CN109554197A - A kind of residual oil hydrogenation-catalytic cracking combined method - Google Patents
A kind of residual oil hydrogenation-catalytic cracking combined method Download PDFInfo
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- CN109554197A CN109554197A CN201710889315.XA CN201710889315A CN109554197A CN 109554197 A CN109554197 A CN 109554197A CN 201710889315 A CN201710889315 A CN 201710889315A CN 109554197 A CN109554197 A CN 109554197A
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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
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a kind of residual oil hydrogenation-catalytic cracking combined methods, use residual hydrogenation equipment, catalytic cracking reaction product is mixed in residual oil raw material and by the residual oil hydrocatalyst bed in residual hydrogenation equipment, obtain hydrogenation products, hydrogenation products, which are fractionated, obtains gasoline, diesel oil distillate and hydrogenation tail oil, and hydrogenation tail oil is fed as catalytic cracking unit.The present invention makes the reduction of reaction feed system viscosity by the incorporation of catalytic cracking reaction product, colloidal stability improves, and preventing asphalitine to be precipitated too early leads to catalyst inactivation, and device smooth operation improves and then extends on-stream time, economic benefit is improved, product quality is improved；Catalytic cracking reaction product participates in reaction process the reactivity worth for improving system so as to improve product quality, obtains high added value clear gusoline, realizes the green high value added utilization to raw material；The application is not limited to residue fixed-bed hydrogenation technique, and the scope of application is wider；It simply operated, be suitable for industrialized production.
Description
Technical field
The present invention relates to a kind of residual oil hydrogenation-catalytic cracking combined methods, belong to PETROLEUM PROCESSING field.
Background technique
With the increasingly raising of environmental requirement, Clean Fuel Production technology is increasingly taken seriously.Compared to other residual oil
Processing technology, residual hydrocracking technology advantage in Clean Fuel Production are huge.Residual hydrocracking-catalytic cracking combination is answered
The important means that refinery realizes residual oil weight-lightening production clear gusoline is increasingly becoming with technology.Residual oil is used as afterwards through hydrogenated processing urges
Change cracked stock and not only reduce the sulfur content of catalytically cracked material, and helps to reduce the sulfur content of catalytic cracking product.
Residual hydrocracking technology will be that most of refineries especially process the preferred of weight inferior raw material refinery within quite long period
Technology, Research Emphasis, which still will focus on, to be extended on the device cycle of operation and working process raw material more inferior.
CN201010245844.4 discloses a kind of residual hydrocracking, catalytic cracking heavy oil adds the group of hydrogen and catalytic cracking
Conjunction method.The resulting reaction product of residual hydrogenation reactor is separated into gaseous stream and liquid phase stream, and wherein liquid phase stream is fractionated
Obtained residual hydrogenation tail oil enters catalytic cracking unit as the raw material of catalytic cracking, the catalytic cracking in catalytic cracking production
Gaseous stream in heavy oil and residual hydrogenation reaction product is mixed into catalytic cracking heavy oil hydrogenator, the catalysis after adding hydrogen
Cracked fuel oil is recycled back to catalytic cracking unit.The invention can the light-end products that are converted by residual oil compared with limits, but technique is excessively
Complexity, and feedstock viscosity is excessive, and device operational stability is poor, and product quality not can guarantee yet.
CN201110156250.0 discloses a kind of residual hydrocracking-catalytic cracking-solvent refining group technology.Residual oil
Enter residual hydrocracking device with hydrogen and carry out hydrogenation reaction, hydrogenated residue enters catalytic cracking unit, and the reaction was continued, will be anti-
Gained heavy catalytic cycle oil and slurry oil is answered to carry out solvent refining, solvent refining extraction oil returns after removing solid impurity
Residual hydrogenation equipment and residual oil enter device together and carry out hydrotreating, refine Returning catalyticing cracking device of raffinating oil, and add hydrogen
Residual oil enters catalytic cracking unit together, and the reaction was continued.This method complex process, especially solvent refining processes solvent loss is big,
It is less economical, and separating effect is bad, easily cause residual hydrogenation equipment catalyst bed to block, industrializing implementation difficulty compared with
Greatly.
Summary of the invention
The present invention provides a kind of residual oil hydrogenation-catalytic cracking combined method, can extend residual hydrogenation equipment by a relatively large margin
On-stream time simultaneously improves product quality, promotes economic benefit.
In order to solve the above technical problems, the technical solution adopted in the present invention is as follows:
A kind of residual oil hydrogenation-catalytic cracking combined method mixes partially catalyzed cracked reaction product, simultaneously in residual oil raw material
By adding hydrogen, hydrogenation products are obtained, hydrogenation products, which are fractionated, obtains naphtha, diesel oil distillate and hydrogenation tail oil, and hydrogenation tail oil is made
For catalytic cracking unit charging.
Making the reduction of reaction feed system viscosity above by the incorporation of catalytic cracking reaction product, colloidal stability improves,
Preventing asphalitine to be precipitated too early leads to catalyst inactivation, device smooth operation improve so that extend on-stream time, improve through
Ji benefit, improves product quality.
The catalytic cracking reaction product is FCC recycle oil (including oily in oily, catalysis two in catalytic diesel oil, catalysis one)
Or at least one of catalytic slurry.In two oil than one in it is oily heavier.
Wherein, FCC recycle oil, catalytic slurry can choose whether removing Solid content as needed.
In order to further ensure products obtained therefrom quality, it is preferable that catalytic cracking reaction product is catalytic slurry；It is further excellent
Choosing, catalytic cracking reaction product be catalytic slurry and catalysis two in oil quality than the mixture for 1:1.
In order to further ensure that the quality of products obtained therefrom, the incorporation mass fraction of catalytic cracking reaction product accounts for combined feed matter
The 0.001%~30% of amount.It is preferred that the incorporation mass fraction of catalytic cracking reaction product accounts for the 6%~12% of combined feed quality.
The application residual hydrogenation equipment can be fixed bed, ebullated bed, moving bed or suspension bed.
Residual oil hydrocatalyst can be support type, be also possible to non-loading type；Residual hydrogenation equipment reactor can
With only one, it is also possible to multiple serial or parallel connections.
In order to further increase product quality, reaction temperature is at 300~500 DEG C during residual hydrocracking, hydrogen pressure
Power reacts liquid hourly space velocity (LHSV) in 0.01~10h in 10~25MPa-1。
Above-mentioned residual oil hydrogenation-catalytic cracking combined method, equipment therefor include: residual hydrogenation reaction unit, residual hydrogenation
Product separator, catalytic cracking reaction device, catalytic cracking production separator；Residual hydrogenation reaction unit, residual hydrogenation
Product separator, catalytic cracking reaction device, catalytic cracking production separator are sequentially connected to, form circulation；In residual oil original
Partially catalyzed cracked reaction product is mixed in material and hydrogen is added by residual hydrogenation reaction unit, hydrogenation products is obtained, through residual hydrogenation
Product separator is fractionated to obtain naphtha, diesel oil distillate and hydrogenation tail oil, and hydrogenation tail oil is as catalytic cracking reaction device
Charging, gained catalytic cracking production obtain catalytically cracked gasoline, catalytic diesel oil, urge after the separation of catalytic cracking production separator
Change oil in one, oil and catalytic slurry in catalysis two.
The unmentioned technology of the present invention is referring to the prior art.
Residual oil hydrogenation-catalytic cracking combined method of the present invention makes reaction feed by the incorporation of catalytic cracking reaction product
System viscosity reduces, and colloidal stability improves, and preventing asphalitine to be precipitated too early leads to catalyst inactivation, and device smooth operation mentions
High and then extension on-stream time, improves economic benefit, improves product quality；Catalytic cracking reaction product, which participates in, to react
Improve the reactivity worth of system in journey so as to improve product quality, obtains high added value clear gusoline, realize to the green of raw material
Color high value added utilization；The application is not limited to residue fixed-bed hydrogenation technique, and the scope of application is wider；It is simple to operation, be suitable for
Industrialized production.
Detailed description of the invention
Fig. 1 residual hydrogenation catalytic cracking combined technique schematic diagram；
1, former residual hydrogenation equipment charging；2, residual hydrogenation reaction unit；3, residual hydrogenation product separator；4, residual oil
Hydrotreated naphtha；5, residual hydrogenation diesel oil；6, residual hydrogenation tail oil；7, catalytic cracking reaction device；8, catalytic cracking reaction produces
Object；9, catalytic cracking production separator；10, catalytically cracked gasoline；11, catalytic diesel oil；12, oil in catalysis one；13, two are catalyzed
Middle oil；14, catalytic slurry；15, residual oil hydrogenation-catalytic cracking connecting line (connecting pipeline).
Specific embodiment
For a better understanding of the present invention, below with reference to the embodiment content that the present invention is furture elucidated, but it is of the invention
Content is not limited solely to the following examples.
Each embodiment equipment therefor includes: residual hydrogenation reaction unit, residual hydrogenation product separator, Catalytic Cracking Unit of Measure
Answer device, catalytic cracking production separator；Residual hydrogenation reaction unit, residual hydrogenation product separator, Catalytic Cracking Unit of Measure
It answers device, catalytic cracking production separator to be sequentially connected to, form circulation；Partially catalyzed cracking reaction is mixed in residual oil raw material
Product simultaneously adds hydrogen by residual hydrogenation reaction unit, obtains hydrogenation products, is fractionated to obtain stone brain through residual hydrogenation product separator
Oil, diesel oil distillate and hydrogenation tail oil, hydrogenation tail oil are fed as catalytic cracking reaction device, and gained catalytic cracking production is through urging
After changing the separation of crackate separator, obtains catalytically cracked gasoline, catalytic diesel oil, is catalyzed oil in one, oil and catalysis in catalysis two
Slurry oil.
Embodiment 1
As shown in Figure 1: on the basis of former residual hydrogenation equipment charging 1, oil in the catalysis two of refining mass fraction 6% is mixed
13, residual hydrogenation reaction unit 2 is entered after mixing, and pass through residual oil hydrocatalyst bed；370 DEG C of reaction temperature, hydrogen pressure
Power 16MPa, reaction velocity 0.2h-1.Products therefrom enter after product separator 3 obtain naphtha 4,5 fraction of diesel oil and
Hydrogenation tail oil 6, hydrogenation tail oil obtain catalytic cracking production 8 through catalytic cracking reaction as the charging of catalytic cracking reaction device 7
Into catalytic cracking separator 9, product 8 obtains catalytic gasoline 10, catalytic diesel oil 11 after separation, is catalyzed oil 12 in one, urges
Change oily 13, catalytic slurry 14 in two, wherein oil 13 enters after mixing by connecting pipeline 15 with residual hydrogenation charging 1 in catalysis two
The reaction was continued for residual hydrogenation equipment.
Embodiment 2
As shown in Figure 1: on the basis of former residual hydrogenation equipment charging 1, the catalytic slurry 14 of refining mass fraction 6% is mixed
(filtered) enters residual hydrogenation reaction unit 2, and passes through residual oil hydrocatalyst bed after mixing；Reaction temperature 370
DEG C, Hydrogen Vapor Pressure 16MPa, reaction velocity 0.2h-1.Products therefrom obtains naphtha 4, diesel oil 5 after entering product separator 3
Fraction and hydrogenation tail oil 6, hydrogenation tail oil obtain catalysis through catalytic cracking reaction as the charging of catalytic cracking reaction device 7 and split
Change product 8 and enter catalytic cracking separator 9, product 8 obtains catalytic gasoline 10 after separation, catalytic diesel oil 11, is catalyzed in one
Oily 13, catalytic slurry 14 in oil 12, catalysis two, wherein catalytic slurry 14 is mixed by connecting pipeline 15 with residual hydrogenation charging 1
Entering residual hydrogenation equipment afterwards, the reaction was continued.
Embodiment 3
As shown in Figure 1: on the basis of former residual hydrogenation equipment charging 1, oil 13 in the catalysis two of refining mass fraction 6% is mixed
Catalytic slurry 14 (filtered) with 6%, enters residual hydrogenation reaction unit 2, and pass through residual oil hydrocatalyst after mixing
Bed；370 DEG C of reaction temperature, Hydrogen Vapor Pressure 16MPa, reaction velocity 0.2h-1.After products therefrom enters product separator 3
Obtain naphtha 4,5 fraction of diesel oil and hydrogenation tail oil 6, hydrogenation tail oil as catalytic cracking reaction device 7 charging through being catalyzed
Cracking reaction obtains catalytic cracking production 8 and enters catalytic cracking separator 9, and product 8 obtains catalytic gasoline 10 after separation, urges
Oily 12 in change diesel oil 11, catalysis one, oily 13, catalytic slurry 14 in two are catalyzed, are led to wherein being catalyzed oil 13 and catalytic slurry 14 in two
Cross after connecting pipeline 15 and residual hydrogenation charging 1 mix that the reaction was continued into residual hydrogenation equipment.
Verify example
Residual hydrogenation products derived from processes described in residual oil raw material and Examples 1 to 3 is subjected to three component analysis of heavy oil, knot
Fruit is as shown in table 1.
Each embodiment hydrogenation products of table 1 analyze result
Seen from table 1, filtered catalytic slurry and catalysis two in oil mixed with 6% mass fraction with residual oil it is laggard
The experiment of row continuously hydrogen adding, the distribution of thick oil liquid group product, which is slightly better than, mixes oily group in refining catalysis two；In the catalysis two of mass fraction 6%
The catalytic slurry of oil+6% carries out continuously hydrogen adding experiment after mixing with residual oil, product distribution is better than catalytic slurry with 6% quality
The case where dividing rate to mix with residual oil.
Claims (10)
1. a kind of residual oil hydrogenation-catalytic cracking combined method, it is characterised in that: mix catalytic cracking reaction in residual oil raw material and produce
Object and by adding hydrogen, obtains hydrogenation products, hydrogenation products are fractionated and obtain naphtha, diesel oil distillate and hydrogenation tail oil, add hydrogen tail
Oil is fed as catalytic cracking unit.
2. according to the method described in claim 1, it is characterized by: catalytic cracking reaction product is FCC recycle oil or catalyzed oil
At least one of slurry.
3. according to the method described in claim 2, it is characterized by: FCC recycle oil include catalytic diesel oil, catalysis one in oil and
Oil in catalysis two.
4. according to the method described in claim 3, it is characterized by: catalytic cracking reaction product is catalytic slurry.
5. according to the method described in claim 3, it is characterized by: catalytic cracking reaction product is in catalytic slurry and catalysis two
Oil quality is than the mixture for 1:1.
6. method described in -5 any one according to claim 1, it is characterised in that: the incorporation quality of catalytic cracking reaction product
Score accounts for the 0.001%~30% of combined feed quality.
7. according to the method described in claim 6, it is characterized by: the incorporation mass fraction Zhan of catalytic cracking reaction product always into
Expect the 6%~12% of quality.
8. method described in -5 any one according to claim 1, it is characterised in that: reaction temperature during residual hydrocracking
At 300~500 DEG C, Hydrogen Vapor Pressure reacts liquid hourly space velocity (LHSV) in 0.01~10h in 10~25MPa-1。
9. method described in -5 any one according to claim 1, it is characterised in that: equipment therefor includes: residual hydrogenation reaction
Device, residual hydrogenation product separator, catalytic cracking reaction device, catalytic cracking production separator；Residual hydrogenation reaction
Device, residual hydrogenation product separator, catalytic cracking reaction device, catalytic cracking production separator are sequentially connected to, are formed
Circulation；Partially catalyzed cracked reaction product is mixed in residual oil raw material and hydrogen is added by residual hydrogenation reaction unit, and hydrogen must be added to produce
Object is fractionated to obtain naphtha, diesel oil distillate and hydrogenation tail oil through residual hydrogenation product separator, and hydrogenation tail oil is as catalysis
Cracking reaction device charging, gained catalytic cracking production through catalytic cracking production separator separation after, obtain catalytically cracked gasoline,
Oily and catalytic slurry in oily, catalysis two in catalytic diesel oil, catalysis one.
10. according to the method described in claim 9, it is characterized by: residual hydrogenation reaction unit is fixed bed, ebullated bed, shifting
Dynamic bed or suspension bed.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113403105A (en) * | 2021-06-10 | 2021-09-17 | 克拉玛依市先能科创重油开发有限公司 | Start-up oil feeding method of suspension bed hydrogenation device using ethylene cracking tar as raw material |
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| CN102732313A (en) * | 2011-04-15 | 2012-10-17 | 中国石油化工股份有限公司 | Hydrotreatment and catalytic cracking deeply-combined method for residuum |
| CN102732311A (en) * | 2011-04-15 | 2012-10-17 | 中国石油化工股份有限公司 | Hydrotreatment and catalytic cracking combined method for residuum |
| CN102732312A (en) * | 2011-04-15 | 2012-10-17 | 中国石油化工股份有限公司 | Hydrotreatment and catalytic cracking deeply-combined method for residuum |
| CN106367113A (en) * | 2015-07-23 | 2017-02-01 | 中国石化扬子石油化工有限公司 | Residual oil hydrotreating method |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102732313A (en) * | 2011-04-15 | 2012-10-17 | 中国石油化工股份有限公司 | Hydrotreatment and catalytic cracking deeply-combined method for residuum |
| CN102732311A (en) * | 2011-04-15 | 2012-10-17 | 中国石油化工股份有限公司 | Hydrotreatment and catalytic cracking combined method for residuum |
| CN102732312A (en) * | 2011-04-15 | 2012-10-17 | 中国石油化工股份有限公司 | Hydrotreatment and catalytic cracking deeply-combined method for residuum |
| CN106367113A (en) * | 2015-07-23 | 2017-02-01 | 中国石化扬子石油化工有限公司 | Residual oil hydrotreating method |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113403105A (en) * | 2021-06-10 | 2021-09-17 | 克拉玛依市先能科创重油开发有限公司 | Start-up oil feeding method of suspension bed hydrogenation device using ethylene cracking tar as raw material |
| CN113403105B (en) * | 2021-06-10 | 2022-12-27 | 克拉玛依市先能科创重油开发有限公司 | Start-up oil feeding method of suspension bed hydrogenation device using ethylene cracking tar as raw material |
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