CN107189814B - A method of diesel oil distillate is separated from lightweight material oil - Google Patents
A method of diesel oil distillate is separated from lightweight material oil Download PDFInfo
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- CN107189814B CN107189814B CN201710558645.0A CN201710558645A CN107189814B CN 107189814 B CN107189814 B CN 107189814B CN 201710558645 A CN201710558645 A CN 201710558645A CN 107189814 B CN107189814 B CN 107189814B
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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
- C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
- C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
- C10G55/06—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one catalytic cracking step
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- Oil, Petroleum & Natural Gas (AREA)
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- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention belongs to PETROLEUM PROCESSING field, in particular to a kind of method that diesel oil distillate is separated from lightweight material oil.Lightweight material oil rich in diesel oil distillate, directly enters main fractionating tower desuperheating section with pyroreaction air-fuel mixture, by its superfluous thermal release diesel oil distillate and wax oil fraction.Diesel oil distillate distillates from main fractionating tower diesel oil draw out mouth and send products pot, and wax oil fraction distillates from recycle oil outlet port and returns riser.It thus is avoided that the catalytic cracking reaction of diesel oil distillate, reduces the yield of dry gas and coke, reduce the ratio that the alkane molecule in diesel oil is converted into aromatic hydrocarbon molecule, improve the quality of catalyst article diesel oil；Again because catalysis processing capacity is reduced, coke output decline is suitable for old plant modification and new equipment designs so that plant energy consumption reduces.
Description
Technical field
The invention belongs to PETROLEUM PROCESSING fields, in particular to a kind of to utilize catalytic cracking unit main fractionating tower desuperheating section point
Its diesel oil distillate is avoided to repeat the process of processing from lightweight material oil.
Background technique
Catalytic cracking is important crude oil secondary operation device, be under the effect of the catalyst, by decomposition, isomerization,
Heavy distillate is converted to the light fractions such as liquefied gas, gasoline, diesel oil oil by the reaction such as hydrogen migration, aromatisation, condensation, and secondary
The technique for producing a certain amount of dry gas, slurry oil and coke.10% point of heavy raw oil boiling range is higher than 350 DEG C, lightweight material oil boiling range
10% point is lower than 340 DEG C, and 30% point of lightweight material oil boiling range is at 340-360 DEG C.
Catalytic cracking unit is mainly made of four reaction regeneration, fractionation, Vapor recovery unit and flue gas energy recovery subsystems.
Anti- the effect of subsystem is to borrow riser reactor that heavy raw oil is converted to reaction product (also known as reaction oil gas) and is borrowed again
Air burn regenerates the catalyst from reaction system surface enrichment coke, and realization recycles；Regenerated flue gas (about 680 DEG C,
Energy regenerating subsystem then 0.2MPag) is sent after by cyclonic separation Removal of catalyst dust, first drives and leads through smoke machine expansion work
Blower, then middle pressure steam occurs into remaining pot, most atmosphere is discharged through desulphurization denitration afterwards；And come from the reaction oil gas of reaction system then into
Enter main fractionating tower, is in superheated vapor phase state since temperature is about 520 DEG C high, therefore first through desuperheating degree section, hot production is taken by circulation slurry oil
Then raw middle pressure steam enters rectifying section for about 385 DEG C, to isolate recycle oil, diesel oil, raw gasoline and rich gas.Recycle oil, which is sent, to be mentioned
Riser secondary response, diesel oil go out device as product, rich gas and raw gasoline then into Vapor recovery unit subsystem, be separated into dry gas,
Liquefied gas and stable gasoline.
Be fractionated it is insufficient etc. due to, the raw material of catalytic cracking unit usually contains a certain amount of light wax oil in constituting
(first vacuum side stream of such as crude(oil)unit, light wax of delayed coking unit etc.), diesel oil distillate ratio is higher, and some even reaches
50% or more, riser reactor is sent together with other heavy raw oils, is forced secondary operation, in addition to increasing catalytic treatment amount,
It is also partially converted into dry gas and coke, furthermore the fine-quality diesel oil fraction rich in alkane is also because cracking reaction has been turned into rich in virtue
The poor-quality diesel-oil by cut fraction of hydrocarbon.Therefore in the appropriate way, the diesel oil distillate in lightweight material oil is separated in advance, and secondary operation is avoided to be
Very necessary.
Summary of the invention
In order to solve in the charging of existing FCC riser, diesel oil that lightweight material oil in part is included
Fraction is forced to carry out catalytic cracking reaction, not only improves unit capacity, also increase coke and dry gas yield and deterioration diesel oil matter
The shortcomings that amount, spy propose a kind of oily using catalytic cracking unit main fractionating tower desuperheating section separation lightweight material and avoid its diesel oil
The technique that fraction repeats processing.
The present invention is a kind of method that diesel oil distillate is separated from lightweight material oil, is catalyzed using catalytic cracking unit
Cracking reaction, the device include main fractionating tower and riser reactor, and main fractionating tower is divided into desuperheating section and rectifying tower section,
Specific step is as follows:
(1) heavy raw oil is passed directly into riser reactor and carries out catalytic cracking reaction, generate pyroreaction oil gas；
(2) desuperheating section and rectifying tower section of main fractionating tower are passed through after mixing pyroreaction oil gas with lightweight material oil,
Isolated diesel oil distillate and freshening oil distillate.
Temperature before the mixing of lightweight material oil described in step (2) is controlled at 160~180 DEG C.
Preferably, the temperature before the mixing of lightweight material oil described in step (2) is controlled at 170 DEG C.
Lightweight material oil described in step (2) by nozzle directly with pyroreaction air-fuel mixture.
Step (1) the desuperheating section head gas temperature control is at 360~380 DEG C.
Preferably, step (1) the desuperheating section head gas temperature control is at 370 DEG C.
The freshening oil distillate that main fractionating tower described in step (1) obtains distillates control at 345-355 DEG C.
Preferably, the freshening oil distillate that main fractionating tower described in step (1) obtains distillates control at 350 DEG C.The present invention
Based on the principle that
1) the column plate separation diesel oil and wax oil of the thermal evaporation lightweight material oil of the surplus of main fractionating tower desuperheating section, rectifying section,
More preferably than one special lightweight material oil fractionating column of setting, not only process is simple, small investment, and low energy consumption；
2) column plate up to more than ten blocks between main fractionating tower recycle oil outlet port and diesel oil draw out mouth, therefore its diesel oil and wax oil point
From effect better than the vacuum tower of atmospheric and vacuum distillation unit and the main fractionating tower of coking plant；
3) different fractions oil is because property difference must distinguish between and selectively treat.Wax oil fraction needs cracking admittedly, but
Diesel oil distillate then need not；Meanwhile a small amount of diesel oil distillate is removed, the not too large property for changing fcc raw material；
4) lightweight material oil is mostly straight-run (such as first vacuum side stream) and thermal cracking fraction (the light wax of such as coking), their institutes with
The diesel component of band is very much not same as catalytic diesel oil, and arene content is much lower, therefore raw material diesel oil does not repeat to react, and not but not drops
The yield (because avoiding cracking and polymerization, yield can also increase a little) of low catalytic diesel oil, can also improve catalytic diesel oil
Quality reduces its arene content, improves Cetane number.
Present invention process have the following advantages that and the utility model has the advantages that
1) diesel oil and wax oil fraction in lightweight material oil are efficiently separated.By means of FCC main fractionating tower surplus heat and technique stream
Journey is fractionated lightweight material oil, simpler and more direct and effective than special fractionating column is arranged, also more feasible than in upstream idetified separation effect
Conveniently.
2) it avoids raw material diesel oil distillate and carries out catalytic cracking reaction.After lightweight material oil is separated by main fractionating tower system,
Diesel oil distillate goes out device directly as product, and wax oil fraction, into riser, realizes raw material dual treatment, meet and urge with recycle oil
Change cracking principle.
3) effective components such as the alkane in raw material diesel oil are protected, to the arene content for reducing catalytic diesel oil, improve bavin
The Cetane number of oil, makes diesel product quality get a promotion；Again and because avoiding the cracking and polymerization of raw material diesel component, device
Dry gas and coking yield can reduce, diesel yield can improve.
4) amount of vaporization can be adjusted flexibly according to the property and flow of lightweight material；Fcc raw material property will not be because of a small amount of bavin
Oil distillate is removed and big change occurs.
5) process change is small, and plant energy consumption reduces.New technological process merely adds light wax stock oil tank and nozzle, is catalyzed processing capacity
It reduces, coke output decline, other do not change, therefore are suitable for old plant modification and new equipment construction.
Detailed description of the invention
Fig. 1 is the regeneration of existing catalytic cracking reaction and the main fractionating tower flow chart of comparative example
Fig. 2 is catalytic cracking reaction regeneration and the main fractionating tower flow chart of the embodiment of the present invention,
1- main fractionating tower column plate 1；2- oil slurry steam generator；3- main fractionating tower column plate 3；4- pushes up circulating reflux；5- is promoted
Pipe reactor；6- settler；7- regenerator sloped tube；8- inclined tube to be generated；9- lightweight material oil burner nozzle；10- main fractionating tower；11- first
Middle section reflux.
Specific embodiment
Present invention will now be described in further detail with reference to the embodiments and the accompanying drawings, but embodiments of the present invention are unlimited
In this.
With certain processing capacity 180 × 104For t/h catalytic cracking unit.
Comparative example 1
This comparative example is that existing catalytic cracking unit reaction regeneration and main fractionating tower technique, process are as shown in Figure 1.Figure
In, through recycle slurry oil once exchange heat to 220 DEG C fresh feed (214t/h, wherein lightweight material first vacuum side stream 24t/h, it
30% engler's boiling range is 365 DEG C) and recycle oil (46t/h, 334 DEG C) from 10 lower part of main fractionating tower it is anti-into riser respectively
Device 5 is answered, under the action of high temperature (about 650 DEG C) regenerated catalyst from regenerator sloped tube 7, along promotion tube edge rising edge to fluidize
Catalytic cracking reaction occurs for state, to settler 6 through dilatation sedimentation and cyclonic separation, by the reclaimable catalyst of area carbon from anti-
It answers in product and removes.Reclaimable catalyst is through inclined tube 8 to be generated from regenerator is pressed into, and reaction oil gas (274.4t/h, 500 DEG C) is then from pressure
Into 10 desuperheating section of main fractionating tower for arranging 10 layers of herringbone baffle.In desuperheating section, the sensible heat of high-temperature oil gas about 2312 ×
104Kcal/h is taken out by circulation slurry oil, and primary heating raw material is secondary that steam generator 2 is sent to generate 3.5MPa saturation steaming to 220 DEG C
Vapour 21t/h, and then enter rectifying section for about 367 DEG C close to the reaction oil gas of saturated mode after desuperheating, in the first middle section, reflux 11 (is taken
Heat 1756 × 104Kcal/h) and top circulating reflux 4 (takes heat 1022 × 104Kcal/h it under the action of), is extracted out at the 3rd block of column plate
The recycle oil 46t/h that 5% boiling range of engler is 340 DEG C extracts the production that 95% boiling range of engler is 342 DEG C out at the 17th block of column plate
Product diesel oil 104.8t/h, bottom harvest product slurry oil 25.4t/h, and top obtains rich gas 30000Nm3/ h, raw gasoline 85t/h.
Boiling range is the most important quality index for evaluating liquid fuel vapo(u)rability.It can illustrate the boiling point model of liquid fuel
It encloses, and can judge the substantially content of weight component in oil product composition.50% recovered (distilled) temperature oil product carries out boiling range under prescribed conditions
The temperature observed simultaneously when being recovered to the condensate liquid of sample half volume in measurement, in graduated cylinder, indicates with DEG C.
Base oil properties factor K is commonly used to judge the content of diesel oil, and K value is bigger, and Determination of Diesel Oil is higher.
T: the mean average boiling point of oil product is typically now used
Denominator: for common relative density, i.e. the ratio between the density that is lauched of oil density and predetermined temperature.
Table 1 is the specific gravity and fraction distribution of comparative example product diesel oil.
The specific gravity and fraction distribution of 1 comparative example product diesel oil of table
Note: the point of the boiling range 95% of qualified diesel oil is not more than 365 DEG C.
Embodiment 1
This example avoids diesel oil from evaporating to be a kind of using catalytic cracking unit main fractionating tower desuperheating section separation lightweight material oil
Divide the new process for repeating processing.Its process is as shown in Figure 2.It is specific as follows:
Firstly, catalytic cracking reaction mechanism is extremely complex, therefore embodiment only calculates the inlet amount of fractionating column and riser
Distribution.It separates diesel oil distillate and is not involved in promotion tube reaction, it is possible to reduce coke and dry gas yield reduce aromatic component in diesel oil
Concentration improves its Cetane number.
Fresh feed (190t/h) without lightweight material first vacuum side stream (24t/h) is through circulation slurry oil primary heating to 220
DEG C and the recycle oil (64t/h, 334 DEG C) from 10 lower part of main fractionating tower successively into riser reactor 5, coming from regenerator sloped tube
Under the action of 7 high temperature (about 650 DEG C) regenerated catalyst, Catalytic Cracking Unit of Measure is carried out with fluidized state along tube edge rising edge is promoted
It answers, rises to settler 6 through dilatation sedimentation and cyclonic separation, the reclaimable catalyst of area carbon is removed from reaction product.
Reclaimable catalyst send regenerator through inclined tube 8 to be generated.Reaction oil gas (268.4t/h, 500 DEG C) is then pressed into main fractionation through oil transfer line certainly
10 desuperheating section of tower.Meanwhile the first vacuum side stream (24t/h, 160 DEG C) from special lightweight material surge tank also by nozzle with
Spray pattern enters oil transfer line, and common (292.4t/h, 468 DEG C) is into desuperheating section.In desuperheating section, recycles slurry oil and take out oil gas
Sensible heat 1836 × 104Kcal/h, wherein primary be used to heat 190t/h raw material to 220 DEG C, it is secondary for being produced in steam generator 2
Raw 3.5MPa saturated vapor 14.7t/h, and then enter rectifying section for about 367 DEG C close to the reaction oil gas of saturated mode after desuperheating,
First middle section reflux 11 (takes heat 1867 × 104Kcal/h) and top circulating reflux 4 (takes heat 1020 × 104Kcal/h under the action of),
It extracts the recycle oil 64t/h that 5% boiling range of engler is 337 DEG C out at the 3rd block of column plate, extracts engler 95% out at the 17th block of column plate
The product diesel oil 104.8t/h that point boiling range is 334 DEG C, bottom harvest product slurry oil 25.4t/h, and top obtains rich gas 30000Nm3/
H, raw gasoline 85t/h.
Table 2 is the specific gravity and fraction distribution of embodiment product diesel oil.
The specific gravity and fraction distribution of 2 embodiment product diesel oil of table
Embodiment 1 is compared with comparative example:
1) 24t/h lightweight first vacuum side stream is direct into 10 desuperheating section of main fractionating tower, and contained 6t/h diesel oil distillate is anti-
Answer oil gas surplus heat direct gasification into rectifying section top, without reacting with recycle oil into riser reactor, not only
Reduce the processing capacity of reaction system, it is thus also avoided that the cracking (Cheng Ganqi) and coking that 6t/h diesel oil distillate is likely to occur.
2) product diesel oil boiling range lightens, and specific gravity drops to 0.878 from 0.881, and characteristic factor is increased to 11.3 from 11.18,
Illustrate that Determination of Alkane Content increases, arene content declines.
3) due to the 24t/h first vacuum side stream that gasified, 10 desuperheating section surplus heat of main fractionating tower is from 2312 × 104Kcal/h drop
To 1836 × 104Kcal/h, decline 20.6%, but the first middle section reflux 11 takes heat from 1756 × 104Kcal/h is raised to × 1867 ×
104Kcal/h rises 6.3%, and top circulation then varies less, and keeps 1022 × 10 substantially4Kcal/h, this illustrates main in this technique
Total surplus heat of fractionating column system reduces, and since the surplus heat of main fractionating tower 10 is burnt from regeneration, this illustrates that this technique is total
Body is energy-efficient.
In conclusion this technique avoid diesel oil distillate enter riser occur catalytic cracking, not only reduce dry gas and
The yield of coke；It protects the alkane molecule in diesel oil to be converted into aromatic hydrocarbon molecule again, improves the quality of catalyst article diesel oil；More
Because catalysis processing capacity is reduced, coke output decline, so that plant energy consumption reduces.Due to only needing torpedo lightweight material oily, this technique
Flow change is small, is suitable for old plant modification and new equipment designs.
The above embodiment is a preferred embodiment of the present invention, but embodiments of the present invention are not by above-described embodiment
Limitation, other any changes, modifications, substitutions, combinations, simplifications made without departing from the spirit and principles of the present invention,
It should be equivalent substitute mode, be included within the scope of the present invention.
Claims (8)
1. a kind of method for separating diesel oil distillate from lightweight material oil, which is characterized in that urged using catalytic cracking unit
Change cracking reaction, the device includes main fractionating tower and riser reactor, and main fractionating tower is divided into desuperheating section and rectifying column
Section, the specific steps are as follows:
(1) heavy raw oil is passed through riser reactor and carries out catalytic cracking reaction, generate pyroreaction oil gas；
(2) it is passed through the desuperheating section and rectifying tower section of main fractionating tower after mixing pyroreaction oil gas with lightweight material oil, separates
Obtain diesel oil distillate and freshening oil distillate.
2. the method according to claim 1, wherein
Temperature before the mixing of lightweight material oil described in step (2) is controlled at 160~180 DEG C.
3. according to the method described in claim 2, it is characterized in that,
Temperature before the mixing of lightweight material oil described in step (2) is controlled at 170 DEG C.
4. the method according to claim 1, wherein
Lightweight material oil described in step (2) by nozzle directly with pyroreaction air-fuel mixture.
5. the method according to claim 1, wherein
Step (1) the desuperheating section head gas temperature control is at 360~380 DEG C.
6. according to the method described in claim 5, it is characterized in that,
Step (1) the desuperheating section head gas temperature control is at 370 DEG C.
7. method described in any one according to claim 1~6, it is characterised in that:
The freshening oil distillate that main fractionating tower described in step (2) obtains distillates control at 345-355 DEG C.
8. according to the method described in claim 7, it is characterized by:
The freshening oil distillate that main fractionating tower described in step (2) obtains distillates control at 350 DEG C.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| GB722369A (en) * | 1951-08-18 | 1955-01-26 | Bataafsche Petroleum | Improvements in and relating to the cracking of heavy hydrocarbon oils |
| US4676888A (en) * | 1986-03-19 | 1987-06-30 | Exxon Research And Engineering Company | Hydrocarbon conversion process with product quenching |
| CN104610995B (en) * | 2013-11-05 | 2018-10-12 | 中国石油化工股份有限公司 | A kind of production method of matrix pitch |
| CN104927909A (en) * | 2015-05-26 | 2015-09-23 | 成都高普石油工程技术有限公司 | Reaction-regeneration device in catalytic cracking |
| CN106883871B (en) * | 2015-12-16 | 2018-11-16 | 中国石油天然气股份有限公司 | A kind of production method of needle-shape coke raw material |
| CN106811234B (en) * | 2017-02-10 | 2018-04-24 | 武汉科技大学 | A kind of delayed coking system and method |
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