CN107177376B - A kind of method that straight-run diesel oil is hydrocracked production jet fuel - Google Patents
A kind of method that straight-run diesel oil is hydrocracked production jet fuel Download PDFInfo
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- CN107177376B CN107177376B CN201610132500.XA CN201610132500A CN107177376B CN 107177376 B CN107177376 B CN 107177376B CN 201610132500 A CN201610132500 A CN 201610132500A CN 107177376 B CN107177376 B CN 107177376B
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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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
- C10G2300/1048—Middle distillates
- C10G2300/1055—Diesel having a boiling range of about 230 - 330 °C
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
- C10G2300/1048—Middle distillates
- C10G2300/1059—Gasoil having a boiling range of about 330 - 427 °C
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a kind of methods that straight-run diesel oil is hydrocracked production jet fuel, it include: that (1) straight-run diesel oil raw material mixes not through hydrogenated processing with hydrogen, it is directly entered and is hydrocracked-pour point depression reaction zone, it is successively contacted with hydrocracking catalyst and pour point depression catalyst, carries out being hydrocracked-pour point depression reaction；(2) the full fraction reaction product that step (1) obtains is after cooling down, and into hydrofining reaction area, under conditions of relative low temperature and/or large volume air speed, carries out aromatic hydrogenation saturation, hydrodesulfurization, hydrodenitrogeneration reaction；(3) the full fraction product after the purification that step (2) obtains obtains naphtha, jet fuel product into separation fractionating system.Compared with prior art, straight-run diesel oil maximum can be produced as jet fuel by the method for the present invention.
Description
Technical field
The present invention relates to a kind of production methods of jet fuel, especially a kind of to be hydrocracked by straight-run diesel oil to produce
The production method of high-quality jet 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) (US 4172815) discloses single hop circulation plus hydrogen a kind of while that produce jet fuel and diesel oil and splits
Change method, process flow are as follows: heavy raw oil after being hydrocracked, product by fractionation, obtain jet fuel fraction,
Diesel oil distillate and tail oil；Jet fuel fraction is completely or partially mixed with tail oil, sends hydrocracking reactor back to.This process flow
Apparent, the disadvantage is that although jet fuel is hydrocracked again improves quality, its yield reduces more, hydrogen consumption and increases, and
Investment also increases more.
United States Patent (USP) (US 5026472) 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 distillate) method.The method of the present invention fully considers the structure-activity relationship of jet fuel property and hydrocarbon structure composition, by excellent
Catalyst system and optimization technological process and condition are selected, jet fuel will be converted into compared with multicomponent in straight-run diesel oil raw material, and protect
Higher jet fuel product yield is held, jet fuel freeze is reduced.
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 raw material mixes not through hydrogenated processing with hydrogen, is directly entered and is hydrocracked-pour point depression reaction zone, according to
It is secondary to be contacted with hydrocracking catalyst and pour point depression catalyst, it carries out being hydrocracked-pour point depression reaction；
(2) the full fraction reaction product that step (1) obtains is after cooling down, into hydrofining reaction area, in relative low temperature
And/or under conditions of large volume air speed, carry out the unsaturated hydrocarbons such as aromatic hydrocarbons adds the reaction such as hydrogen saturation, hydrodesulfurization, hydrodenitrogeneration；
(3) the full fraction product after the purification that step (2) 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 atmospheric tower
Fraction is 220 DEG C of the initial boiling point any fractions done within the scope of 380 DEG C, and initial boiling point is generally 290~340 DEG C, is done general
It is 330~380 DEG C, the general 100 μ g/g of < of nitrogen content, sulfur content > 2000 μ g/g.The alkane mass content of straight-run diesel oil raw material
Generally 30%~60%, preferably 35%~55%.The aromatics quality content of straight-run diesel oil raw material is generally 10%~35%, preferably
15%~30%.
Hydrocracking catalyst used in step (1) hydrocracking reaction area is existing goods catalyst or presses existing side
The catalyst of method preparation.Be specifically as follows Fushun Petrochemical Research Institute's development and production 3901,3973,3974, FC-16, FC-
26, or mixtures thereof catalyst such as FC-40, FC-50, DHC-8, DHC-32 of Uop Inc.'s development and production, HC-115, HC-215,
Or mixtures thereof catalyst such as HC-110, HC-120LT.Also it can according to need, according to it is well known that method is voluntarily prepared point
The son sieve satisfactory hydrocracking catalyst of content.The hydrocracking catalyst is generally with VI B race and/or VIII race's metal
Active metal component, the content of Y molecular sieve is 3~30wt% in catalyst, preferably 15~25wt%, and molecular sieve can be Y points
Son sieve and/or beta-molecular sieve.Molecular sieve can be modified according to conventional method in that art.Such as the lattice constant of modified Y molecular sieve
Generally 2.425~2.435nm, preferably 2.425 to less than 2.435nm(2.425~< 2.435nm), modified Y molecular sieve
SiO2/Al2O3Molar ratio is generally 5.0~50.0, and relative crystallinity is 90~120%.
In the method for the present invention, the pour point depression catalyst is the conventional pour point depression catalyst in this field, as hydro dewaxing is urged
Agent, isomerization-visbreaking catalyst etc..The catalyst includes containing shape slective cracking molecular sieve or isomery performance molecular sieve etc..Institute
The shape slective cracking molecular sieve stated is hydrogen type molecular sieve, and the molecular sieve can be selected from Hydrogen ZSM-5, ZSM-11, ZSM-12, ZSM-
22, one of ZSM-23, ZSM-35 and ZSM-38 molecular sieve or a variety of, preferably ZSM-5 molecular sieve；The shape slective cracking molecule
The silica alumina ratio of sieve is generally 10~150, preferably 20~120.Hydrogenation active metals described in pour point depression catalyst can be with
The group VIII and/or group vi metallic element in the periodic table of elements, wherein group VIII active metal can be Ni and/or
Co, group vi active metal are W and/or Mo.On the basis of the weight of catalyst, hydrogenation active metal component is in terms of oxide
Content is 10%~25%, is 50%~90% containing shape slective cracking molecular sieve silica-alumina supports content, wherein shape slective cracking molecular sieve exists
Content is 10%~40% in silica-alumina supports, remaining is aluminium oxide.The Hydrodewaxing catalyst can choose existing various
Commercial catalysts, such as the hydro dewaxings catalysis such as FDW-1, FDW-3 that Fushun Petrochemical Research Institute (FRIPP) develops
Agent；Also can according to need and prepared by the common sense of this field, for example, be referred to CN1952074A, CN1352231A,
Content disclosed in CN101143333A, CN102451748A prepares satisfactory Hydrodewaxing catalyst.Pour point depression catalyst
Volumetric usage is the 20%~120% of hydrocracking catalyst, preferably 30%~80%.
Step is hydrocracked described in (1)-operating condition of pour point depression reaction zone are as follows: reaction pressure 3.0~16.0MPa, and it is excellent
It is selected as 6.0MPa~12.0MPa；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 0.5~2.0 h-1；Hydrogen to oil volume ratio 200: 1~2500: 1, preferably 300: 1~2000: 1.
Catalyst used in step (2) 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 hydrofining reaction area described in step (2) are as follows: 3.0~16.0MPa of reaction pressure, preferably
6.0MPa~12.0MPa；Average reaction temperature is 250 DEG C~320 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 (3) 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 (2) hydrofining reaction area refer to step (1) plus
In comparison, specifically, following two condition at least selects one: (one) step (2) plus hydrogen are smart for hydrogen cracking-pour point depression reaction zone
The reaction temperature of reaction zone processed is hydrocracked than step (1)-and pour point depression reaction zone is 20~100 DEG C low, and it is 40~70 DEG C preferably low；(2)
The volume space velocity in step (2) hydrofining reaction area be step (1) be hydrocracked-pour point depression reaction zone volume space velocity 1.2~5
Times, 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 technical effect.It is controlled by reaction result, it is preferable that at the operating condition in rate-determining steps (2) hydrofining reaction area
In the dynamics Controlling area of aromatic hydrogenation saturation, the arene content in product is effectively reduced.
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) plus hydrogen are split
Change the cooperation of reaction zone and step (2) hydrofining reaction area condition, raw material is not hydrocracked first directly through hydrogenated processing
Cracking.(compared with routine techniques, in conventional hydrocracking reaction, need before material is contacted with hydrocracking catalyst, it will
Sulphur, nitrogen are removed to reduced levels, generally in 10mgg-1Below), organic sulfur compound, organic nitrogen compound and aromatic hydrocarbons are remained, it is special
Be not the organic compounds containing sulfur of macromolecular, these substances on hydrocracking catalyst competitive Adsorption as a result, sending out raw material
Isomerization reaction and cracking reaction collaboration are given birth to, after isomery occurs for alkane, in the competitive Adsorption condition of macromolecular organic sulfur compound
Under, the reaction mechanism mechanism of reaction is changed, the selectivity of purpose product increases, and increases the product yield that can be used for jet fuel obviously
Add.Product after cracking passes through post-refining, can achieve other quality index (mainly smoke point etc.) of jet fuel.But it is former
The nitrogen content of material can not be too high, therefore need to control raw material nitrogen content parameter index.
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 and nitride construct the new reaction mechanism mechanism of reaction, effectively increase spray to the temporary intoxication of hydrocracking catalyst
The yield of gas fuel product.
Straight-run diesel oil and hydrogen, which are mixed into, is hydrocracked-pour point depression reaction zone, is catalyzed with hydrocracking catalyst and pour point depression
Agent successively contacts, and under specific reaction environment, concerted reaction occurs, changes straight-run diesel oil paraffin cracking reaction course,
The yield for being conducive to improve jet fuel, reduces jet fuel freeze, material enters hydrofining reaction area later, relatively low
Under conditions of temperature and/or large volume air speed, the hydrofining reactions such as aromatic hydrogenation saturation are carried out, product unsaturated hydrocarbons is reduced and contains
Amount, but retain the part macromolecular sulfur-containing compound beneficial to jet fuel.Think through research, the absorption of nitride, which is poisoned, to be made
With within a certain period of time, it is suppressed that the cracking activity of hydrocracking catalyst effectively reduces the generation of second pyrolysis reaction,
In addition, in raw material part labyrinth sulfur-containing compound, such as benzothiophenes, oil-source rock correlation be big
There are 2 major class suction types in molecule sulfur-containing compound and hydrocracking catalyst activated centre: π cooperation absorption and sulphur and metal are straight
The M-S key absorption that effect is formed is connect, the activated centre function of hydrocracking catalyst is effectively had adjusted, forms under reactiveness
Steric hindrance catalytic center structure, make alkane isomery, and asymmetry chain rupture is occurred into for the alkane after isomery, subtract simultaneously
The generation of second pyrolysis reaction is lacked, collaboration ensure that the yield of jet fuel product.Exist in a certain amount of organosulfur compound
Under, significant change has occurred in the distribution of straight-run diesel oil isocrackate, and jet fuel yield significantly improves, this is that this field is new
Discovery.In addition, hydrocracking reaction area middle rank is equipped to fill out hydrocracking catalyst and Hydrodewaxing catalyst, give full play to
Two kinds of catalyst couple advantage, and because reactor top hydrocracking reaction is strong exothermal reaction, the reaction of lower part hydro dewaxing
For the endothermic reaction, energy has obtained reasonable utilization, reduces the temperature of reactant outflow reactor, effectively reduces subsequent heat exchange
The load of unit reduces energy consumption.
It is hydrocracked the full fraction product of production, is exchanged heat, temperature is reduced, product is empty in relative low temperature and/or large volume
Under speed, the operating condition of high pressure, hydrofinishing is carried out, due to being usually the dynamics control of aromatic hydrogenation saturation under this operating condition
Therefore area processed can effectively convert aromatic hydrocarbons and unsaturated hydro carbons, further increase jet fuel smoke point.
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 is hydrocracked production jet fuel.
Specific embodiment
The method for being hydrocracked production jet fuel to a kind of straight-run diesel oil of the invention with reference to the accompanying drawing carries out detailed
Explanation.M% indicates mass percent.
As shown in Figure 1, the method flow that a kind of straight-run diesel oil of the invention is hydrocracked production jet fuel is as follows: straight run
Diesel oil 1 and hydrogen 2 are mixed into hydrocracking reactor 3, successively connect with hydrocracking catalyst 4 and Hydrodewaxing catalyst 5
Touching reaction, it is by the low cycloalkane appropriateness open loop of smoke point, the high alkane progress isomery of the high molecule carbon number of freezing point, chain rupture is anti-
It answers.It is then hydrocracked full fraction and generates oil 6 through heat exchange reduction temperature, into hydrofining reaction area 7, in relative low temperature, height
Under conditions of pressure, hydrofining reaction is carried out, the unsaturated hydrocarbons content such as aromatic hydrocarbons is effectively reduced, further increase smoke point, reduces naphthalene
It is hydrocarbon.Production oil 8 enters separation system 9 later, and hydrogen-rich gas 10 after processing, is recycled by circulating hydrogen compressor, is obtained
The liquid product 11 obtained is fractionated into fractionating column 12, obtains gas 13, naphtha 14, jet fuel 15, diesel oil 16.
The method that production jet fuel is hydrocracked to a kind of straight-run diesel oil of the invention followed by specific embodiment
It is further described.
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
FC-50 hydrocracking catalyst, FDW-3 Hydrodewaxing catalyst load in the commercial catalysts of hair, hydrocracking reaction area.Add hydrogen
FF-46 Hydrobon catalyst is loaded in refining reaction area, and the concrete operations process of use is shown in attached drawing 1.Two are used in embodiment
The concatenated form of reactor.Raw material oil nature is shown in Table 1, and catalyst fundamental 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；The feedstock oil of embodiment 4~6 is straight-run diesel oil B, technological operation
Condition and it 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 sulfur content of liquid product is 25 gg-1 after first segment FF-46 reaction zone hydrotreating.
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, process flow is simple, and jet fuel yield is high, 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 sulfur content of * liquid product after first segment FF-46 reaction zone hydrotreating is 57 gg-1.
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 (11)
1. a kind of method that straight-run diesel oil is hydrocracked production jet fuel, including the following contents:
(1) straight-run diesel oil raw material mixes not through hydrogenated processing with hydrogen, is directly entered and is hydrocracked-pour point depression reaction zone, successively with
Hydrocracking catalyst and the contact of pour point depression catalyst carry out being hydrocracked-pour point depression reaction；
(2) the full fraction reaction product that step (1) obtains is after cooling down, into hydrofining reaction area, in relative low temperature and/or
Under conditions of large volume air speed, aromatic hydrogenation saturation, hydrodesulfurization, hydrodenitrogeneration reaction are carried out；It is described " relative low temperature and/
Or large volume air speed " refer to being hydrocracked of step (1)-pour point depression reaction zone in comparison, specifically, following two condition is extremely
Selecting one less: the reaction temperature in (one) step (2) hydrofining reaction area is hydrocracked than step (1)-and pour point depression reaction zone is low
20~100 DEG C；(2) volume space velocity in step (2) hydrofining reaction area is that step (1) is hydrocracked-pour point depression reaction zone volume
1.2~5 times of air speed；
(3) the full fraction product after the purification that step (2) obtains obtains naphtha, jet fuel produces into separation fractionating system
Product.
2. according to the method described in claim 1, it is characterized by: straight-run diesel oil raw material is the bavin that crude oil is obtained through atmospheric tower
Oil distillate is 220 DEG C of the initial boiling point any fractions done within the scope of 380 DEG C, 100 μ g/g of nitrogen content <, sulfur content > 2000 μ g/
g。
3. according to the method described in claim 1, it is characterized by: step (1) pour point depression catalyst volume dosage is to be hydrocracked
The 20%~120% of catalyst.
4. according to the method described in claim 3, it is characterized by: step (1) pour point depression catalyst volume dosage is to be hydrocracked
The 30%~80% of catalyst.
5. according to the method described in claim 1, it is characterized by: be hydrocracked described in step (1)-behaviour of pour point depression reaction zone
Make condition are as follows: reaction pressure is 3.0~16.0MPa, and average reaction temperature is 330 DEG C~420 DEG C, and volume space velocity is 0.1~3.0
h-1, hydrogen to oil volume ratio 200: 1~2500: 1.
6. according to the method described in claim 1, it is characterized by: be hydrocracked described in step (1)-behaviour of pour point depression reaction zone
Make condition are as follows: reaction pressure is 6.0MPa~12.0MPa, and average reaction temperature is 350 DEG C~390 DEG C, volume space velocity 0.5
~2.0 h-1, hydrogen to oil volume ratio 300: 1~2000: 1.
7. according to the method described in claim 1, it is characterized by: the operation item in hydrofining reaction area described in step (2)
Part are as follows: reaction pressure is 3.0~16.0MPa, and average reaction temperature is 250 DEG C~320 DEG C, and volume space velocity is 0.1~6.0 h-1,
Hydrogen to oil volume ratio is 200: 1~2000: 1.
8. according to the method described in claim 1, it is characterized by: the operation item in hydrofining reaction area described in step (2)
Part are as follows: reaction pressure is 6.0MPa~12.0MPa, and average reaction temperature is 270 DEG C~290 DEG C, and volume space velocity is 0.5~3.0
h-1, hydrogen to oil volume ratio 300: 1~1500: 1.
9. according to the method described in claim 1, it is characterized by: the reaction temperature in step (2) hydrofining reaction area is than step
Suddenly (1) be hydrocracked-pour point depression reaction zone is 40~70 DEG C low.
10. according to the method described in claim 1, it is characterized by: the volume space velocity in step (2) hydrofining reaction area is step
Suddenly (1) is hydrocracked -1.5~3 times of pour point depression reaction zone volume space velocity.
11. according to the method described in claim 10, it is characterized by: the volume space velocity in step (2) hydrofining reaction area is
Step (1) is hydrocracked -2~3 times of pour point depression reaction zone volume space velocity.
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5980729A (en) * | 1998-09-29 | 1999-11-09 | Uop Llc | Hydrocracking process |
| US6340430B1 (en) * | 1999-09-15 | 2002-01-22 | Uop Llc | Distillate dewaxing process |
| CN1417298A (en) * | 2001-10-30 | 2003-05-14 | 中国石油化工股份有限公司 | Combined hydrogenation method of producing diesel oil with high cetane number and low solidifying point |
| CN1453338A (en) * | 2002-04-26 | 2003-11-05 | 中国石油化工股份有限公司 | Jet fuel producing process |
| CN101376839A (en) * | 2007-08-27 | 2009-03-04 | 中国石油化工股份有限公司 | Diesel fraction deep hydrogenation method |
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Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5980729A (en) * | 1998-09-29 | 1999-11-09 | Uop Llc | Hydrocracking process |
| US6340430B1 (en) * | 1999-09-15 | 2002-01-22 | Uop Llc | Distillate dewaxing process |
| CN1417298A (en) * | 2001-10-30 | 2003-05-14 | 中国石油化工股份有限公司 | Combined hydrogenation method of producing diesel oil with high cetane number and low solidifying point |
| CN1453338A (en) * | 2002-04-26 | 2003-11-05 | 中国石油化工股份有限公司 | Jet fuel producing process |
| CN101376839A (en) * | 2007-08-27 | 2009-03-04 | 中国石油化工股份有限公司 | Diesel fraction deep hydrogenation method |
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