, decompressed wax oil, wax tailings, delayed coking wax oil,
Gas oil viscosity reduction, reduced crude, Fisher-Tropsch synthesis fuels or deasphalted oil etc., or coal artificial oil or coal tar etc..
Used as technical term commonly used in the art, indication hydrofining reaction is typically wrapped with hydrocracking condition in the application
Include：Reaction pressure 5.0MPa~25.0MPa, preferred 6.0MPa~19.0MPa；200 DEG C~480 DEG C, preferably 270 DEG C of reaction temperature
~450 DEG C；Volume space velocity 0.1h-1~15.0h-1, preferred 0.2h-1~3.0h-1；Hydrogen to oil volume ratio 100:1~2500:1, preferably
400:1~2000:1.In the first hydrocracking reaction area, the average reaction temperature of usual hydrocracking catalyst II is relatively hydrogenated with
The average reaction temperature of Cracking catalyst I wants high 3~20 DEG C, preferably high 5~15 DEG C.
Heat exchanger described in the inventive method, can be the usual heat exchanger in this area, and preferably High Temperature High Pressure is inverse
Spread heat winding heat exchange of heat pipe.Described High Temperature High Pressure countercurrent heat-transfer winding heat exchange of heat pipe can choose the existing various phases in market
Patented technology is closed, e.g., the winding heat exchange of heat pipe CN 202902937U, Ke Yishi of Zhenhai Petrochemical Jianan Engineering Co., Ltd.'s exploitation
The full countercurrent heat-transfer of existing High Temperature High Pressure is high with heat transfer efficiency（Cold and hot end heat transfer temperature difference is little, generally 3 DEG C~8 DEG C）, heat exchange area
Greatly, using number of units is few, low manufacturing expense and the features such as little floor space.
Reaction heating furnace described in the inventive method be served only for meeting device go into operation the intensification of temperature-rise period low-temperature space will
Ask, reaction heating furnace only puts altar lamp during normal operating.The design load of reaction heating furnace is far below same device same treatment
The popular response heating furnace of amount, generally the 20%~60% of the similar treating capacity of same device, construction investment and operation energy consumption are significantly
Reduce.
Compared with prior art, the method have the advantages that：
1st, the present invention splits High Temperature High Pressure countercurrent heat-transfer technology and hydrogenation on the basis of existing hydrocracking process technology
Change catalyst grade with organically combining, technique is highly gathered with engineering, innovates supporting start-up method, develops the normal operating flames of anger
Reaction heating furnace is hydrocracked complete technology, and scientific and reasonable make use of hydrogenation reaction heat, reduce construction investment, reduce
Fuel consumption.
2nd, in the inventive method, hydrocracking reaction area select two kinds of hydrocracking catalysts contain different content,
Particularly there is the modified Y molecular sieve of different lattice constants as cracking active component.Two kinds of catalyst can be by certain volume
Ratio is loaded.The hydrocracking catalyst I of upstream contains higher molecular sieve content, and it has stronger aromatic hydrocarbons conversion energy
Power, can be converted into less molecule by the aromatic hydrocarbons of heavy constituent in raw material, and be distributed in heavy naphtha fraction and boat coal fraction；
Simultaneously the hydrocracking catalyst II in downstream has stronger alkane cracking capability, and two kinds of different moleculars sieve being hydrocracked for content
Catalyst synergism, hence it is evident that improve the quality of hydrocracked product, in particular improves the smoke point of boat coal fraction, and effectively
Reduce the BMCI values of tail oil.
3rd, the present invention circulates cracker by arranging single tail oil, can by tail oil it is some or all of be converted into
Light oil based on jet fuel, by adjusting operating condition, can flexibly produce the jet fuel and hydrogenation tail oil for obtaining high-quality.This
Product slates can also be improved outward, dry gas yied is reduced, improve economy.
4th, because two kinds of hydrocracking catalysts have activity difference, by the arrangement filling order of science, can be comprehensive
Using the reaction heat of upper bed layer, between bed can not liquid hydrogen injection, or few liquid hydrogen injection.The chilling of cracker can be greatly reduced
Hydrogen consumption and the cold hydrogen reserve level of hydrocracking unit accident（30~70% can typically be reduced）, play good energy-conservation and reduce fortune
Change into this effect.
5th, because whole reactor reaction temperature show an ascending trend is distributed, the relative raising of reactor outlet temperature is made, is improved
The temperature of heat exchanger thermal source, and the inventive method is from the high High Temperature High Pressure adverse current winding heat exchange of heat pipe of heat transfer efficiency, energy
Amount can obtain more reasonably comprehensively utilizing, it is possible to achieve the reaction heating furnace normal operating flames of anger, greatly reduce fuel
Consume.
6th, two-stage reaction shares a set of piece-rate system and hydrogen gas system in the present invention, so as to greatly simplify technological process, drop
Low cost of equipment and energy consumption.
Description of the drawings
Fig. 1 is a principle process flow diagram of the present invention.
Specific embodiment
The method of the present invention is described in detail below in conjunction with the accompanying drawings.
As shown in figure 1, a kind of technological process of the method for hydrogen cracking of the high-output qulified jet fuel of low energy consumption of the invention is such as
Under：Raw oil mixes with hydrogen, through hot high score gas/cold mixing feed exchanger 1, reaction effluent/hot mixing charging heat exchange
Device 2, twice heat exchange heats up, and the Jing heating furnaces 3 that go into operation rise to reaction temperature, carry out hydrofinishing into hydrotreating reaction area 4 anti-
Should；Finishing reactor product, with hydrogen the first hydrocracking reaction area 5 is mixed into, respectively with hydrocracking catalyst I 6
With the haptoreaction of hydrocracking catalyst II 7, reaction generation oil and the reacted effluent of raw oil/hot mixing feed exchanger 2
After heat exchange, into high pressure hot separator 8 gas-liquid separation, the top of the high pressure hot separator 8 hot high scores of hot high score gas Jing out are carried out
After gas/cold mixing feed exchanger 1 exchanges heat, then the cooling of Jing air coolers enters cold high pressure separator 9, and hot high score gas is in cold anticyclone point
Oil, Water, Gas three phase separation is carried out in device 9, gas Jing circulating hydrogen compressors 10 Jing after processing are recycled, high pressure hot separator
8 bottoms hot high score oil out enters the flash distillation of thermal low-pressure separators 11, and hot low point of gas is mixed into after cooling with cold high score oil
The flash distillation of cold low separator 12, cold low point of oil is mixed into fractionating system 13 with hot low point of oil, and fractional distillation obtains gas, light naphthar
14th, heavy naphtha 15, intermediate oil 16 and tail oil 17, wherein tail oil 17 can be according to the market demands, partly or entirely circulation
The second hydrocracking reaction area 18 is entered with hydrogen, respectively with hydrocracking catalyst I 19 or/and hydrocracking catalyst II
20 haptoreactions.Generate oil to go to separate fractionating system with the first hydrocracking reaction area reaction effluent mixing.
Followed by be hydrocracked side of the specific embodiment to a kind of high-output qulified jet fuel of low energy consumption of the present invention
Method is further described.
Embodiment 1-3
Embodiment 1-3 is using the exemplary flow shown in Fig. 1, and tail oil is all recycled to the second hydrocracking reaction area, used
The property of raw oil is shown in Table 1, from FF-46 hydrogenation pretreatment catalysts, different volumes ratio hydrocracking catalyst I/plus
The catalyst system of hydrogen Cracking catalyst II, the composition and property of catalyst are shown in Table 2.The process conditions and product of embodiment 1~3
Matter is listed in table 3,4, and the boiling range scope of each fraction is respectively in embodiment：65~160 DEG C of heavy naphtha, intermediate oil 160~
300 DEG C, tail oil>300℃.
One section refers to described in embodiment, and the single hop that hydrotreating reaction area is constituted with the first hydrocracking reaction area is connected
Reaction zone；The two-stage nitration refers to the second hydrocracking reaction area.
The result of embodiment 1-3 shows, using the method for hydrogen cracking of the present invention, can turn heavy raw oil maximum
Turn to the product based on high-quality jet fuel.
The raw oil main character of table 1
The catalyst main character of table 2.
Table 3 is hydrocracked technological condition.
* load ratio and refer to I/hydrocracking catalyst of hydrocracking catalyst II.
The hydrocracked product of table 4 is distributed and property.
Comparative example 1
Raw oil with embodiment 1-3, from urging for FF-46 pretreating catalyst by hydrocracking and hydrocracking catalyst I
Agent system.Process conditions and product property are listed in table 5, and the boiling range scope of each fraction is respectively in comparative example：Heavy naphtha 65
~160 DEG C, 160~300 DEG C of intermediate oil, tail oil>300℃.
The process conditions and product property of the comparative example 1 of table 5.
Embodiment 4-5
Embodiment 4-5 is the 50% of tail oil growing amount using the exemplary flow shown in Fig. 1, tail oil part circulation, circulating load,
Its raw oil and catalyst system are listed in table 6 with embodiment 1~3, process conditions and product property.Each fraction evaporates in embodiment
Journey scope is respectively：65~160 DEG C of heavy naphtha, 160~330 DEG C of intermediate oil, tail oil>330℃.
Comparative example 2
Raw oil with embodiment 1-3, from urging for FF-46 pretreating catalyst by hydrocracking and hydrocracking catalyst I
Agent system.Process conditions and product property are listed in table 6, and the boiling range scope of each fraction is respectively in comparative example：Heavy naphtha 65
~160 DEG C, 160~330 DEG C of intermediate oil, tail oil>330℃.
The process conditions of table 6 and product property
Claims (10)
1. a kind of method for hydrogen cracking of the high-output qulified jet fuel of low energy consumption, including following content：
（1）After heavy raw oil and hydrogen mixing, through hot high score gas/cold mixing feed exchanger, reaction effluent/hot mixing
Feed exchanger, twice heat exchange heats up, then rises to reaction temperature with or without reaction heating furnace, into hydrotreating reaction area
Contact with Hydrobon catalyst, carry out hydrofining reaction；
（2）Hydrofining reaction product enters the first hydrocracking reaction area, splits with hydrocracking catalyst I and hydrogenation successively
Change catalyst II haptoreaction；Hydrocracking catalyst I and hydrocracking catalyst II contain modified Y molecular sieve, described to add
In hydrogen Cracking catalyst I content of modified Y molecular sieve be 15~50wt%, modified Y molecular sieve in the hydrocracking catalyst II
Content be 3~30wt%, the content of modified Y molecular sieve in hydrocracking catalyst II compared with changing wherein in hydrocracking catalyst I
The content of property Y molecular sieve is high 10~25 percentage points；
（3）Step（2）Gained reaction effluent carries out gas-liquid separation into separator, and gained fluid product is carried out into fractionating column
Fractional distillation obtains gas, Petroleum, jet fuel and tail oil；
（4）Step（3）The part or all of and hydrogen of resulting tail oil is mixed into the second hydrocracking reaction area, further enters
Row is hydrocracked；
（5）Step（4）The reaction product return to step for obtaining（3）, the reaction outflow obtained with the first hydrocracking reaction area
After thing mixing, gas-liquid separation and fractional distillation are carried out, obtain gas, Petroleum and the jet fuel of quantity increase；
Wherein, the lattice constant of modified Y molecular sieve is 2.435~2.445nm, SiO in described hydrocracking catalyst I2/
Al2O3Mol ratio is 5.0~70.0, and relative crystallinity is 90~130%；The crystalline substance of modified Y molecular sieve in hydrocracking catalyst II
Born of the same parents' constant is 2.425 to less than 2.435nm, SiO2/Al2O3Mol ratio is 5.0~50.0, and relative crystallinity is 90~120%.
2. in accordance with the method for claim 1, it is characterised in that described hydrocracking catalyst I and hydrocracking catalyst
With VI B races and/or VIII race's metal as active metal component, by weight the content of active component is 15% ~ 35% for agent II.
3. in accordance with the method for claim 1, it is characterised in that in the first described hydrocracking reaction area, be hydrocracked
Catalyst I is 1 with the admission space ratio of hydrocracking catalyst II:5~5:1.
4. in accordance with the method for claim 1, it is characterised in that individually load hydrogenation in the second described hydrocracking reaction area
Cracking catalyst I or hydrocracking catalyst II, or level is with using hydrocracking catalyst I and hydrocracking catalyst II.
5. in accordance with the method for claim 4, it is characterised in that level is with using hydrogenation in the second hydrocracking reaction area
Cracking catalyst I and hydrocracking catalyst II, hydrocracking catalyst I is 1 with the volume ratio of hydrocracking catalyst II:5
~5:1.
6. in accordance with the method for claim 1, it is characterised in that the first hydrocracking reaction area includes at least 2 catalyst
Bed, at least 2 beds are arranged in a reactor, or are respectively arranged at plural reactor
It is interior.
7. in accordance with the method for claim 1, it is characterised in that step（3）Described in tail oil initial boiling point be 270~385
℃。
8. in accordance with the method for claim 1, it is characterised in that described hydrofining reaction area, first be hydrocracked it is anti-
Area and the reaction condition in the second hydrocracking reaction area is answered to include：Reaction pressure 5.0MPa~25.0MPa, 200 DEG C of reaction temperature
~480 DEG C, volume space velocity 0.1h-1~15.0h-1, hydrogen to oil volume ratio 100:1~2500:1.
9. in accordance with the method for claim 8, it is characterised in that in the first hydrocracking reaction area, hydrocracking catalyst
The average reaction temperature of agent II is high compared with the average reaction temperature of hydrocracking catalyst I 3~20 DEG C.
10. in accordance with the method for claim 1, it is characterised in that described hot high score gas/cold mixing feed exchanger, anti-
Answer effluent/hot mixing feed exchanger and wind heat exchange of heat pipe for High Temperature High Pressure countercurrent heat-transfer.
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| CN107304375B (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 conversion process catalyst grade matches 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 |
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