CN107177374B - A kind of method of straight-run diesel oil production jet fuel - Google Patents
A kind of method of straight-run diesel oil production jet fuel Download PDFInfo
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- CN107177374B CN107177374B CN201610132497.1A CN201610132497A CN107177374B CN 107177374 B CN107177374 B CN 107177374B CN 201610132497 A CN201610132497 A CN 201610132497A CN 107177374 B CN107177374 B CN 107177374B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
- C10G65/12—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
Abstract
The present invention relates to a kind of methods of straight-run diesel oil production jet fuel, including the following contents: (1) straight-run diesel oil raw material and hydrogen are mixed into hydrotreating reaction area, and hydrodesulfurization, hydrodenitrogeneration reaction are carried out under relative low temperature and/or large volume space velocities；(2) refined straight-run diesel that step (1) obtains enters hydrocracking reaction area, contacts with hydrocracking catalyst, carries out hydrocracking reaction；(3) the hydrogenation of total effluent crackate that step (2) obtains enters supplement hydrofining reaction area, carries out aromatic hydrogenation saturated reaction；(4) the full fraction product after the purification that step (4) obtains obtains the products such as naphtha, jet fuel into separation fractionating system.Straight-run diesel oil maximum can be produced as jet fuel by the method for the present invention, improve added value of product.
Description
Technical field
The present invention relates to a kind of production methods of jet fuel, especially a kind of that high-quality jet is produced by straight-run diesel oil
The production method of fuel.
Background technique
As international air transport industry scale constantly expands, the whole world increases the demand of jet fuel year by year, and year increases
Rate is about 5.0%, significantly larger than the annual growth of petrol and diesel oil 1.0% to 1.5%, and high degree has driven global refined products market to excellent
The demand of matter jet fuel product, while also promoting the fast development of oil refining industry production jet fuel technology.World wide
Interior, existing jet fuel production technology is mainly straight run jet fuel fraction Hydrofining Technology and hydrocracking technology, jet
Fuel product compared with diesel oil or gasoline products in profit advantageously, be greatly facilitated major oil refining enterprise volume increase jet fuel
Product, but its yield is subject to processing oil property and two kinds of jet fuel production technology features restrictions and needs without being able to satisfy market
It asks.
United States Patent (USP) (US4172815) discloses single hop circulation that is a kind of while producing jet fuel and diesel oil and is hydrocracked
Method, process flow are as follows: for heavy raw oil after being hydrocracked, product obtains jet fuel fraction, bavin by fractionation
Oil distillate and tail oil；Jet fuel fraction is completely or partially mixed with tail oil, sends hydrocracking reactor back to.This process flow is bright
Although aobvious disadvantage is that jet fuel is hydrocracked improves quality again, its yield reduces more, hydrogen consumption and increases, and throw
Money also increases more.
United States Patent (USP) (US5026472) discloses one kind and is hydrocracked and product cut oil repeated hydrogenation purification Joint Production
The method of high-quality jet fuel.Its process flow can be briefly described are as follows: cracker comes out product and passes through thermal high twice point
After device separation, obtained kerosene distillate repeated hydrogenation in finishing reactor is refined, and wherein used catalyst is precious metal catalyst
Agent；Finishing reactor comes out product and the heavy distillate of cracker is mixed into fractionating column.This method technical characterstic is
Only kerosene distillate is refined, achievees the purpose that produce jet fuel.But this method needs to increase more equipment, and adds hydrogen
Purification catalyst used is noble metal catalyst, and cost is larger, and cannot obtain the hydrogenation tail oil of high quality.
Chinese patent (CN 1272524) discloses the work of a kind of middle pressure hydrocracking and the combination of kerosene Deep Hydrotreating
Skill process.The process is at one by the kerosene distillate oil of higher arene content obtained in middle pressure hydrocracking process compared with low pressure
Power, hydrogen purity be higher, compared with aromatic hydrocarbons saturation is carried out under conditions of low reaction temperatures, and used catalyst is containing Pt or Ni reduction-state gold
The catalyst of category.The patent can the kerosene distillate well to higher arene content handle, obtain qualified jet combustion
Material.But this method needs to increase more equipment, and the internal circulating load of kerosene distillate is larger, increases plant investment, and operate
It is increasingly complex.
Summary of the invention
In view of the problems of the existing technology, the present invention provides a kind of straight-run diesel oil hydro-conversion production jet fuel (i.e.
Kerosene) method.The method of the present invention fully considers the structure-activity relationship of jet fuel property and hydrocarbon structure composition, by preferably urging
The relatively multicomponent in straight-run diesel oil raw material is converted jet fuel product by agent system and optimization technological process and condition, protects
Hold higher jet fuel product yield.
A kind of method of straight-run diesel oil hydro-conversion production jet fuel provided by the invention, including the following contents:
(1) straight-run diesel oil and hydrogen are mixed into hydrotreating reaction area, in relative low temperature and/or large volume space velocities
Lower progress either shallow hydrodesulfurization, hydrodenitrogeneration, aromatic hydrocarbons saturated reaction；
(2) refined straight-run diesel that step (1) obtains enters hydrocracking reaction area, contacts with hydrocracking catalyst,
Carry out hydrocracking reaction；
(3) the hydrogenation of total effluent crackate that step (2) obtains enters supplement hydrofining reaction area, carries out aromatic hydrogenation
The reaction such as saturation；
(4) the full fraction product after the purification that step (4) obtains obtains naphtha, jet combustion into separation fractionating system
The products such as material.
In the method for the present invention, the straight-run diesel oil raw material is the diesel oil that various types crude oil is obtained through conventional destilling tower
Fraction can be any fraction of 220 DEG C of initial boiling point~do within the scope of 380 DEG C.The alkane quality of straight-run diesel oil raw material contains
Amount generally 30%~60%, preferably 35%~55%.The aromatics quality content of straight-run diesel oil raw material is generally 10%~35%, preferably
It is 15%~30%.
Catalyst used in step (1) hydrofining reaction area is that conventional hydro handles catalyst, can be each business
Catalyst, as Fushun Petrochemical Research Institute (FRIPP) development and production 3926,3936, CH-20,3996, FF-14, FF-16,
The hydrotreating catalysts such as FF-18, FF-26, FF-36, FF-46, FF-56, HR-416, HR- of Compagnie Francise des Petroles (IFP)
448 equal catalyst, TK-525, TK-557 catalyst of rope company of Top of Denmark (Topsor), the KF- of Dutch Acker assistant (AKZO)
752, KF-840, KF-901, KF-907 etc..The FH- of bulk phase catalyst such as Fushun Petrochemical Research Institute (FRIPP) development and production
FS etc..Above-mentioned hydrotreating catalyst can also be prepared by ability domain knowledge, and common hydrotreating catalyst (urge by support type
Agent, active metallic content is relatively low, is generally calculated as 20%~45% with oxide) catalyst carrier is first generally prepared, then
With infusion process supported active metals component；Bulk phase catalyst (active metallic content is high, is generally calculated as 50%~85% with oxide)
Generally prepared using coprecipitation.
The operating condition in hydrotreating reaction area described in step (1) are as follows: 3.0~16.0MPa of reaction pressure, preferably
The MPa of 6.0MPa~12.0；Average reaction temperature is 300 DEG C~370 DEG C, preferably 320 DEG C~350 DEG C；Volume space velocity 1.0~
5.0 h-1, preferably 2.0~3.0 h-1；Hydrogen to oil volume ratio 200: 1~2500: 1, preferably 300: 1~2000: 1.
Catalyst used in step (2) hydrocracking reaction area is hydrocracking catalyst, can be Fushun petroleum
The development and production of work research institute 3901,3973,3974, or mixtures thereof catalyst such as FC-16, FC-26, FC-40, FC-50,
The catalyst such as DHC-8, DHC-32, HC-115, HC-215, HC-110, HC-120LT of Uop Inc.'s development and production or its mixing
Object.Also it can according to need, according to it is well known that method voluntarily prepares the satisfactory hydrocracking catalyst of molecular sieve content
Agent.The hydrocracking catalyst is generally using VI B race and/or VIII race's metal as active metal component, molecular sieve in catalyst
Content is 3~30wt%, preferably 15~25wt%, and molecular sieve can be Y molecular sieve and/or beta-molecular sieve.Molecular sieve can basis
Conventional method in that art is modified.If the lattice constant of modified Y molecular sieve is generally 2.425~2.435nm, preferably
2.425 to less than 2.435nm(2.425~< 2.435nm), the SiO of modified Y molecular sieve2/Al2O3Molar ratio is generally 5.0~
50.0, relative crystallinity is 90~120%.Hydrocracking catalyst preferably has the hydrocracking catalyst of isomery performance, such as contains
The hydrocracking catalyst etc. of beta-molecular sieve.
The operating condition in hydrocracking reaction area described in step (2) are as follows: 3.0~16.0MPa of reaction pressure, preferably
The MPa of 6.0MPa~12.0；Average reaction temperature is 330 DEG C~420 DEG C, preferably 350 DEG C~390 DEG C；Volume space velocity 0.1~
3.0 h-1, preferably 0.8~2.0 h-1；Hydrogen to oil volume ratio 200: 1~2500: 1, preferably 300: 1~2000: 1.
It is that conventional hydro handles catalyst that step (3), which supplements catalyst used in hydrofining reaction area, can be with step
Suddenly hydrofining reaction area is consistent in (1), can also be selected by ability domain knowledge.
The operating condition in hydrofining reaction area is supplemented described in step (3) are as follows: 3.0~16.0MPa of reaction pressure, preferably
For the MPa of 6.0MPa~12.0；Average reaction temperature is 250 DEG C~370 DEG C, preferably 270 DEG C~290 DEG C；Volume space velocity 0.1
~6.0 h-1, preferably 0.5~3.0 h-1；Hydrogen to oil volume ratio 200: 1~2000: 1, preferably 300: 1~1500: 1.
Separation fractionating system described in step (4) is that conventional oil product well known to those skilled in the art separates fractionation train
System, for obtaining the purpose product of appropriate fraction.
" relative low temperature and/or large volume air speed " described in step (1) hydrotreating reaction area refer to step (2) plus
In comparison, specifically, following two condition at least selects one: (one) step (1) hydrotreating is anti-in hydrogen cracking reaction area
Answer the reaction temperature in area 10~50 DEG C lower than step (2) hydrocracking reaction area, it is 15~30 DEG C preferably low；(2) step (1) adds
The volume space velocity of hydrogen processing reaction zone is 1.2~5 times of step (2) hydrocracking reaction area volume space velocity, preferably 1.5~3
Times, most preferably 2~3 times.It is preferred that the operation temperature and air speed coordinated of two step reactions, obtain optimal technology effect
Fruit.It is controlled by reaction result, it is preferable that the sulfur content of liquid product is 100 μ gg after rate-determining steps (1) hydrotreating-1With
On, preferably 100~500 μ gg-1, more preferable 200~400 μ gg-1.Sulphur after hydrotreating in liquid product is mainly
The sulfur-containing organic compound for more difficult removing that structure is complicated, such as benzothiophene, dibenzothiophenes, 4,6- dimethyl Dibenzothiophene
Deng.
In order to further increase product quality, freezing point, the condensation point of by-product diesel oil distillate of jet fuel, Ke Yi are such as reduced
Hydrocracking reaction area properly mixes pour point depression catalyst, such as hydrodewaxing catalyst or isomerization-visbreaking catalyst, can also add
Pour point depression reaction zone is set after hydrogen cracking reaction area.
Technical staff knows that crude oil is commonly referred to as straight-run oil (directly distillation by the various distillates that distillation obtains
Obtained distillate), generally comprise straight-run naphtha fraction, straight run kerosene fraction, straight(-run) diesel distillate etc..Straight run kerosene fraction
Mainly for the production of jet fuel, straight(-run) diesel distillate is mainly for the production of diesel oil.Naphtha cut is mainly 40 DEG C~180 DEG C
Fraction, kerosene are mainly 140 DEG C~280 DEG C fractions, and diesel oil distillate is mainly 200 DEG C~350 DEG C fractions.From typical carbon number
It sees, the typical carbon number of naphtha cut is C4~C12, and the typical carbon number of jet fuel is C8~C15, the allusion quotation of straight(-run) diesel distillate
Type carbon number is within the scope of C10~C20.Straight(-run) diesel distillate to be mainly characterized by paraffinicity higher, studies have shown that straight run bavin
For such alkane of oil distillate when carrying out conventional hydrocracking reaction, most of product is naphtha cut, and kerosene distillate
Product yield is lower, therefore is difficult to effectively realize with the route of straight(-run) diesel distillate production jet fuel.And secondary operation obtains
Diesel oil distillate (such as catalytic cracking diesel oil), since molecular structure and straight-run diesel oil have biggish different (arene content height),
It is easy to instead through hydrocracking and the technological means such as hydrogen saturation is added to obtain jet fuel, therefore the two does not have comparativity, presses
Existing theoretical and practice (including laboratory and industry), the conclusion of those of ordinary skill is that straight-run diesel oil is not to be hydrocracked skill
The Suitable base of art production jet fuel.
In the present invention, the feature high for straight-run diesel oil feed paraffins content, arene content is low, step (1) adds at hydrogen
Manage the cooperation of reaction zone and step (2) hydrocracking reaction area condition, the desulfurization degree of step (1), denitrification percent, aromatic hydrocarbons saturation factor phase
To it is lower (compared with routine techniques, in conventional hydrocracking reaction, need before material is contacted with hydrocracking catalyst,
Sulphur, nitrogen are removed to reduced levels, generally in 10 μ gg-1Below), a certain amount of organic sulfur compound, organic nitrogen compound are remained
And the organic compounds containing sulfur of aromatic hydrocarbons, especially macromolecular, these substances on hydrocracking catalyst competitive Adsorption as a result,
Make raw material that isomerization reaction and cracking reaction collaboration have occurred, after isomery occurs for alkane, in the competition of macromolecular organic sulfur compound
Under adsorption conditions, the reaction mechanism mechanism of reaction is changed, improves the selectivity of purpose product, reduces the generation of second pyrolysis reaction, most
Obviously increase the product yield that can be used for jet fuel.Product after cracking passes through post-refining, can achieve jet
Other quality index (mainly smoke point etc.) of fuel.
The method of the present invention fully considers the structure-activity relationship of jet fuel property and hydrocarbon structure composition, passes through preferred catalyst
System and optimization technological process and condition, it is special using adsorption structure of the benzothiophenes on hydrocracking catalyst
Property, the new reaction mechanism mechanism of reaction is constructed, the yield of jet fuel product is effectively increased.
Straight-run diesel oil and hydrogen are mixed into hydrotreating reaction area, and either shallow occurs under relative low temperature, large volume air speed
Hydrofining reaction remains part benzothiophene kind macromolecular organic sulfur compound and part organonitrogen compound and aromatic hydrocarbons；
Subsequent refined oil enters hydrocracking reaction area, contacts with hydrocracking catalyst, and under specific reaction environment, it is anti-that collaboration occurs
It answers, changes the reaction mechanism mechanism of reaction, improve the selectivity of purpose product, reduce the generation of second pyrolysis reaction, be conducive to improve
The yield of jet fuel.It is a discovery of the invention that passing through the suction type of benzothiophenes and hydrocracking catalyst, effectively
The activated centre function of having adjusted hydrocracking catalyst forms the steric hindrance catalytic center structure under reactiveness, makes
Alkane isomery is embodied in being effectively reduced for jet fuel freeze.Think that either shallow hydrofinishing can retain original through research
The sulfur-containing compound of part labyrinth in material, such as benzothiophenes, oil-source rock correlation, such big point
There are 2 major class suction types in sub- sulfur-containing compound and hydrocracking catalyst activated centre: π cooperation absorption and sulphur and metal are direct
The M-S key absorption that effect is formed, effectively has adjusted the activated centre function of hydrocracking catalyst, forms under reactiveness
Steric hindrance catalytic center structure makes alkane isomery, and asymmetry chain rupture is occurred for the alkane after isomery, reduces simultaneously
The generation of second pyrolysis reaction, ensure that the yield of jet fuel product.In addition, retaining a small amount of macromolecular sulfide in jet
In fuel product, product greasy property can be improved.In the presence of a certain amount of organosulfur compound, especially bigger molecule is organic
In the presence of sulfide, significant change is had occurred in the distribution of straight-run diesel oil isocrackate, and jet fuel yield significantly improves, this
It is the new discovery in this field.
It is hydrocracked the full fraction product of production, is exchanged heat, reduces temperature, product is in relative low temperature, the operation item of high pressure
Under part, supplement hydrofinishing is carried out, due to being usually the dynamics Controlling area of aromatic hydrogenation saturation under this operating condition,
Aromatic hydrocarbons and unsaturated hydro carbons can be effectively converted, jet fuel smoke point is further increased.
Detailed description of the invention
Fig. 1 is the flow diagram for the method that a kind of straight-run diesel oil of the present invention produces jet fuel.
Specific embodiment
A kind of method of straight-run diesel oil production jet fuel of the invention is described in detail with reference to the accompanying drawing.
As shown in Figure 1, a kind of method flow of straight-run diesel oil production jet fuel of the invention is as follows: straight-run diesel oil 1 with
Hydrogen 2 is mixed into hydrotreating reaction area 4 and contacts with hydrotreating catalyst, and progress hydrodenitrogeneration, either shallow hydrodesulfurization are anti-
It answers.Enter hydrocracking reaction area 5 later to contact with the hydrocracking catalyst with isomery performance, by the high chain of molecule carbon number
Alkane carries out isomery, chain-breaking reaction.It is then hydrocracked full fraction and generates oil 6 through heat exchange reduction temperature, into supplement plus hydrogen essence
Reaction zone 7 processed carries out supplement hydrofinishing under conditions of relative low temperature, high pressure, and aromatic hydrocarbons is effectively reduced and unsaturated hydrocarbons contains
Amount further increases smoke point, reduces naphthalene system hydrocarbon.Production oil 8 enters separation system 9 later, and hydrogen-rich gas 10 after processing, passes through
Circulating hydrogen compressor is recycled, and the liquid product 11 of acquisition is fractionated into fractionating column 12, obtains gas 13, naphtha
14, jet fuel 15, diesel oil 16.
Make followed by method of the specific embodiment to a kind of straight-run diesel oil production jet fuel of the invention further
Explanation.M% indicates mass percent.
Examples 1 to 6
For the present embodiment using two kinds of straight-run diesel oils of A, B as feedstock oil, catalyst is that Fushun Petrochemical Research Institute's development is opened
FF-46 hydrotreating catalyst is loaded in the commercial catalysts of hair, hydrotreating reaction area and supplement hydrofining reaction area, adds hydrogen
Load FC-50 catalyst in cracking reaction area.The concrete operations process of use is shown in attached drawing 1.Embodiment is using two reactor series connection
Form, hydrotreating reaction area and hydrocracking reaction area are in a reactor.Raw material oil nature is shown in Table 1, catalyst base
This property is shown in Table 2, and the feedstock oil of Examples 1 to 3 is straight-run diesel oil A, process condition and the results are shown in Table 3~table 4；Implement
The feedstock oil of example 4~6 is straight-run diesel oil B, process condition and the results are shown in Table 5~table 6.
Comparative example 1 ~ 2
Comparative example 1 ~ 2 is conventional straight-run diesel oil hydrocracking process, generates oily be fractionated and obtains jet fuel product.
1 raw material oil nature of table
2 catalyst property of table
The process conditions and product distribution that 3 straight-run diesel oil A of table is hydrocracked
The product property that 4 straight-run diesel oil A of table is hydrocracked
Using straight-run diesel oil A as the relatively narrow raw material of the fraction of representative, after hydro-conversion, generating oil only need to be by naphtha
It cuts out, can be obtained jet fuel product, jet fuel yield is high, and process flow is simple, plant construction investment and operation energy consumption
It is lower.
The process conditions and product distribution that 5 straight-run diesel oil B of table is hydrocracked
The product property that 6 straight-run diesel oil B of table is hydrocracked
Pledge can be produced using the technology of the present invention under appropriate conditions using straight-run diesel oil B as the long distillate raw material of representative
Excellent jet fuel product is measured, process flow is simple, is transformed using existing diesel hydrotreating unit or new device, energy
Enough steady production high value jet fuel products, are effectively reduced diesel and gasoline ratio, improve Business Economic Benefit.
Claims (12)
1. a kind of method of straight-run diesel oil production jet fuel, including the following contents:
(1) straight-run diesel oil raw material and hydrogen are mixed into hydrotreating reaction area, in relative low temperature and/or large volume space velocities
Lower progress hydrodesulfurization, hydrodenitrogeneration reaction；
(2) refined straight-run diesel that step (1) obtains enters hydrocracking reaction area, contacts with hydrocracking catalyst, carries out
Hydrocracking reaction；
(3) the hydrogenation of total effluent crackate that step (2) obtains enters supplement hydrofining reaction area, carries out aromatic hydrogenation saturation
Reaction；
(4) the full fraction product after the purification that step (3) obtains obtains naphtha, jet fuel produces into separation fractionating system
Product；
" relative low temperature and/or large volume air speed " described in step (1) hydrotreating reaction area refers to that with step (2) plus hydrogen is split
Change reaction zone in comparison, specifically, following two condition at least selects one: (one) step (1) hydrotreating reaction area
Reaction temperature it is 15~30 DEG C lower than step (2) hydrocracking reaction area；(2) volume in step (1) hydrotreating reaction area is empty
Speed is 1.2~5 times of step (2) hydrocracking reaction area volume space velocity.
2. according to the method described in claim 1, it is characterized by: the volume space velocity in step (1) hydrotreating reaction area is step
Suddenly 1.5~3 times of (2) hydrocracking reaction area volume space velocity.
3. according to the method described in claim 1, it is characterized by: the straight-run diesel oil raw material is crude oil through conventional destilling tower
And the diesel oil distillate obtained, it is 220 DEG C of the initial boiling point any fractions done within the scope of 380 DEG C.
4. according to the method described in claim 3, it is characterized by: the alkane mass content of straight-run diesel oil raw material be 30%~
60%, the aromatics quality content of straight-run diesel oil raw material is 10%~35%.
5. according to the method described in claim 3, it is characterized by: the alkane mass content of straight-run diesel oil raw material be 35%~
55%；The aromatics quality content of straight-run diesel oil raw material is 15%~30%.
6. according to the method described in claim 1, it is characterized by: the operation item in hydrotreating reaction area described in step (1)
Part are as follows: 3.0~16.0MPa of reaction pressure, average reaction temperature are 300 DEG C~370 DEG C, 1.0~5.0 h of volume space velocity-1, hydrogen oil
Volume ratio 200: 1~2500: 1.
7. according to the method described in claim 1, it is characterized by: the operation item in hydrotreating reaction area described in step (1)
Part are as follows: reaction pressure is the MPa of 6.0MPa~12.0, and average reaction temperature is 320 DEG C~350 DEG C, volume space velocity 2.0~3.0
h-1, hydrogen to oil volume ratio 300: 1~2000: 1.
8. according to the method described in claim 1, it is characterized by: the operation item in hydrocracking reaction area described in step (2)
Part are as follows: 3.0~16.0MPa of reaction pressure, average reaction temperature are 330 DEG C~420 DEG C, 0.1~3.0 h of volume space velocity-1, hydrogen oil
Volume ratio 200: 1~2500: 1.
9. according to the method described in claim 1, it is characterized by: the operation item in hydrocracking reaction area described in step (2)
Part are as follows: reaction pressure is the MPa of 6.0MPa~12.0, and average reaction temperature is 350 DEG C~390 DEG C, and volume space velocity is 0.8~2.0
h-1, hydrogen to oil volume ratio 300: 1~2000: 1.
10. according to the method described in claim 1, it is characterized by: supplementing the behaviour in hydrofining reaction area described in step (3)
Make condition are as follows: 3.0~16.0MPa of reaction pressure；Average reaction temperature is 250 DEG C~370 DEG C；0.1~6.0 h of volume space velocity-1；
Hydrogen to oil volume ratio 200: 1~2000: 1.
11. according to the method described in claim 10, it is characterized by: supplement hydrofining reaction area described in step (3)
Operating condition are as follows: reaction pressure is the MPa of 6.0MPa~12.0；Average reaction temperature is 270 DEG C~290 DEG C；Volume space velocity is
0.5~3.0 h-1；Hydrogen to oil volume ratio is 300: 1~1500: 1.
12. according to the method described in claim 1, it is characterized by: in hydrocracking reaction area mixing pour point depression catalyst, or
Pour point depression reaction zone is set after hydrocracking reaction area, to reduce the freezing point or condensation point of product.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| WO2022150097A1 (en) * | 2021-01-07 | 2022-07-14 | Saudi Arabian Oil Company | Distillate hydrocracking process with an n-paraffins separation step to produce a high octane number isomerate stream and a steam pyrolysis feedstock |
| US11807818B2 (en) | 2021-01-07 | 2023-11-07 | Saudi Arabian Oil Company | Integrated FCC and aromatic recovery complex to boost BTX and light olefin production |
| US11820949B2 (en) | 2021-01-15 | 2023-11-21 | Saudi Arabian Oil Company | Apparatus and process for the enhanced production of aromatic compounds |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114456838B (en) * | 2020-10-22 | 2023-01-10 | 中国石油化工股份有限公司 | Production method of ethylene steam cracking raw material |
| 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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| US11820949B2 (en) | 2021-01-15 | 2023-11-21 | Saudi Arabian Oil Company | Apparatus and process for the enhanced production of aromatic compounds |
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| CN107177374A (en) | 2017-09-19 |
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