CN105623705B - Method for producing diesel oil and product diesel oil - Google Patents
Method for producing diesel oil and product diesel oil Download PDFInfo
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- CN105623705B CN105623705B CN201410594508.9A CN201410594508A CN105623705B CN 105623705 B CN105623705 B CN 105623705B CN 201410594508 A CN201410594508 A CN 201410594508A CN 105623705 B CN105623705 B CN 105623705B
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Abstract
The invention discloses a method for producing diesel oil. The method comprises the following steps: carrying out first fractionation on hydrocracking diesel distillate with distillation range of 145-380 DEG C so as to obtain light diesel distillate, medium diesel distillate and heavy diesel distillate; taking out at least part of the medium diesel distillate, taking the light diesel distillate and the heavy diesel distillate or/and the rest part of medium diesel distillate out of a device so as to obtain a product diesel oil, wherein distillation range of the medium diesel distillate is 205-300 DEG C. The invention also discloses a product diesel oil produced by the above method. By the method, diesel quality of an existing hydrocracking unit can be economically and flexibly raised. Specifically, by the method, density of hydrocracked whole fraction diesel oil can be reduced, and cetane number of the product diesel oil can be raised.
Description
Technical field
The present invention relates to a kind of method for producing diesel oil and a kind of product diesel oil.
Background technology
In recent years, with the Deep mining of global crude oil, crude quality becomes worse and worse, and relative density and sulfur content are not
It is disconnected to rise；And world's refined products market, towards the increase in demand of intermediate oil (diesel oil and kerosene), the demand of heavy fuel oil is continuous
The direction of reduction is developed.Therefore, oil, as a kind of non-renewable energy, is adequately and reasonably to implement money using its heavy distillat
The important means of source sustainable development.
In China, on the one hand, with developing rapidly for national economy, light-weight fuel oil demand is continuously increased, especially
Demand amplification to diesel oil is bigger；On the other hand, while oil product increase in demand, the lifting of product quality turns into oil refining enterprise
The bigger challenge for facing.Hydrocracking technology is important secondary operation means, can be obtained while heavy oil lighting is realized
Meet the cleaning products of environmental requirement.Therefore, development and application hydrocracking technology turns into the maximally effective hand that solves the above problems
Section.Currently, corresponding with crude quality variation, charging in poor quality, the degree of heaviness of hydrocracking unit are also constantly being deepened.
One of outstanding feature that hydrocracking unit charging is deteriorated is that raw material aromatic hydrocarbons and naphthene content amplification are obvious, and its change can influence
To the quality of diesel oil.
At present, new national standard is to the quality requirement more and more higher of diesel product, except to sulphur, nitrogen content and other impurity in diesel oil
There is strict demand outer, further requirement also is proposed to density and Cetane number.For example in GB 19147-2013 require No. 5
To-No. 10 diesel oil densities in 810-850kg/m3In the range of, Cetane number is not less than 51；- No. 20 diesel oil densities are in 790-
840kg/m3Scope, Cetane number is not less than 49；- 35 and-No. 50 diesel oil densities in 790-840kg/m3Scope, Cetane number is not
Less than 47.
For Petrochemical Enterprises, to pursue high yield, expect that hydrocracking unit can process heavier, faulty wax oil cut,
Also need to obtain qualified product simultaneously.However, being generated very with the diesel product specification for increasingly improving the characteristics of charging inferior
Big contradiction.
It is to reduce diesel oil density, raising diesel oil 16 by improving conversion level for existing hydrocracking process
After the effective ways of alkane value, but raising conversion level, diesel yield can accordingly decline (for full conversion process)；Also hydrogen consumption increases
Plus, accordingly growth etc. is negatively affected for lighter hydrocarbons and light naphthar.In addition, how to be increased substantially for existing hydrocracking unit
Conversion level also has the difficulty in specific implementation.CN101117594A discloses a kind of method of hydrotreating for producing cleaning diesel oil.Should
Method enters the second hydroconversion reaction zone after feedstock oil is mixed with circulating hydrogen, is carried out in the presence of Hydrobon catalyst anti-
Should, lightweight, heavier diesel fraction are obtained, part or all of heavier diesel fraction enters the first hydrogenation reaction after mixing with new hydrogen
Area, continues to react with catalyst for hydro-upgrading, and remaining heavy diesel fuel is with the mixed diesel oil distillate of light diesel fuel as product diesel oil.Should
The treatment of heavier diesel fraction repeated hydrogenation for processing high-sulfur, nitrogen high and doing diesel oil distillate high, but is failed to provide by method
Diesel oil density and the method for improving Cetane number are reduced simultaneously.
CN101210198A discloses a kind of method of hydrotreating for producing fine-quality diesel oil and high-quality reformer feed.The method is by bavin
Oil and/or the hydrogenated cracking reaction of light wax oil raw material obtain naphtha, kerosene, diesel oil and tail oil, wherein being voluminous reformer feed
Can select (175-230 DEG C) circulation freshening of kerosene distillate.However, how the prior art is not mentioned for inferior raw material yet
Diesel oil density and the method for improving Cetane number are reduced simultaneously.
CN103013559A discloses a kind of method for hydrogen cracking of selective increasing of aviation kerosene yield.The method is by heavy diesel fuel cut
(320-370 DEG C) returns to feedstock oil and carries out continuation reaction together, wherein, circulation heavy diesel fuel cut accounts for the matter of gross weight diesel oil distillate
Amount percentage is 10-100%.However, the method does not suggest that the scheme for how improving diesel oil distillate quality.
At present, for hydrocracking raw material inferior and its further process technology of poor diesel oil distillate mainly include with
Descend some：(1) it is refined (reducing refining stage air speed) using multistage；(2) by the poor diesel oil distillate of property by further reaction,
Production catalytic reforming feedstock；(3) light diesel fuel cut (kerosene distillate) is partly or entirely extracted out, circulation cracking generation catalytic reforming feedstock；Or
Diesel oil distillate higher will be done to extract out, further cracking produces qualified diesel oil distillate.However, multistage is refined can increase extra
Operating cost, additionally, for epipodium paraffinic feedstock, effect is also limited；The Cetane number of heavy distillat diesel oil is higher, further to its
Cracking will influence the Cetane number of integral product diesel oil.
For existing hydrocracking unit, under the obvious big situation of feed properties in poor quality trend, how it is improved
Diesel quality, it is a problem demanding prompt solution especially to take into account diesel oil density and Cetane number.
The content of the invention
The purpose of the present invention is the defect for overcoming prior art, there is provided one kind can be economical and neatly improves existing hydrogenation
The method of cracking unit diesel quality, specifically, the method for the present invention enable to be hydrocracked the density reduction of diesel oil and
The Cetane number of product diesel oil is improved simultaneously.
The present inventor has found that become weight with boiling range, the boiling range density of the narrow fraction of different cut points is simultaneously under study for action
Linearly increasing trend is not presented, but the variation tendency of approximate index as shown in table 1 is presented；In contrast, different cuttings
The Cetane number of the narrow fraction of point is then presented the variation tendency of approximate log as shown in table 2, and, both have very strong phase
Closing property and complementarity.Therefore, the present inventor thinks, accordingly, if can optionally in the middle of extraction section
Cut, then can take into account diesel oil density and the aspect of Cetane number two, with less cost, obtain that density is low, Cetane number number compared with
Product diesel oil high.So as to the present inventor completes technical scheme accordingly.
The difference of the full cut diesel oil of table 1 fritters the density of cut
| Boiling range scope (DEG C) | 20 DEG C of density (g/mL) |
| 145-175 | 0.776 |
| 175-205 | 0.802 |
| 205-235 | 0.822 |
| 235-270 | 0.828 |
| 270-300 | 0.832 |
| 300-330 | 0.830 |
| 330-370 | 0.827 |
The difference of the full cut diesel oil of table 2 fritters the Cetane number of cut
| Boiling range scope (DEG C) | Cetane lndex |
| 145-175 | 35.5 |
| 175-205 | 39.2 |
| 205-235 | 42.8 |
| 235-270 | 53.1 |
| 270-300 | 62.2 |
| 300-330 | 75.5 |
| 330-370 | 85.0 |
To achieve these goals, on the one hand, the present invention provides a kind of method for producing diesel oil, the method includes：To evaporate
Journey carries out the first fractionation for 145-380 DEG C of the diesel oil distillate that is hydrocracked, and obtains light diesel cut, middle matter diesel oil distillate and weight
Matter diesel oil distillate；Take out at least partly middle matter diesel oil distillate, and by the light diesel cut and heavier diesel fraction or
Matter diesel oil distillate goes out device in person and remainder, obtains product diesel oil, wherein, the boiling range of the middle matter diesel oil distillate is
205-300℃。
On the other hand, the present invention provides a kind of product diesel oil obtained by the above method of the invention production.
The present invention is by optionally extracting from full cut diesel oil at least part of boiling range out in the range of 205-300 DEG C
Matter diesel oil distillate, and by light diesel cut and heavier diesel fraction or and the middle matter diesel oil distillate of remainder go out dress
Put, can access density reduction, and cetane number boost quality product diesel oil.And, produced using the method for the present invention
During above-mentioned quality product diesel oil, compared with the method that other raisings are hydrocracked diesel quality, at least partly specific diesel oil is extracted out
During cut, it is only necessary to which the fractionating column in fractionating system is transformed, and change smaller, cost is relatively low；On the other hand, it is of the invention
The method operating cost is relatively low, and extracted amount can be adjusted according to the charging of device and its service cycle, relatively more flexibly.
Other features and advantages of the present invention will be described in detail in subsequent specific embodiment part.
Specific embodiment
Specific embodiment of the invention is described in detail below.It should be appreciated that described herein specific
Implementation method is merely to illustrate and explain the present invention, and is not intended to limit the invention.
In the present invention, described " first ", " second ", " the 3rd " do not represent sequencing, only for distinguishing, this area skill
Art personnel should not be construed as the limitation to technical scheme.
On the one hand, the present invention provides a kind of method for producing diesel oil, and the method includes：By boiling range for 145-380 DEG C plus
Hydrogen cracked diesel oil cut carries out the first fractionation, obtains light diesel cut, middle matter diesel oil distillate and heavier diesel fraction；It is taken out to
Middle matter diesel oil distillate described in small part, and by the light diesel cut and heavier diesel fraction or and remainder in matter
Diesel oil distillate goes out device, obtains product diesel oil, wherein, the boiling range of the middle matter diesel oil distillate is 205-300 DEG C.
In method of the present invention, " at least partly middle matter diesel oil is taken out due to being used in the method for the present invention
The means of cut ", therefore, it is described " by the light diesel cut and heavy bavin when the taking-up part middle matter diesel oil distillate
Oil distillate or and remainder in matter diesel oil distillate go out device " refer to：The light diesel cut and heavy diesel are evaporated
Divide and the middle matter diesel oil distillate of remainder goes out device.When take out all the middle matter diesel oil distillate when, it is described " will it is described gently
Matter diesel oil distillate and heavier diesel fraction or and remainder in matter diesel oil distillate go out device " refer to：By the lightweight bavin
Oil distillate and heavier diesel fraction go out device.
In the present invention, refer to that cutting is hydrocracked diesel oil when the boiling range of the middle matter diesel oil distillate is 205-300 DEG C
The cut point that cut obtains light diesel cut, middle matter diesel oil distillate and heavier diesel fraction is respectively 205 DEG C and 300 DEG C, under
Similarly, the present invention is repeated no more to this for the specific declaration of will of the boiling range on middle matter diesel oil distillate in text.
In the present invention, boiling range includes that 205 DEG C and 300 DEG C of two endpoint values take for 205-300 DEG C of middle matter diesel oil distillate
The cut for obtaining, correspondingly, the cut that light diesel cut is obtained when not including 205 DEG C, and heavier diesel fraction does not include 300 DEG C
When the cut that obtains, remaining is similar to, no longer describes in detail.
Density reduction can just be obtained by the above method provided using the present invention, and the high-quality of cetane number boost is produced
Product diesel oil.And, the above method that the present invention is provided only needs to transform the fractionating column in fractionating system, and changes smaller,
Cost is relatively low；And, above method operating cost of the invention is relatively low, and extracted amount can be according to the charging of device and its operating week
Phase is adjusted, relatively more flexibly.
According to method of the present invention, to it is described be hydrocracked diesel oil distillate and carry out the method and condition of the first fractionation do not have
There is special restriction, those skilled in the art can be carried out using conventional use of various methods, as long as the present invention can be obtained
Described light diesel cut, middle matter diesel oil distillate and heavier diesel fraction.The present invention will not be repeated here.
According to method of the present invention, in order that the quality for obtaining obtained product diesel oil can be obtained greatly
Improve, the boiling range of the present invention preferably middle matter diesel oil distillate is 205-235 DEG C.
According to method of the present invention, in order that the quality for obtaining obtained product diesel oil can be obtained greatly
Improve, the boiling range of the present invention preferably middle matter diesel oil distillate is 235-270 DEG C.
According to method of the present invention, in order that the quality for obtaining obtained product diesel oil can be obtained greatly
Improve, the boiling range of the present invention preferably middle matter diesel oil distillate is 205-270 DEG C.
Under preferable case, in method of the present invention, the middle matter diesel oil distillate and the mass ratio of product diesel oil of taking-up
Can be 0.1-1：1.
In the case of more preferably, in method of the present invention, the middle matter diesel oil distillate and the quality of product diesel oil of taking-up
Than that can be 0.12-0.8：1.
According to method of the present invention, the diesel oil distillate that is hydrocracked can be hydrocracked by by feedstock oil
And obtain.
There is no particular limitation to the condition being hydrocracked for method of the present invention, and those skilled in the art can be with
Selected in the range of various parameters commonly used in the art according to actual needs.In order that must be by the method for the present invention
The density of the product diesel oil of acquisition reduces more and Cetane number increase rate is bigger, and the method for the present invention is preferably described to be added
The condition of hydrogen cracking includes：Temperature is 320-440 DEG C, and pressure is 5-20MPa, and volume space velocity is 0.1-4h during liquid-1, hydrogen oil volume
Than being 400-2000：1.
According to method of the present invention, the diesel oil distillate that is hydrocracked can be for 20% relative to the yield of feedstock oil
More than；Preferably more than 40%；More preferably more than 50%.
According to the present invention, methods described can also be adopted to be carried out with the following method：By by obtaining after hydrocracking reaction
Product stream carries out gas-liquid separation and the 3rd fractionation successively, in the 3rd fractional distillation process, collects lightweight bavin of the present invention
Oil and heavy diesel or and remainder in matter diesel oil, that is, obtain product diesel oil of the present invention.
According to method of the present invention, to the species of the feedstock oil, there is no particular limitation, under preferable case, when adopting
Inferior feedstock oil is processed with method of the present invention, such as when catalytic cracking diesel oil, decompressed wax oil and wax tailings, can be made
The quality for obtaining product diesel oil obtains more obvious improvement.
According to method of the present invention, the density drop of diesel oil distillate is hydrocracked described in the density ratio of the product diesel oil
Low 0.0007-0.0068g/mL；The Cetane number of the product diesel oil is than the cetane number boost for being hydrocracked diesel oil distillate
0.9-11 high.
According to method of the present invention, the method can also include：In presence of hydrogen, under hydrocracking condition,
Feedstock oil is contacted with hydrocracking catalyst, isocrackate is obtained；The isocrackate is cooled down successively
And separation, hydrogen-rich gas and liquid phase thing are obtained, then the liquid phase thing is carried out into after-fractionating, obtain naphtha cut, tail oil and evaporate
Point and the boiling range be hydrocracked diesel oil distillate for 145-380 DEG C.
There is no particular limitation to the cooling and separate method and apparatus equipment for the present invention, and those skilled in the art can
Selected with using various methods commonly used in the art, the present invention will not be repeated here.
A kind of specific preferred embodiment of the invention, the method for the present invention includes：
(1) in presence of hydrogen, under hydrocracking condition, feedstock oil is contacted with hydrocracking catalyst, is added
Hydrogen crackate, the isocrackate is cooled down and separated successively, obtains hydrogen-rich gas and liquid phase thing, then will be described
Liquid phase thing carries out after-fractionating, obtains the diesel oil that is hydrocracked that naphtha cut, tail oil fraction and boiling range are 145-380 DEG C and evaporates
Point；
(2) diesel oil distillate that is hydrocracked is carried out into first fractionation, obtains light diesel cut, middle matter diesel oil and evaporate
Divide and heavier diesel fraction；
(3) take out at least partly middle matter diesel oil distillate, and by the light diesel cut and heavier diesel fraction or
Matter diesel oil distillate goes out device in person and remainder, obtains product diesel oil.
In the present invention, to the species of the hydrocracking catalyst, there is no particular limitation, it is possible to use in the art
The conventional use of various hydrocracking catalysts for carrying out hydrocracking reaction.In the present invention, it is additionally may included in institute
Load appropriate well known to a person skilled in the art pretreating catalyst by hydrocracking before stating hydrocracking catalyst bed.
On the other hand, the present invention provides a kind of product diesel oil obtained by the above method of the invention production.
The above method of the invention has the following advantages that：
1st, the method provided using the present invention, can effectively improve the matter of diesel oil under conditions of reaction system is not changed
Amount, is embodied in：Take into account reduction diesel oil density and improve the aspect of diesel cetane-number two, produce qualified or high-quality product bavin
Oil；
2nd, the method for the present invention can be used for hydrocracking unit raw material variation or operate latter stage catalyst activity reduction
In the case of, extract out by the appropriate cutting to specific cut and selectively so as to improve diesel quality, reach the qualified diesel oil of production
Target.
Below will the present invention will be described in detail by embodiment.
The diesel oil distillate that is hydrocracked used in following examples and comparative example is obtained by the following method：
In presence of hydrogen, under hydrocracking condition, by Middle East decompressed wax oil and research institute of Sinopec
RN-32V (pretreating catalyst by hydrocracking) and RHC-3 catalyst (hydrocracking catalyst) contact of exploitation, are hydrogenated with
Crackate, the isocrackate is cooled down and separated successively, obtains hydrogen-rich gas and liquid phase thing, then by the liquid
Phase thing carries out after-fractionating, obtains the diesel oil that is hydrocracked that naphtha cut, tail oil fraction and the boiling range are 145-380 DEG C and evaporates
Divide (property is shown in Table 3), wherein, the hydrocracking condition is：Temperature is 365 DEG C, and pressure is 14MPa, and volume space velocity is during liquid
1.4h-1, hydrogen to oil volume ratio is 800：1.
Embodiment 1
The diesel oil distillate that is hydrocracked by boiling range for 145-380 DEG C carries out the first fractionation, obtains light diesel cut, middle matter
Diesel oil distillate and heavier diesel fraction；Matter diesel oil distillate in whole is taken out, and the light diesel cut and heavy diesel are evaporated
Separate device, obtain product diesel oil, the property of each cut as shown in table 3, wherein, the middle matter diesel oil distillate of extraction with go out device
Product diesel quality ratio is 0.74：1.
Table 3
From table 3 it can be seen that with full cut diesel oil (as it is of the invention it is foregoing be hydrocracked diesel oil distillate, similarly hereinafter) phase
Than, 0.0068g/mL is reduced by the density for extracting the product mix diesel oil that specific middle matter diesel oil distillate scheme is obtained out, and ten
Six alkane value numbers increased 11 units.
Comparative example 1
This comparative example is carried out using method similar to Example 1, except that：
Using the light diesel cuts that extraction is whole in this comparative example, and middle matter diesel oil distillate and heavier diesel fraction are gone out
Device, obtains product diesel oil, and the property of each cut is as shown in table 4, wherein, light diesel cut and the product for going out device of extraction
Diesel quality ratio is 0.36：1.
Table 4
From table 4, it can be seen that compared with full cut diesel oil, the product diesel oil that the method for light diesel cut is obtained is extracted out
Density 0.0105g/mL high, Cetane number number increased 5 units；But (it is shown in Table 3) compared with matter diesel oil distillate in selecting to extract out,
The product diesel oil density about 0.0173g/mL high for obtaining, while Cetane number number also reduces about 6 units, from density and 16
The aspect of alkane value number two is not as good as the method proposed in the embodiment of the present invention 1.
Comparative example 2
This comparative example is carried out using method similar to Example 1, except that：
Using the heavier diesel fractions that extraction is whole in this comparative example, and light diesel cut and middle matter diesel oil distillate are gone out
Device, obtains product diesel oil, the property of each cut as shown in table 5, wherein, the heavier diesel fraction of extraction and the product for going out device
Diesel quality ratio is 0.45：1.
Table 5
As can be seen from Table 5, compared with full cut diesel oil, the product diesel oil that obtains of method of heavier diesel fraction is extracted out
The low 0.0053g/mL of density, Cetane number number reduces about 8 units；But (it is shown in Table compared with matter diesel oil distillate in selecting to extract out
3) the product diesel oil density 0.0015g/mL high for, obtaining, while Cetane number number also reduces about 19 units, from density and ten
The aspect of six alkane value number two is not as good as the method proposed in the embodiment of the present invention 1.
Embodiment 2
The present embodiment is carried out using method similar to Example 1, except that：
The boiling range of the middle matter diesel oil distillate of the present embodiment is 205-235 DEG C.
The property of each cut of the present embodiment is as shown in table 6, wherein, middle matter diesel oil distillate and the product for going out device of extraction
Diesel quality ratio is 0.17：1.
Table 6
| Raw material | The full cut of diesel oil | Go out device product diesel oil distillate |
| Boiling range scope (DEG C) | 145-380 | The mixed fraction of 145-205 and 235-380 |
| Yield (%) | 51.7 | 44.3 |
| Density (20 DEG C)/(g/mL) | 0.8174 | 0.8167 |
| Boiling range (D-86) | ||
| Initial boiling point (DEG C) | 145 | 145 |
| 10 volumes % (DEG C) | 182 | 178 |
| 30 volumes % (DEG C) | 217 | 218 |
| 50 volumes % (DEG C) | 259 | 272 |
| 70 volumes % (DEG C) | 292 | 303 |
| 90 volumes % (DEG C) | 337 | 340 |
| 95 volumes % (DEG C) | / | 359 |
| The end point of distillation (DEG C) | 380 | 379 |
| Cetane number number | 54.4 | 57.4 |
Embodiment 3
The present embodiment is carried out using method similar to Example 1, except that：
The boiling range of the middle matter diesel oil distillate of the present embodiment is 235-270 DEG C.
The property of each cut of the present embodiment is as shown in table 7, wherein, middle matter diesel oil distillate and the product for going out device of extraction
Diesel quality ratio is 0.18：1.
Table 7
| Raw material | The full cut of diesel oil | Go out device product diesel oil distillate |
| Boiling range scope (DEG C) | 145-380 | The mixed fraction of 145-235 and 270-380 |
| Yield (%) | 51.7 | 43.7 |
| Density (20 DEG C)/(g/mL) | 0.8174 | 0.8156 |
| Boiling range (D-86) | ||
| Initial boiling point (DEG C) | 145 | 145 |
| 10 volumes % (DEG C) | 182 | 177 |
| 30 volumes % (DEG C) | 217 | 207 |
| 50 volumes % (DEG C) | 259 | 261 |
| 70 volumes % (DEG C) | 292 | 304 |
| 90 volumes % (DEG C) | 337 | 341 |
| 95 volumes % (DEG C) | / | 360 |
| The end point of distillation (DEG C) | 380 | 380 |
| Cetane number number | 54.4 | 55.3 |
Embodiment 4
The present embodiment is carried out using method similar to Example 1, except that：
The boiling range of the middle matter diesel oil distillate of the present embodiment is 205-270 DEG C.
The property of each cut of the present embodiment is as shown in table 8, wherein, middle matter diesel oil distillate and the product for going out device of extraction
Diesel quality ratio is 0.42：1.
Table 8
| Raw material | The full cut of diesel oil | Go out device product diesel oil distillate |
| Boiling range scope (DEG C) | 145-380 | The mixed fraction of 145-205 and 270-380 |
| Yield (%) | 51.7 | 36.3 |
| Density (20 DEG C)/(g/mL) | 0.8174 | 0.8143 |
| Boiling range (D-86) | ||
| Initial boiling point (DEG C) | 145 | 145 |
| 10 volumes % (DEG C) | 182 | 173 |
| 30 volumes % (DEG C) | 217 | 200 |
| 50 volumes % (DEG C) | 259 | 287 |
| 70 volumes % (DEG C) | 292 | 314 |
| 90 volumes % (DEG C) | 337 | 344 |
| 95 volumes % (DEG C) | / | 362 |
| The end point of distillation (DEG C) | 380 | 380 |
| Cetane number number | 54.4 | 61.6 |
The preferred embodiment of the present invention described in detail above, but, the present invention is not limited in above-mentioned implementation method
Detail, in range of the technology design of the invention, various simple variants can be carried out to technical scheme, this
A little simple variants belong to protection scope of the present invention.
It is further to note that each particular technique feature described in above-mentioned specific embodiment, in not lance
In the case of shield, can be combined by any suitable means, in order to avoid unnecessary repetition, the present invention to it is various can
The combination of energy is no longer separately illustrated.
Additionally, can also be combined between a variety of implementation methods of the invention, as long as it is without prejudice to originally
The thought of invention, it should equally be considered as content disclosed in this invention.
Claims (14)
1. a kind of method for producing diesel oil, the method includes：The diesel oil distillate that is hydrocracked by boiling range for 145-380 DEG C carries out the
One fractionation, obtains light diesel cut, middle matter diesel oil distillate and heavier diesel fraction；At least partly middle matter diesel oil is taken out to evaporate
Point, and by the light diesel cut and heavier diesel fraction or and remainder in matter diesel oil distillate go out device, obtain
Product diesel oil, wherein, the boiling range of the middle matter diesel oil distillate is 205-300 DEG C.
2. method according to claim 1, wherein, the boiling range of the middle matter diesel oil distillate is 205-235 DEG C.
3. method according to claim 1, wherein, the boiling range of the middle matter diesel oil distillate is 235-270 DEG C.
4. method according to claim 1, wherein, the boiling range of the middle matter diesel oil distillate is 205-270 DEG C.
5. the method according to any one in claim 1-4, wherein, the middle matter diesel oil distillate of taking-up and product diesel oil
Mass ratio is 0.1-1：1.
6. method according to claim 5, wherein, the middle matter diesel oil distillate of taking-up and the mass ratio of product diesel oil are
0.12-0.8：1.
7. method according to claim 1, wherein, the method includes：In presence of hydrogen, under hydrocracking condition,
Feedstock oil is contacted with hydrocracking catalyst, isocrackate is obtained；The isocrackate is cooled down successively
And separation, hydrogen-rich gas and liquid phase thing are obtained, then the liquid phase thing is carried out into after-fractionating, obtain naphtha cut, tail oil and evaporate
Point and the boiling range be hydrocracked diesel oil distillate for 145-380 DEG C.
8. method according to claim 7, wherein, the hydrocracking condition includes：Temperature is 320-440 DEG C, pressure
It is 5-20MPa, volume space velocity is 0.1-4h during liquid-1, hydrogen to oil volume ratio is 400-2000：1.
9. method according to claim 7, wherein, the feedstock oil includes catalytic cracking diesel oil, decompressed wax oil and coking
Wax oil.
10. method according to claim 7, wherein, the yield for being hydrocracked diesel oil distillate is more than 20%.
11. methods according to claim 10, wherein, the yield for being hydrocracked diesel oil distillate is more than 40%.
12. methods according to claim 11, wherein, the yield for being hydrocracked diesel oil distillate is more than 50%.
13. methods according to claim 1, wherein, it is hydrocracked diesel oil distillate described in the density ratio of the product diesel oil
Density reduction 0.0007-0.0068g/mL；The Cetane number of the product diesel oil is hydrocracked the ten of diesel oil distillate than described
Six alkane values raise 0.9-11.
The product diesel oil that the 14. method production as described in any one in claim 1-13 is obtained.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410594508.9A CN105623705B (en) | 2014-10-29 | 2014-10-29 | Method for producing diesel oil and product diesel oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410594508.9A CN105623705B (en) | 2014-10-29 | 2014-10-29 | Method for producing diesel oil and product diesel oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105623705A CN105623705A (en) | 2016-06-01 |
| CN105623705B true CN105623705B (en) | 2017-05-24 |
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| CN101144029A (en) * | 2007-09-21 | 2008-03-19 | 袁培林 | Catalytic cracking processing technique for inferior oil material |
| CN101210198A (en) * | 2006-12-27 | 2008-07-02 | 中国石油化工股份有限公司 | Hydrogenation method for producing high grade diesel oil and high grade reforming raw material |
| WO2009116989A1 (en) * | 2008-03-17 | 2009-09-24 | Shell Oil Company | Process for the preparation of a middle distillate fuel |
| CN101914389A (en) * | 2009-09-18 | 2010-12-15 | 北京金伟晖工程技术有限公司 | Method for preparing high-quality diesel by double-hydrogenation system |
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| CN101210198A (en) * | 2006-12-27 | 2008-07-02 | 中国石油化工股份有限公司 | Hydrogenation method for producing high grade diesel oil and high grade reforming raw material |
| CN101144029A (en) * | 2007-09-21 | 2008-03-19 | 袁培林 | Catalytic cracking processing technique for inferior oil material |
| WO2009116989A1 (en) * | 2008-03-17 | 2009-09-24 | Shell Oil Company | Process for the preparation of a middle distillate fuel |
| CN101914389A (en) * | 2009-09-18 | 2010-12-15 | 北京金伟晖工程技术有限公司 | Method for preparing high-quality diesel by double-hydrogenation system |
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