CN105694966B - A kind of method that naphtha and clean gasoline are produced by catalytic cracking diesel oil - Google Patents
A kind of method that naphtha and clean gasoline are produced by catalytic cracking diesel oil Download PDFInfo
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- CN105694966B CN105694966B CN201610178572.8A CN201610178572A CN105694966B CN 105694966 B CN105694966 B CN 105694966B CN 201610178572 A CN201610178572 A CN 201610178572A CN 105694966 B CN105694966 B CN 105694966B
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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
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
- C10G65/12—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/30—Physical properties of feedstocks or products
- C10G2300/301—Boiling range
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
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- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention is a kind of method that naphtha and clean gasoline are produced by catalytic cracking diesel oil, including：Enter the middle part for the hydrocracking reactor hydrofining reactor that inverted sequence is loaded after catalytic cracking diesel oil is mixed with hydrogen, the crackate come with hydrocracking reactor enters hydrofining reactor after mixing and carries out hydrofining reaction, to remove the impurity such as sulphur nitrogen, and carry out olefin saturation and aromatic hydrogenation saturation；Cutting process is carried out for the product after hydrofinishing, the distillate less than 165 DEG C is gone as raw materials for catalytic reforming device as naphtha product；165~205 DEG C of distillate is used as clean gasoline blend component；205~320 DEG C of distillate returns to the top of the hydrocracking reactor hydrofining reactor of inverted sequence filling, is hydrocracked, hydrofining reaction；Distillate more than 320 DEG C returns to the further cracking of catalytic cracking unit or enters other hydrogenation plant working processes.The inventive method is for the purpose of voluminous naphtha product, while clean gasoline can be produced.
Description
Technical field
A kind of method that the present invention produces naphtha and clean gasoline for utilization catalytic cracking diesel oil.
Background technology
In the case where developing low-carbon economy, recycling economy, realizing the situation of sustainable development, China's oil quality upgrading paces are bright
Aobvious to accelerate, the requirement to arene content in diesel oil is also more and more stricter.Clear gusoline is produced to send out as current petroleum refining industry of China
One of emphasis of exhibition.During China's diesel oil is constituted, it is catalytic cracking diesel oil to have 25~30%.Catalytic cracking diesel oil has arene content
High (the general ＞ 60% of arene content), the characteristics of Cetane number is low, its inferior quality, it is necessary to changed by hydrofinishing or hydrogenation
Matter just can be used as fuel oil blend component.But hydro-upgrading operating cost is high, condition harsh, and Cetane number improves limited,
Cause fuel oil cost unprecedented soaring.Increasingly strict with domestic clear gusoline standard, catalytic cracking diesel oil is contained due to aromatic hydrocarbons
Amount is high to turn into the bottleneck that restriction relevant unit production high standard cleans diesel oil, how to reduce arene content in catalytic cracking diesel oil,
Turn into a problem of puzzlement refinery so as to improve its Cetane number.
At the same time, world market is also constantly accelerated to the growth rate of aromatic hydrocarbons demand.With China's arene industrial
Develop, supply falls short of demand for the light aromatics such as BTX, and added value of product is higher.Domestic catalytic reforming unit quantity increases, and I
State's processing crude oil is heavier, and light oil yield is low, causes naphtha breach big.Substantial amounts of aromatic radical is rich in catalytic cracking diesel oil
Group, about containing 50~80% aromatic hydrocarbons, this part aromatic component is complicated, it is difficult to which separation is utilized, and is the potential resource for preparing BTX,
Therefore carrying out catalytic cracking diesel oil lighting production naphtha technology has good market application foreground.
At this stage, the industrial main method for improving catalytic cracking diesel oil quality is hydrofinishing and hydro-upgrading, hydrogenation
Refined research is relatively more, is also significantly improved on the basis of traditional Hydrofining Technology.Although hydrofinishing can be real
Existing deep desulfuration denitrogenation, but Cetane number is typically only capable of raising 4~8, is split especially for the high catalysis inferior of arene content
Change diesel oil, hydrofining diesel oil Cetane number is still less than 35, it is difficult to make preferable diesel oil blending component.It is another through frequently with
Method be hydro-upgrading, typically first pass through hydrofinishing desulfurization removing nitric, then hydrogenated modification improves diesel cetane-number, it is this
The hydro-upgrading of poor quality catalytic cracking diesel needs to consume substantial amounts of hydrogen and uses relatively low reaction velocity, corresponding operating cost
With height.Current China Diesel yield has no longer been the high (hexadecane of arene content in that short situation of past, catalytic cracking diesel oil
Value<25) it has not been in the present case an economically viable route, to take hydrogenation modification method to produce diesel oil, wherein containing
A large amount of aromatic hydrocarbon resources fail to make full use of.
CN1064988C discloses a kind of diesel oil fraction hydrogenation converting process, and this method uses a kind of hydrogenation containing molecular sieve
Reforming catalyst, using one-stage process, series connection one-stage process and two-stage method hydrogenation technique flow to poor ignition quality fuel, particularly catalytic diesel oil
(LCO) Porous deproteinized bone, desulfurization are carried out and diesel cetane-number is improved.But the diesel oil regulation index of this method production is relatively low, as sulphur contains
Amount is less than 0.05 heavy %, and a large amount of aromatic components that arene content is less than in 20 heavy %, catalytic cracking diesel oil raw material are hydrogenated saturation,
Fail utilization very well.
A kind of method that US6623628B1 discloses use two-stage method production low-sulfur, low aromatic hydrocarbons and high cetane number diesel oil.
Using two reactors in this method, one it is anti-in catalyst using at least one from vib and at least one from the
Element in VIII is active component, two it is anti-in catalyst use at least one noble metal in group VIII
For active component.Stripper is provided between two reactors, the gaseous impurities such as the anti-hydrogen sulfide produced and ammonia are removed totally,
To protect two anti-noble metal catalysts.It is 150 DEG C~370 DEG C of intermediate oil that this method, which can process boiling range, production low-sulfur,
Low aromatic hydrocarbons and high cetane number diesel oil.But raw material used is lighter in this method, and arene content is low；In addition, being used in this method
Noble metal catalyst causes cost to increase, and operating risk is big, operating flexibility declines.
CN101760239A discloses a kind of Application way of catalytic cracking diesel oil, and catalytic cracking diesel oil is separated into boiling point
Component and boiling point less than 230 DEG C are more than 230 DEG C of component, and the component to boiling point higher than 230 DEG C is hydrogenated with many cyclophanes
Hydrocarbon is converted into mononuclear aromatics, finally isolates the diesel oil rich in mononuclear aromatics from the component after two kinds of processing and carries out catalysis and splits
Change.This method can improve hydrogenation selectivity, and arene content and the high FCC gasoline of octane number is made, but due to taking catalysis to split
The diesel oil that change method is rich in mononuclear aromatics to isolating is handled, and necessarily causes a large amount of dry gas, liquefied gas and coke etc. to produce,
Economy is poor in actual production.
The above method, either hydrofinishing or solvent refining, is all only absorbed in the improvement of catalytic cracking diesel oil property,
Without being comprehensively utilized to aromatic hydrocarbons therein, the maximization generated profit.
Uop Inc. is developed with catalytic cracking diesel oil (also known as light circulation to provide more xylene production raw materials
Oil, LCO) it is the LCO-X techniques that raw material produces high-quality dimethylbenzene, the removal of impurity is gone by hydrotreating, then light naphthar is entered
Row conversion, realizes that aromatic hydrocarbon product is maximized, substantially produces benzene and mixed xylenes.It is right in LCO-X technique xylene products
Xylene concentration is higher than other aromatics production techniques, and the mixed xylenes of output can provide higher for chemical products user
Paraxylene yield.
Some technical concerns are in the exploitation of catalytic cracking diesel oil hydrocracking technology at this stage, to improve gasoline fraction yield
And octane number.
CN103773487B discloses a kind of method for hydrogen cracking of catalytic cracking diesel oil, the mixing of diesel raw material and hydrogen
Thing is in hydrofining reactor and Hydrobon catalyst haptoreaction, and hydrofining reactor liquid efflunent is without any point
From, contact, react with hydrocracking catalyst into hydrocracking reactor, the reaction effluent warp point of hydrocracking reactor
From, fractionation after obtain hydrogen-rich gas, light naphtha fraction, gasoline fraction, freshening cut and diesel oil distillate, described freshening cut
Boiling range be 190 DEG C~300 DEG C, the freshening cut is back to hydrocracking reactor entrance.
CN104611050A discloses a kind of catalytic cracking diesel oil method for transformation.Catalytic diesel oil is introduced into after being mixed with hydrogen
Hydrofining reactor carries out hydrofining reaction；Hydrofining reaction effluent is directly entered hydrocracking reactor, with splitting
Change the beds haptoreaction that level is matched somebody with somebody in reactor；At least two Cracking catalyst are wherein set in hydrocracking reactor
Bed, according to the flow direction of reaction mass, the hydrogenation activity of hydrocracking catalyst is in reduction trend；Hydrocracking reaction stream
Go out thing by separation and be fractionated, obtain naphtha and diesel oil.
Above-mentioned two method purpose is that gasoline fraction yield and octane number can be effectively improved, using hydrofinishing with adding
Hydrogen cracking tandem process technology carries out hydrotreating.Exist for catalytic cracking diesel oil raw material sulfur-nitrogen compound, it is hydrogenated refined
Generation hydrogen sulfide and ammonia afterwards, hydrofining reactor effluent is directly entered hydrocracking reactor, due to basic nitrogen compound with
The presence of ammonia, will influence the acid centre of hydrocracking catalyst, cause Cracking catalyst activity decrease, bad stability.
To ensure naphtha yield, the boiling range general control of freshening cut is less than 300 DEG C；Simultaneously with fresh material and freshening cut sum
Meter, to ensure cracking zone conversion ratio, hydrocracking reactor volume is big and loaded catalyst is big, causes plant investment big.
If using the advantage of integrated petrified enterprise, by catalytic cracking diesel oil hydro-upgrading and Aromatic Hydrocarbon United Plant,
Optimize existing apparatus raw material and process structure, all kinds of raw material resources can be made full use of, be expected to while solving clean fuel and virtue
Hydrocarbon industry problem encountered.Deep desulfuration denitrogenation can be realized to catalytic cracking diesel oil using hydrogen addition technology, is changed into simultaneously
High arene underwater content naphtha, as raw materials for catalytic reforming device, realizes increase aromatic hydrocarbon product yield, alleviates market supply and demand lance
Shield.
The content of the invention
It is an object of the invention to provide the method for a kind of catalytic cracking diesel oil production naphtha and clean gasoline, with maximum
Metaplasia produces naphtha, and high-quality feed naphtha is provided for catalytic reforming unit.
The method that naphtha and clean gasoline are produced by catalytic cracking diesel oil that the present invention is provided, comprises the following steps：
1) hydrocracking reactor-hydrofinishing of an inverted sequence filling is entered after catalytic cracking diesel oil is mixed with hydrogen
The middle part of reactor, the crackate come with top hydrocracking reactor is downwardly into hydrofining reactor after mixing,
Hydrofining reaction is carried out under hydrogenation conditions；
2) cutting process is carried out for the product after hydrofinishing, wherein：
~165 DEG C a.65 distillate goes, as raw materials for catalytic reforming device, to produce aromatic hydrocarbon product as naphtha product；
~205 DEG C b.165 distillate is used as clean gasoline blend component；
~320 DEG C c.205 distillate returns to the top of hydrocracking reactor-hydrofining reactor of inverted sequence filling
Portion, enters hydrocracking reactor and carries out hydrocracking reaction, isocrackate is downwardly into hydrogenation essence after being mixed with hydrogen
Reactor processed；
d.>320 DEG C of distillate returns to the further cracking of catalytic cracking unit or gone at other hydrogenation plant processing
Reason.
In above-mentioned technical proposal of the present invention, wherein hydrocracking reactor-hydrofinishing that 1) inverted sequence described in step is loaded
The admission space ratio of reactor, hydrocracking catalyst and Hydrobon catalyst is 0.2:1~1:1, hydrofining reaction
Device fresh catalyst cracked diesel oil mass space velocity is 0.5~1.5h-1, hydrogen/oil volume ratio is 300~800：1, hydrocracking reactor
205~320 DEG C of distillate mass space velocity is 0.5~1.5h-1。
Hydrofining reactor preferably shares a set of make-up hydrogen compressor with hydrocracking reactor and a set of followed in the present invention
Ring hydrogen processing system, to realize reduction equipment investment.
The Cetane number of described catalytic cracking diesel oil is less than 35, wherein the aromatic hydrocarbons containing 50~85 mass %.
The end point of distillation of described catalytic cracking diesel oil cuts to 390 DEG C.
Compared with prior art, this have the advantage that：
1st, the method provided using the present invention, can obtain the naphtha production that sulphur nitrogen content is respectively less than 0.5ug/g, Gao Fangqian
Product, meet the feed needs of catalytic reforming unit.
2nd, the method provided using the present invention, because hydrotreated product is separated except ammonia, then it is cleaved, split into hydrogenation
Change reactor oil distillation is light, nitrogen content is low, is hydrocracked high conversion rate, and inverted sequence hydrotreating is beneficial to Cracking catalyst activity hair
Wave and keep activity stability, it is ensured that maximization obtains high-quality naphtha product, and the plant running cycle is long.
3rd, the method provided using the present invention, the technological process of production is simple, and equipment investment is low, and adaptability to raw material is good, can locate
Manage high-sulfur, high nitrogen, the catalytic cracking diesel oil cut that boiling range scope is wide and tenor is high.
4. the inventive method is for the purpose of maximizing production naphtha, naphtha yield is more than 60 mass %, while and production
Clean gasoline blend component.Naphtha product can directly enter catalytic reforming unit, finally give lightweight BTX aromatic hydrocarbon products, from
And realize effective utilization of catalytic cracking diesel oil each component.
Brief description of the drawings
Fig. 1 is a kind of one kind side of being preferable to carry out of the method for catalytic cracking diesel oil production naphtha and clean gasoline of the invention
The schematic flow sheet of formula.
1 is catalytic cracking diesel oil feedstock oil, and 2,16 be new hydrogen, and 3 be hydrofining reactor, and 4 be high-temperature separator, and 5 are
High-temperature separator top gas, 6 be cooler, and 7 be cold catch pot, and 8 be cold catch pot top gas, and 9 be caustic wash tower, 10
It is recycle hydrogen for circulating hydrogen compressor, 11,12,13 be stabilizer, and 14 be fractionating column, and 15 be 205~320 DEG C of distillate, 17
It is hydrocracking reactor for heating furnace, 18,19 be liquefied petroleum gas, and 20 be dry gas, 21 heat exchangers
Embodiment
The following examples and accompanying drawing will be further described to the inventive method, but therefore not limit this hair
It is bright.
The method of catalytic cracking diesel oil production naphtha and clean gasoline of the present invention, first mixes catalytic cracking diesel oil with hydrogen
Close, into the middle part of hydrocracking reactor-hydrofining reactor of an inverted sequence filling, with top hydrocracking reactor
Hydrofining reactor is downwardly into after the crackate mixing come, it is anti-that hydrogenation desulfurization and denitrogenation mainly occurs for hydrofining reactor
Answer, while occurring alkene saturation and aromatic hydrocarbons saturation, wherein aromatic hydrocarbons saturated reaction is mainly the hydrogenation saturation of polycyclic aromatic hydrocarbon.
Inverted sequence filling be hydrocracked-hydrofinishing of hydrofining reactor bottom after product carry out cutting separation, wherein
205~320 DEG C of distillate returns to the top of hydrocracking reactor-hydrofining reactor of inverted sequence filling, into adding
Hydrogen cracker carries out hydrocracking reaction, and isocrackate is downwardly into hydrofining reactor；This is hydrocracked instead
Answer device hydrocracked, treated mainly to occur mononuclear aromatics chain rupture, opening cyclic paraffins chain-breaking reaction, make to produce by hydrocracked, treated
Thing boiling range is reduced to less than 205 DEG C.Enter hydrocracking reactor, phase due to there was only 205~320 DEG C of distillate as raw material
For catalytic cracking diesel oil processing capacity, the size and loaded catalyst of hydrocracking reactor are reduced.
Isocrackate is mixed into hydrofining reactor with catalytic cracking diesel oil raw material, realizes that the depth of product takes off
Sulphur denitrogenation and olefin saturation, realize sulphur, the nitrogen content respectively less than 0.5ug/g, vapour of the distillate of 65~165 DEG C of polishing
Oil product sulphur, nitrogen content are respectively less than 10ug/g.
Product is cut after hydrofinishing, and described 65~165 DEG C of distillate enters as catalytic reforming raw material after cutting
Enter catalytic reforming unit, wherein cycloalkane and arene content is no less than 60 mass %.
Catalytic cracking diesel oil hydrofining reactor, available reaction temperature be 320~390 DEG C, hydrogen dividing potential drop be 5.0~
10.0MPa, fresh catalyst cracked diesel oil mass space velocity is 0.5~1.5h-1, hydrogen/oil volume ratio is 300~800：1.
If carbon residue or tenor are higher in catalytic cracking diesel oil feedstock oil, to prevent the pressure drop of beds
Limit value is reached soon, and adding for hydrofinishing agent volume total amount 5~20% can be accounted in Hydrobon catalyst bed top loading
Hydrogen protective agent, to protect major catalyst, avoid the quick coking of bed.
205~320 DEG C of distillate returns to hydrocracking reactor after refined products cutting, available to be hydrocracked instead
It is 380~440 DEG C to answer temperature, and hydrogen dividing potential drop is 5.0~10.0MPa, 205~320 DEG C of distillate mass space velocity for 0.5~
1.5h-1, hydrogen/oil volume ratio is 300~800：1.
With the difference of the catalytic cracking diesel oil raw material end point of distillation, it is hydrogenated it is refined after, the cut oil content more than 320 DEG C is general
About 10~20%, due to cut weight, cracking activity is low, is difficult to convert into hydrocracking reactor, can return to catalysis
The further cracking of cracking unit, or other hydrogenation plant working processes are gone, such as with straight-run diesel oil, coker gas oil mixed hydrogenation essence
System production cleaning diesel product, or go high-pressure hydrocracking device working process.
One kind of method of a kind of catalytic cracking diesel oil production naphtha of the invention and clean gasoline is given in Fig. 1 preferably
Some equipment, such as pump, heat exchanger are eliminated in the schematic flow sheet of embodiment, figure, but this is to ordinary skill people
Member is known.As shown in figure 1, the flow of the inventive method is described in detail as follows：Catalytic cracking diesel oil raw material from pipeline
Oil 1 enters after being mixed with new hydrogen 2 to be hydrocracked in the middle part of hydrocracking reactor-hydrofining reactor that inverted sequence is loaded with top
Enter hydrofining reactor 3 after the crackate mixing of reactor 18, carry out desulfurization, denitrogenation, alkene saturation and aromatic hydrocarbons full
And reaction.Refined products enter high-temperature separator 4, after high-temperature separator top gas 5 is cooled down through cooler 6, into low temperature point
From device 7, after cold catch pot top gas 8 is washed through caustic wash tower 9, into circulating hydrogen compressor 10, part recycle hydrogen 11 go with
Catalytic cracking diesel oil raw material 1 is mixed, and part recycle hydrogen 12 carrys out 205~320 DEG C of distillates 15 with fractionating column and mixed.High-temperature separator
4 bottom liquids flow out thing and enter the removing dry gas 20 of stabilizer 13 and liquefied petroleum gas 19, and the bottoms effluent of stabilizer 13, which enters, to be divided
Evaporate tower 14 and carry out cutting separation, add wherein 205~320 DEG C of distillate 15 returns to enter after mixing with new hydrogen 16, recycle hydrogen 12
Hot stove 17 heats, exchange heat after, at the top of the hydrocracking reactor loaded into inverted sequence-hydrofining reactor, be downwardly into plus
Hydrogen cracker 18 carries out hydrocracked, treated, then proceedes to be downwardly into hydrofining reactor 3, finally with hydrofinishing
Product outflow reactor, goes later separation, and after the cutting of fractionating column 14, the distillate less than 165 DEG C goes to make as naphtha product
For raw materials for catalytic reforming device, 165~205 DEG C of distillate is used as clean gasoline blend component；>320 DEG C of distillate is returned
Go the further cracking of catalytic cracking unit or go other hydrogenation plant working processes.
The product designation THDS-I of Hydrobon catalyst used, the business of hydrocracking catalyst in example below
Brand number is THHC-II, by CNOOC Tianjin Chemical Research ＆ Design Institute's development and production.Feedstock oil used has two kinds in embodiment
Catalytic cracking diesel oil, its main character is as shown in table 1.
The catalytic cracking diesel oil main character of table 1
| Feedstock oil | Catalytic cracking diesel oil I | Catalytic cracking diesel oil II |
| Density (20 DEG C), g/cm3 | 0.9042 | 0.9762 |
| Sulfur content, μ g/g | 2890 | 5370 |
| Nitrogen content, μ g/g | 1359 | 801 |
| Bromine valency, gBr/100g | 3.4 | 11.3 |
| Aromatic hydrocarbons, quality % | 75.9 | 85.2 |
| Polycyclic aromatic hydrocarbon, quality % | 22.4 | 63.3 |
| Boiling range ASTM D-1160, DEG C | ||
| IBP | 185 | 185 |
| 5% | 211 | 210 |
| 10% | 239 | 225 |
| 50% | 288 | 268 |
| 90% | 372 | 339 |
| FBP | 390 | 368 |
Embodiment 1
Catalytic cracking diesel oil, production naphtha and clean gasoline product are handled by the inventive method.
Enter inverted sequence serial hydrocracking-hydrogenation essence using catalytic cracking diesel oil I as raw material, after being mixed with new hydrogen with recycle hydrogen
The middle part of High-pressure Hydrogenation Unit processed, is downwardly into second segment hydrofining reactor.Hydrofinishing section Hydrobon catalyst dress
The amount of filling out is 200mL, is hydrocracked section hydrocracking catalyst loadings for 200mL.Hydrotreated product is laggard through gas-liquid separation
Enter continuous distillation plant, cut cutting is carried out, after 205~320 DEG C of distillates returns are mixed with new hydrogen with recycle hydrogen, into inverted sequence
That connects is hydrocracked-hydrofinishing High-pressure Hydrogenation Unit top first paragraph hydrocracking reactor, then is hydrogenated with by second segment
Finishing reactor.Hydrogen dividing potential drop is 5.5MPa, and hydrofinishing section reaction temperature is 350 DEG C, fresh catalyst cracked diesel oil mass space velocity
For 0.8h-1, hydrogen/oil volume ratio is 600：1, section reaction temperature is hydrocracked for 380 DEG C, is hydrocracked section>355 DEG C of cut oil
Amount air speed is 0.65h-1, hydrogen/oil volume ratio is 450：1.
65~165 DEG C of distillates are obtained after product fractionation as catalytic reforming unit feed naphtha, its property is shown in Table
4.165~205 DEG C of distillates are shown in Table 5 as high-knock rating gasoline blend component, its property.
Embodiment 2~5
Step is processed to catalytic cracking diesel oil I and catalytic cracking diesel oil II respectively as described in Example 1, no
Same is the selection of reaction condition, and the experimental condition of selection is shown in Table 2.
Calculated with catalytic cracking diesel oil raw material, different fractions oil product property is shown in Table 3~table 4, different fractions oil product is received
Rate is shown in Table 5.
The experimental condition of table 2
3 65~165 DEG C of naphtha properties of table
| Project | Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | Embodiment 5 |
| Density (20 DEG C), g/cm3 | 0.705 | 0.701 | 0.730 | 0.728 | 0.732 |
| Sulfur content, μ g/g | 0.3 | 0.2 | 0.2 | 0.2 | 0.2 |
| Nitrogen content, μ g/g | 0.2 | 0.1 | 0.1 | 0.1 | 0.2 |
| Aromatic hydrocarbons, quality % | 35.1 | 33.2 | 40.8 | 40.5 | 42.6 |
| Cycloalkane, quality % | 40.1 | 42.6 | 44.2 | 44.1 | 41.3 |
4 165~205 DEG C of cut oil natures of table
| Project | Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | Embodiment 5 |
| Density (20 DEG C), g/cm3 | 0.715 | 0.716 | 0.742 | 0.746 | 0.748 |
| Sulfur content, μ g/g | <1 | <1 | <1 | <1 | <1 |
| Nitrogen content, μ g/g | <1 | <1 | <1 | <1 | <1 |
| Aromatic hydrocarbons, quality % | 46.8 | 46.1 | 47.5 | 47.9 | 49.2 |
| Polycyclic aromatic hydrocarbon, quality % | 0.6 | 0.4 | 0.8 | 0.5 | 0.9 |
| Research octane number (RON) | 91.7 | 91.5 | 92.1 | 92.4 | 92.8 |
The different fractions oil product yield of table 5
From the result of 3~table of table 5, catalytic cracking diesel oil is handled by the inventive method, 65~165 DEG C of obtained naphthas
Middle sulphur, nitrogen content are respectively less than 0.5 μ g/g, and aromatic hydrocarbons and naphthene content are more than 65 mass %, can be filled as the catalytic reforming of high-quality
Feed naphtha is put, aromatic hydrocarbon product is produced.The research octane number (RON) of 165~205 DEG C of clean gasoline cuts reaches more than 91.To locate
The catalytic cracking diesel oil raw material of reason is calculated, and 65~165 DEG C of naphtha yields are more than 60 mass %, while can obtain clean gasoline
Product.
Claims (6)
1. a kind of method that naphtha and clean gasoline are produced by catalytic cracking diesel oil, comprises the following steps：
1）Enter hydrocracking reactor-hydrofining reaction of an inverted sequence filling after catalytic cracking diesel oil is mixed with hydrogen
The middle part of device, the crackate come with top hydrocracking reactor is downwardly into hydrofining reactor after mixing, in hydrogenation
Hydrofining reaction is carried out under reaction condition；
2）Cutting separating treatment is carried out for the product after hydrofinishing, wherein：
A) 65 ~ 165 DEG C of distillate is naphtha product, is further used as raw materials for catalytic reforming device, produces aromatic hydrocarbon product；
B) 165 ~ 205 DEG C of distillate is used as clean gasoline blend component；
C) 205 ~ 320 DEG C of distillate returns to the top of hydrocracking reactor-hydrofining reactor of inverted sequence filling, with
Enter hydrocracking reactor after hydrogen mixing and carry out hydrocracking reaction, isocrackate is downwardly into hydrofining reaction
Device；
d)>320 DEG C of distillate enters other hydrogenation plant working processes.
2. in accordance with the method for claim 1, it is characterised in that 1）Walk inverted sequence filling hydrocracking reactor-plus
The admission space ratio of hydrogen finishing reactor, hydrocracking catalyst and Hydrobon catalyst is 0.2:1~1:1, hydrogenation essence
Reactor fresh catalyst cracked diesel oil mass space velocity processed is 0.5~1.5h-1, hydrogen/oil volume ratio is 300~800：1, it is hydrocracked
The distillate mass space velocity of 205 ~ 320 DEG C of reactor is 0.5~1.5h-1。
3. in accordance with the method for claim 1, it is characterised in that hydrofining reactor shares one with hydrocracking reactor
Cover make-up hydrogen compressor and a set of recycle hydrogen processing system.
4. according to the method described in claim 1, it is characterised in that 65 ~ 165 DEG C described of distillate is as urging after cutting
Change reformer feed and enter catalytic reforming unit, wherein cycloalkane and arene content is no less than 60 mass %.
5. according to the method described in claim 1, it is characterised in that the Cetane number of described catalytic cracking diesel oil is less than 35,
Wherein contain 50~85 mass % aromatic hydrocarbons.
6. according to the method described in claim 1, it is characterised in that the end point of distillation of described catalytic cracking diesel oil cuts to 390
℃。
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| US20210340449A1 (en) * | 2018-09-29 | 2021-11-04 | Uop Llc | Process for maximizing production of heavy naphtha from a hydrocarbon stream |
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| CN116333777A (en) * | 2021-12-24 | 2023-06-27 | 中国石油天然气股份有限公司 | Method for catalyzing diesel oil hydrocracking and catalytic cracking product obtained by same |
| CN116515524A (en) * | 2022-07-25 | 2023-08-01 | 中国石油化工股份有限公司 | Method for producing light aromatic hydrocarbon by secondary hydrogenation of inferior diesel oil |
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