CN107033952A - A kind of processing of heavy oil method - Google Patents
A kind of processing of heavy oil method Download PDFInfo
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- CN107033952A CN107033952A CN201610076818.0A CN201610076818A CN107033952A CN 107033952 A CN107033952 A CN 107033952A CN 201610076818 A CN201610076818 A CN 201610076818A CN 107033952 A CN107033952 A CN 107033952A
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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
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Abstract
The present invention relates to oil refining field, a kind of processing of heavy oil method is disclosed, this method comprises the following steps：(1) heavy oil is subjected to vacuum distillation processing, obtains decompressed wax oil and decompression residuum；(2) decompression residuum is subjected to solvent directional separation processing, obtains frivolous coal tar, heavy deasphalted oil and de-oiled asphalt；(3) heavy deasphalted oil and the de-oiled asphalt are subjected to delayed coking processing；(4) the part decompressed wax oil and the part frivolous coal tar are subjected to hydrocracked, treated；(5) wax tailings produced during the hydrocracking tail oil produced during remaining decompressed wax oil, remaining frivolous coal tar, the hydrocracked, treated and delayed coking processing are subjected to catalytic cracking processing.The method that the present invention is provided can improve light oil yield and quality, increase added value of product.
Description
Technical field
The present invention relates to oil refining field, in particular it relates to a kind of processing of heavy oil method.
Background technology
In recent years because the yield of heavy crude constantly increases, in crude oil, residue content is high and lightweight oil content
It is low, and partly external sour crude is constantly introduced, and residual oil weight-lightening becomes countries in the world today oil
One of major subjects of processing.Therefore, rational method processing heavy oil how is selected, just turns into and improves refining
The grand strategy target of oily factory's economic benefit.
Delayed coking is the important method of decompression residuum processing, although cost of investment is relatively low with operating cost,
To the strong adaptability of crude oil, but yield of light oil is low, and low value-added coke output is high, and delayed coking
Product quality is poor, and the particularly coke chemicals containing sulfur feedstock are required to secondary operation.RFCC
It is also the important method of decompression residuum processing, its application is mainly limited by impurity content in feedstock oil, slag
Metal in oil can be deposited causes permanent catalyst deactivation on a catalyst, and is typically only capable of in decompressed wax oil
In mix refining part reduced pressure residual oil.If Vacuum Residue Properties difference mixes refining than improving, need first to decompression residuum
Carry out weighted BMO spaces.Although residual hydrogenation technology develops comparatively fast in recent years, its high investment and behaviour
It is the bottleneck for limiting its development as expense.To make full use of the heavy oil resources light oil with high yield product of preciousness, refining
Factory is passed through frequently with heavy oil Combined machining scheme.
CN1546613A discloses a kind of combined technique for processing heavy oil, utilizes heavy oil fluidized decarburization, residual oil
Hydrotreating and RFCC group technology produce light-weight fuel oil from heavy oil, by decarburization and hydrogenation
Organically combine.CN1844325A discloses a kind of combined technique for processing heavy oil, heavy oil individually or
Handled after being mixed with catalytic cracking clarified oil through solvent deasphalting and obtain deasphalted oil and de-oiled asphalt；De-oiling
Pitch is individually or with progress coking processing after the mixing of another part heavy oil, and obtained coking heavy oil returns to solvent
Deasphalting unit enters heavy oil hydroprocessing units, catalytic cracking unit and hydrocracking unit；De- drip
Blue or green oil individually or with decompressed wax oil, reduced crude, decompression residuum, catalytic cracking recycle oil, coking heavy oil
In one or more of mixing after carry out hydrotreating, improve heavy oil hydroprocessing units feed properties, delay
With heavy oil hydroprocessing units operating condition.CN101050383A is related to a kind of combined technique for processing heavy oil,
Decompression residuum obtains two components of deasphalted oil and de-oiling pitch after being handled through butane deasphalting；Depitching
Oil splits after being mixed with the one or more of other catalytically cracked material reduced crudes, decompressed wax oil as catalysis
Disguise the raw material put, it is difficult to which the catalytic cracked oil pulp of cracking is divided into light oil slurry after vacuum fractionation PROCESS FOR TREATMENT
Two components are starched with plug heavy oil；Light oil is starched and the part de-oiling pitch produced by solvent deasphalting unit
The raw material as viscosity breaking plant is mixed, No. 7 merchantable fuel(s) oil are produced；Plug heavy oil is starched and another portion
De-oiling pitch is divided to be adequately mixed production asphalt for high-grade highway.Related publication also includes
CN101892074A, CN102234536A, CN102234529A, by solvent de-asphalting process, are urged
Change process, catalytic cracked oil pulp plug technique and pitch mediation technique organically to combine, realize
Raw material between each technique is mutually supplied and optimized, and improves reasonability, flexibility and the macroeconomic of processing of heavy oil
Benefit.In the combined technology for processing heavy oil containing solvent deasphalting of document report, deasphalted oil is typically made
It is processed for the raw material of catalytic cracking, light oil yield is not high enough, and catalytically cracked gasoline and diesel quality
It is poor, it is still necessary to following process processing.
The content of the invention
The purpose of the present invention is to overcome during processing of heavy oil of the prior art that light oil yield is high, catalysis
There is provided a kind of processing of heavy oil method with the poor defect of diesel quality for cracking gasoline.
To achieve these goals, the invention provides a kind of processing of heavy oil method, wherein, this method bag
Include following steps：
(1) heavy oil is subjected to vacuum distillation processing, obtains decompressed wax oil and decompression residuum；
(2) decompression residuum is subjected to solvent directional separation processing, obtains frivolous coal tar, takes off again
Coal tar and de-oiled asphalt；
(3) heavy deasphalted oil and the de-oiled asphalt are subjected to delayed coking processing；
(4) the part decompressed wax oil and the part frivolous coal tar are subjected to hydrocracked, treated；
(5) by remaining decompressed wax oil, remaining frivolous coal tar, the hydrocracked, treated mistake
The wax tailings produced during the hydrocracking tail oil produced in journey and delayed coking processing enter
Row catalytic cracking is handled.
In processing of heavy oil method of the present invention, the decompression residuum can after solvent directional separation
Frivolous coal tar, heavy deasphalted oil and de-oiled asphalt are obtained, the property of the frivolous coal tar is much better than institute
Decompression residuum is stated, carbon residue content is less than 6%, Ni+V contents and is less than 15 μ g/g, carbon residue and tenor
Far below decompression residuum, corresponding be hydrocracked can be targetedly selected to carry out subsequently adding with catalytic cracking
Work, realizes the deep conversion of part high-quality resource in heavy oil, improves light oil yield and quality, increases product
Added value.
Other features and advantages of the present invention will be described in detail in subsequent embodiment part.
Brief description of the drawings
Accompanying drawing is, for providing a further understanding of the present invention, and to constitute a part for specification, with
Following embodiment is used to explain the present invention together, but is not construed as limiting the invention.
In accompanying drawing：
Fig. 1 is a kind of schematic diagram of the embodiment for the methods described that the present invention is provided.
Description of reference numerals
1- vacuum distillation apparatus；2- solvent directional separation devices；3- delayed coking units；4- is hydrocracked
Device；5- catalytic cracking units.
Embodiment
The embodiment of the present invention is described in detail below in conjunction with accompanying drawing.It should be appreciated that
Embodiment described herein is merely to illustrate and explain the present invention, and is not limited to this hair
It is bright.
The invention provides a kind of processing of heavy oil method, wherein, this method comprises the following steps：
(1) heavy oil is subjected to vacuum distillation processing, obtains decompressed wax oil and decompression residuum；
(2) decompression residuum is subjected to solvent directional separation processing, obtains frivolous coal tar, takes off again
Coal tar and de-oiled asphalt；
(3) heavy deasphalted oil and the de-oiled asphalt are subjected to delayed coking processing；
(4) the part decompressed wax oil and the part frivolous coal tar are subjected to hydrocracked, treated；
(5) by remaining decompressed wax oil, remaining frivolous coal tar, the hydrocracked, treated mistake
The wax tailings produced during the hydrocracking tail oil produced in journey and delayed coking processing enter
Row catalytic cracking is handled.
According to the present invention, in step (1), the process of the vacuum distillation processing can according to it is various often
The mode of rule is implemented, for example, can be carried out in vacuum distillation tower.The principle of the vacuum distillation processing
It is：The principle for being reduced and being reduced with system pressure according to oil product boiling point, using the side of reduction column pressure
Method is distilled, and the heavy distillate by boiling point under normal pressure at 350 DEG C -500 DEG C (subtracts at a lower temperature
Pressure wax oil) steam.In the present invention, there is no particular limitation for the condition handled the vacuum distillation.
According to the present invention, in step (2), the process of the solvent directional separation processing can be according to each
Plant conventional mode to implement, for example, can carry out in solvent directional separation device.The solvent orientation
The principle of separating treatment is：The decompression residuum obtained during the vacuum distillation processing is heated
Enter one-section abstraction device after being mixed afterwards with the solvent from solvent heating furnace in predetermined ratio, settle down
The de-oiled asphalt separated herein with deasphalted oil, by the one-section abstraction device bottom discharge；It is described de-
Coal tar enters two sections of heating furnaces at the top of the one-section abstraction device, is raised to after preset temperature and enters two sections points
From tower, the heavy constituent in the deasphalted oil is further separated out from the solvent, with the heavy depitching
The form of oil enters molten in surge tank, said heavy deasphalted oil from the bottom of two sections of knockout towers
Agent is recycled.The frivolous coal tar that two sections of separation columns are drawn enters solvent by decompression
Separator, heats volatilization by solvent and returns to solvent tank through cooling, two sections of separation tower bottom obtains institute
State frivolous coal tar.
According to the present invention, the solvent during the solvent directional separation processing can be this area
The solvent used during middle conventional solvent directional separation, it is preferable that the solvent is butane or fourth
Alkane and pentane admixture.When the solvent is butane, under preferable case, the solvent directional separation
Condition includes：Pressure is 3-6MPa, and temperature is 90-130 DEG C；When the solvent is that butane and pentane are mixed
During compound, under preferable case, the condition of the solvent directional separation processing includes：Pressure is 3-6MPa,
Temperature is 110-170 DEG C.
In the present invention, when the solvent is butane and pentane admixture, to the butane and the pentane
Consumption there is no particular limitation.
In the present invention, to the selection of the butane and the pentane, there is no particular limitation, and the butane can
Think at least one of normal butane and iso-butane, the pentane can be pentane, isopentane and new penta
At least one of alkane.
In the present invention, the weight ratio of the solvent and the decompression residuum is had no particular limits, as long as
The consumption of the solvent is enough by the frivolous coal tar, the heavy deasphalted oil in the decompression residuum
Separated with the de-oiled asphalt.Under preferable case, the weight ratio of the solvent and the decompression residuum
For 1-10：1, preferably 3-5：1, more preferably 4-5：1.
According to the present invention, in step (3), the process of the delayed coking processing can according to it is various often
The mode of rule is implemented, for example, can be carried out in delayed coking unit.The master of the delayed coking processing
Syllabus is that the Residual oil of high carbon residue is converted into light oil, and equipment therefor can carry out circulate operation, will
Heavier cut is as recycle oil in the coker distillate of the heavy oil, and in a device the residence time compared with
It is long.In the present invention, to the vacuum distillation handle condition there is no particular limitation, but in order to obtain compared with
Under high yield of light oil, preferable case, the condition of the delayed coking processing includes：Reaction temperature
440-510 DEG C, pressure is 0.15-0.4MPa, recycle ratio 0.1-0.3.
According to the present invention, in step (4), the process of the hydrocracked, treated can according to it is various often
The mode of rule is implemented, for example, can be carried out in hydrocracking unit.Under preferable case, the hydrogenation
The condition of cracking processing includes：Temperature is 390-420 DEG C, and pressure is 9-14MPa, and hydrogen to oil volume ratio is
800-1400, liquid hourly space velocity (LHSV) is 1-2.5h-1；In the case of more preferably, the condition bag of the hydrocracked, treated
Include：Temperature is 400-420 DEG C, and pressure is 9-10MPa, and hydrogen to oil volume ratio is 1000-1400, liquid space-time
Speed is 1-1.5h-1.According to the present invention, during the hydrocracked, treated, with the part reduced pressure
The gross weight of the frivolous coal tar of wax oil and the part is 100 parts by weight meters, the use of the frivolous coal tar
Measure as 5-30 parts by weight, preferably 5-25 parts by weight, more preferably 10-25 parts by weight, it is further excellent
Elect 10-20 parts by weight as.
According to the present invention, in step (5), the process of the catalytic cracking processing can according to it is various often
The mode of rule is implemented, for example, can be carried out in catalytic cracking unit.The catalytic cracking processing refers to
Heavier petroleum fraction is occurred cracking reaction in the presence of high temperature and catalyst, be changed into cracked gas, vapour
The process of oil and diesel oil etc..Under preferable case, the condition of the catalytic cracking processing includes：Temperature is
480-530 DEG C, liquid hourly space velocity (LHSV) is 10-30h-1, agent oil quality ratio is 4-8, and water oil quality ratio is 0.04-0.12；
In the case of more preferably, the condition of the catalytic cracking processing includes：Temperature is 480-500 DEG C, liquid space-time
Speed is 15-25h-1, agent oil quality ratio is 5-7, and water oil quality ratio is 0.08-0.1.
In the present invention, the selection of catalyst used is not special during handling the catalytic cracking
Restriction, can be catalyst conventional in the art.In the present invention, to the consumption of the catalyst
There is no particular limitation, as long as the consumption of the catalyst disclosure satisfy that catalytic cracking reaction.Raw material
Including the remaining decompressed wax oil in step (5), the remaining frivolous coal tar, it is described plus
Hydrogen cracking tail oil and the wax tailings.
According to the present invention, the decompressed wax oil splits during the hydrocracked, treated with the catalysis
Weight distribution ratio during change is handled is 1-7：1, preferably 2-4：1.
In the present invention, the heavy oil is at least one of reduced crude, decompression residuum, preferably normal pressure
Residual oil.
It should be noted that in the case of no specified otherwise, heretofore described pressure refers to definitely
Pressure.
The present invention will be further described in detail by specific embodiment below.
Carried out in following examples using embodiment as shown in Figure 1.Embodiment is as follows：By heavy oil
Vacuum distillation processing is carried out by vacuum distillation apparatus 1, decompressed wax oil and decompression residuum is obtained；Again by institute
State decompression residuum and solvent directional separation processing is carried out by solvent directional separation device 2, obtain frivolous pitch
Oil, heavy deasphalted oil and de-oiled asphalt；The heavy deasphalted oil and the de-oiled asphalt are passed through into delay coke
Makeup put 3 carry out delayed coking processing, obtain dry gas, liquefied gas, gasoline, diesel oil, wax tailings and
Petroleum coke；The part decompressed wax oil and the part frivolous coal tar are entered by hydrocracking unit 4
Row hydrocracked, treated, obtains dry gas, liquefied gas, gasoline, diesel oil and hydrocracking tail oil；By residue
Decompressed wax oil, remaining frivolous coal tar, described being hydrocracked of producing in the hydrocracking process
The wax tailings produced in tail oil and the delayed coking are urged by catalytic cracking unit 5
Change cracking processing, obtain dry gas, liquefied gas, gasoline, diesel oil and slurry oil.
In order to make it easy to understand, different component is represented with letter respectively in following examples, including：Depressurize wax
Oily (VGO), decompression residuum (VR), frivolous coal tar (LDAO), heavy deasphalted oil (HDAO),
De-oiled asphalt (DOA).
Following examples and comparative example Peng Lai that extra large oil Huizhou oil refining branch company mainly processes in choosing are former
Oil and Da Liya crude oil carry out true boiling point distillation to it and obtain reduced crude, i.e. heavy oil as raw material, point
PZ and DZ are not denoted as it.The true boiling point distillation data of two kinds of reduced crudes are as shown in table 1.
Table 1
| Boiling range, DEG C | PZ, wt% | DZ, wt% |
| Initial boiling point -500 | 42.67 | 44.59 |
| More than 500 | 55.93 | 54.19 |
| Loss | 1.40 | 1.22 |
| It is total | 100 | 100 |
Embodiment 1
The present embodiment is used to illustrate the processing of heavy oil method using PZ as raw material.
PZ is subjected to vacuum distillation processing by vacuum distillation apparatus 1, VGO is obtained1And VR1, VGO1
With VR1Specific nature it is as shown in table 2；
Using iso-butane as solvent, by 20 parts by weight VR1With 80 parts by weight iso-butanes temperature be 90 DEG C,
Pressure obtains to carry out solvent directional separation processing by solvent directional separation device 2 under conditions of 4MPa
To LDAO1、HDAO1And DAO1, LDAO1、HDAO1And DAO1The yield such as institute of table 3,
LDAO1Property it is as shown in table 4；
By HDAO1And DAO1Temperature be 500 DEG C, pressure be that 0.2MPa, recycle ratio are 0.2
Under the conditions of by delayed coking unit 3 carry out delayed coking processing, obtain dry gas, liquefied gas, gasoline,
Diesel oil, wax tailings and petroleum coke；
By 90 parts by weight VGO1(VGO1Handled during hydrocracked, treated with catalytic cracking
During weight distribution ratio be 3.07：1) with 10 parts by weight LDAO1It is 400 DEG C, pressure in temperature
For 9MPa, hydrogen to oil volume ratio be 1000 and liquid hourly space velocity (LHSV) is 1h-1Under conditions of pass through hydrocracking unit
4 carry out hydrocracked, treated, obtain dry gas, liquefied gas, gasoline, diesel oil and hydrocracking tail oil；
By remaining VGO1, remaining LDAO1, hydrocracking tail oil and wax tailings mixing, in temperature
Spend for 480 DEG C, liquid hourly space velocity (LHSV) is 15h-1, agent oil quality ratio is 6, and water oil quality is than the condition for 0.08
Catalytic cracking processing is carried out by catalytic cracking unit 5 down, dry gas, liquefied gas, gasoline, diesel oil is obtained
And slurry oil.
The product distribution of embodiment 1 is as shown in table 5.
Embodiment 2
The present embodiment is used to illustrate the processing of heavy oil method using PZ as raw material.
According to the method processing heavy oil of embodiment 1, except that, by 80 parts by weight VGO1With 20
Parts by weight LDAO1Carry out hydrocracked, treated.
The product distribution of embodiment 2 is as shown in table 5.
Embodiment 3
The present embodiment is used to illustrate the processing of heavy oil method using PZ as raw material.
According to the method processing heavy oil of embodiment 1, except that, by 70 parts by weight VGO1With 30
Parts by weight LDAO1Carry out hydrocracked, treated.
The product distribution of embodiment 3 is as shown in table 5.
Embodiment 4
The present embodiment is used to illustrate the processing of heavy oil method using PZ as raw material.
According to the method processing heavy oil of embodiment 1, except that, using iso-butane and pentane as solvent,
And the weight ratio of iso-butane and pentane is 4：1.
The product distribution of embodiment 4 is as shown in table 5.
Embodiment 5
The present embodiment is used to illustrate the processing of heavy oil method using DZ as raw material.
According to the method processing heavy oil of embodiment 1.Except that, using DZ as raw material.Obtain VGO2
And VR2, VGO2With VR2Specific nature it is as shown in table 2；Obtain LDAO2、HDAO2And DAO2,
LDAO2、HDAO2And DAO2Yield as shown in table 3, LDAO2Property it is as shown in table 4；
The product distribution of embodiment 5 is as shown in table 6.
Embodiment 6
The present embodiment is used to illustrate the processing of heavy oil method using DZ as raw material.
According to the method processing heavy oil of embodiment 5.Except that, by 80 parts by weight VGO2With 20
Parts by weight LDAO2Carry out hydrocracked, treated.
The product distribution of embodiment 6 is as shown in table 6.
Comparative example 1
This comparative example is used to illustrate the processing of heavy oil method using PZ as raw material.
According to the method processing heavy oil of embodiment 1.Except that, VR1Without solvent directional separation
Processing, directly carries out delayed coking processing.
The product distribution of comparative example 1 is as shown in table 5.
Comparative example 2
This comparative example is used to illustrate the processing of heavy oil method using DZ as raw material.
According to the method processing heavy oil of embodiment 6.Except that, VR2Without solvent directional separation
Processing, directly carries out delayed coking processing.
The product distribution of comparative example 2 is as shown in table 6.
Table 2
| Parameter | VGO1 | VR1 | VGO2 | VR2 |
| Density (50 DEG C), gcm-3 | 0.906 | 1.022 | 0.917 | 0.962 |
| Viscosity (100 DEG C), mm2·s-1 | 9.39 | 1339.79 | 6.58 | 447.03 |
| Carbon residue, wt% | 0.03 | 15.68 | 0.14 | 14.12 |
| C, wt% | 86.81 | 86.18 | 87.06 | 86.76 |
| H, wt% | 12.29 | 11.10 | 12.13 | 11.23 |
| S, wt% | 0.27 | 0.50 | 0.40 | 0.82 |
| N, wt% | 0.15 | 1.09 | 0.08 | 0.70 |
| Saturation point, wt% | 68.48 | 27.28 | 71.41 | 30.06 |
| Fragrance point, wt% | 22.35 | 34.16 | 23.03 | 37.77 |
| Colloid, wt% | 7.38 | 37.13 | 5.37 | 28.94 |
| Asphalitine, wt% | 1.79 | 2.28 | 0.19 | 3.22 |
Table 3
| Ingredient names | Yield, wt% |
| LDAO1 | 54.21 |
| HDAO1 | 3.17 |
| DAO1 | 42.62 |
| LDAO2 | 65.62 |
| HDAO2 | 4.17 |
| DAO2 | 30.21 |
Table 4
| Parameter | LDAO1 | LDAO2 |
| Density (50 DEG C), gcm-3 | 0.917 | 0.940 |
| Viscosity (100 DEG C), mm2·s-1 | 68.16 | 71.87 |
| Carbon residue, wt% | 4.11 | 4.23 |
| Ni+V, μ g/g | 8.5 | 9.2 |
| C, wt% | 86.42 | 86.62 |
| H, wt% | 11.84 | 11.68 |
| S, wt% | 0.38 | 0.69 |
| N, wt% | 0.72 | <0.3 |
| Saturation point, wt% | 35.93 | 42.17 |
| Fragrance point, wt% | 39.96 | 40.01 |
| Colloid, wt% | 24.11 | 17.78 |
| Asphalitine, wt% | 0 | 0 |
Table 5
Table 6
| Product, wt% | Embodiment 5 | Embodiment 6 | Comparative example 2 |
| Dry gas | 3.16 | 2.93 | 5.94 |
| Liquefied gas | 11.69 | 10.65 | 9.06 |
| Gasoline | 47.90 | 48.34 | 48.89 |
| Diesel oil | 22.40 | 24.28 | 19.33 |
| Slurry oil | 2.88 | 2.63 | 1.58 |
| Petroleum coke | 8.36 | 8.36 | 14.22 |
| Coke | 4.84 | 4.39 | 2.48 |
| Light oil | 70.30 | 72.62 | 68.22 |
| Liquid is received | 81.99 | 83.27 | 77.28 |
| Light oil rises in value | 2.09 | 4.40 | — |
| Liquid receives increment | 4.72 | 5.99 | — |
From the data of table 4 can be seen that the inventive method, VR1And VR2By solvent directional separation
The LDAO obtained after processing1And LDAO2Carbon residue be less than 6%, Ni+V contents be less than 15 μ g/g.
The light oil obtained according to the method processing heavy oil of the present invention is can be seen that from the data of table 5 and table 6
Yield is substantially higher than the light oil yield that conventional method is obtained, and total liquid yield is also significantly increased, i.e., product is attached
Value added increase.
The preferred embodiment of the present invention is described in detail above in association with accompanying drawing, still, the present invention is not limited
Detail in above-mentioned embodiment, can be to the present invention in the range of the technology design of the present invention
Technical scheme carry out a variety of simple variants, these simple variants belong to protection scope of the present invention.
It is further to note that each particular technique described in above-mentioned embodiment is special
Levy, in the case of reconcilable, can be combined by any suitable means.In order to avoid need not
The repetition wanted, the present invention no longer separately illustrates to various possible combinations.
In addition, various embodiments of the present invention can be combined randomly, as long as its
Without prejudice to the thought of the present invention, it should equally be considered as content disclosed in this invention.
Claims (9)
1. a kind of processing of heavy oil method, it is characterised in that this method comprises the following steps：
(1) heavy oil is subjected to vacuum distillation processing, obtains decompressed wax oil and decompression residuum；
(2) decompression residuum is subjected to solvent directional separation processing, obtains frivolous coal tar, takes off again
Coal tar and de-oiled asphalt；
(3) heavy deasphalted oil and the de-oiled asphalt are subjected to delayed coking processing；
(4) the part decompressed wax oil and the part frivolous coal tar are subjected to hydrocracked, treated；
(5) by remaining decompressed wax oil, remaining frivolous coal tar, the hydrocracked, treated mistake
The wax tailings produced during the hydrocracking tail oil produced in journey and delayed coking processing enter
Row catalytic cracking is handled.
2. processing of heavy oil method according to claim 1, wherein, in the solvent directional separation
During processing, solvent used and the weight ratio of the decompression residuum are 1-10：1, preferably 3-5：
1；
Preferably, the solvent is butane or butane and pentane admixture.
3. processing of heavy oil method according to claim 2, wherein, when the solvent is butane,
The condition of the solvent directional separation processing includes：Pressure is 3-6MPa, and temperature is 90-130 DEG C；
When the solvent is butane and pentane admixture, the condition bag of the solvent directional separation processing
Include：Pressure is 3-6MPa, and temperature is 110-170 DEG C.
4. processing of heavy oil method according to claim 1, wherein, the delayed coking processing
Condition includes：440-510 DEG C of reaction temperature, pressure is 0.15-0.4MPa, recycle ratio 0.1-0.3.
5. the processing of heavy oil method according to any one in claim 1-4, wherein, it is described to subtract
Press wax oil during the hydrocracked, treated and the weight during the catalytic cracking is handled
Distribution ratio is 1-7：1, preferably 2-4：1.
6. the processing of heavy oil method according to any one in claim 1-5, wherein, it is described to add
Hydrogen cracking handle during, using the total amount of the decompressed wax oil and the consumption of the frivolous coal tar as
100 parts by weight meters, the consumption of the frivolous coal tar is 5-30 parts by weight.
7. processing of heavy oil method according to claim 1, wherein, the hydrocracked, treated
Condition includes：Temperature is 390-420 DEG C, and pressure is 9-14MPa, and hydrogen to oil volume ratio is 800-1400,
Liquid hourly space velocity (LHSV) is 1-2.5h-1；
Preferably, the condition of the hydrocracked, treated includes：Temperature is 400-420 DEG C, and pressure is
9-10MPa, hydrogen to oil volume ratio is 1000-1400, and liquid hourly space velocity (LHSV) is 1-1.5h-1。
8. processing of heavy oil method according to claim 1, wherein, the catalytic cracking processing
Condition includes：Temperature is 480-530 DEG C, and liquid hourly space velocity (LHSV) is 10-30h-1, agent oil quality ratio is 4-8, water
Oil quality ratio is 0.04-0.12；
Preferably, the condition of the catalytic cracking processing includes：Temperature is 480-500 DEG C, liquid hourly space velocity (LHSV)
For 15-25h-1, agent oil quality ratio is 5-7, and water oil quality ratio is 0.08-0.1.
9. the processing of heavy oil method according to any one in claim 1-8, wherein, it is described heavy
Oil is at least one of reduced crude, decompression residuum, preferably reduced crude.
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| CN1844325A (en) * | 2006-04-17 | 2006-10-11 | 中国石油化工集团公司 | Combined process for processing heavy oil |
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| CA2891872A1 (en) * | 2014-05-21 | 2015-11-21 | IFP Energies Nouvelles | Method for converting a heavy hydrocarbon load integrating selective deasphalting before the conversion step |
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| CN1844325A (en) * | 2006-04-17 | 2006-10-11 | 中国石油化工集团公司 | Combined process for processing heavy oil |
| CN102807892A (en) * | 2011-05-31 | 2012-12-05 | 中国石油大学(北京) | Combined technology for heavy oil processing |
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