CN106479566B - A kind of method for hydrogen cracking producing premium and diesel oil - Google Patents
A kind of method for hydrogen cracking producing premium and diesel oil Download PDFInfo
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- CN106479566B CN106479566B CN201510797913.5A CN201510797913A CN106479566B CN 106479566 B CN106479566 B CN 106479566B CN 201510797913 A CN201510797913 A CN 201510797913A CN 106479566 B CN106479566 B CN 106479566B
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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
-
- 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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- 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
- C10G2400/04—Diesel oil
Abstract
The invention discloses a kind of method for hydrogen cracking producing premium and diesel oil.After the hydrogenated pretreatment of vegetable and animals oils, into hydrocracking reactor, with hydrocracking catalyst I under relative low temperature, large volume space velocities haptoreaction；After gained product is mixed with poor ignition quality fuel hydrofinishing product again, with II haptoreaction of hydrocracking catalyst；Reaction product is through detaching and fractionation obtains premium and diesel oil.The present invention has fully considered the reapective features of vegetable and animals oils hydro-upgrading and poor ignition quality fuel hydroconversion process, reasonably effectively combines two kinds of techniques, can produce high octane gasoline products and diesel product simultaneously, and improves the greasy property of diesel product.
Description
Technical field
It is more specifically a kind of with high arene content diesel oil distillate and dynamic the invention discloses a kind of method for hydrogen cracking
Vegetable oil is raw material, and produce high-knock rating gasoline and fine-quality diesel oil is hydrocracked combined method.
Background technology
Since 21st century, with being increasingly enhanced of people's environmental consciousness, national environmental protection regulation it is increasingly stringent
And the fast development of national economy, demand of the countries in the world to cleaning automotive fuel are all being continuously increased.
Catalytic cracking（FCC）Technology is one of main technique means of heavy oil lighting, the oil refining enterprise in countries in the world
In all occupy important status.In Chinese heavy oil lighting processing unit (plant), catalytic cracking unit working ability institute accounting
Example is more prominent, and in petrol and diesel oil product composition, catalytically cracked gasoline accounts for 80% or so, and catalytic diesel oil accounts for 30% or so.In recent years,
With the increasingly heaviness of crude oil, the raw material that catalytic cracking is processed also heaviness and in poor quality increasingly, in addition many enterprises be
Achieve the purpose that improve quality of gasoline or propylene enhancing, catalytic cracking unit has been carried out to be transformed or improve catalytic cracking dress
The operating severity set causes the quality of the product of catalytic cracking, especially catalytic diesel oil more to deteriorate, and performance is predominantly close
Degree is high, and arene content is high, and sulphur nitrogen content is high, and Cetane number is low etc..Further include coal tar with above-mentioned property diesel oil distillate raw material,
Coal direct liquefaction oil etc..
Existing diesel oil distillate Raw material processing mode includes mainly hydrofinishing, hydro-upgrading and is hydrocracked.Add hydrogen smart
System, which can only remove impurity, the Cetane number such as sulphur, nitrogen in raw material, can only generally improve several units, and refined products evaporate for diesel oil
Point, but product cannot be satisfied other index requests of vehicle fuel.Hydro-upgrading purpose product be diesel product, removing sulphur,
Change molecular structure while nitrogen, to effectively improve Cetane number index, in general can by raw material Cetane number improve 10 ~
15 units, but for the too low raw material of Cetane number, the diesel oil that this method obtains still cannot be satisfied requirement.It is hydrocracked
Be by macromolecular cleavage it is small molecule, when using catalytic diesel oil as raw material, main purpose product is gasoline fraction, but art technology
Personnel know that the octane number for being hydrocracked gasoline is too low, are not used to blended gasoline product, the gasoline fraction in general obtained
It is divided into light naphthar and heavy naphtha two parts, light naphthar octane number is slightly higher, can be used for blended gasoline product, can also use
Preparing ethylene by steam cracking raw material is done, heavy naphtha octane number is lower, is generally used for reformer feed, is in addition hydrocracked gasoline fraction
It can be also used for production solvent oil product.
As world oil reserves are fewer and fewer, the utilization of the renewable resources such as vegetable and animals oils is also increasingly taken seriously.
The main component of animal and plant fat is straight chain fatty acid triglyceride, and wherein aliphatic acid face length is generally C12~C24, and
It is in the majority with C16 and C18.The Typical fatty acid that animal and plant fat contains includes saturated acid（Palmitic acid, stearic acid）, unitary it is unsaturated
Acid（Oleic acid）And polyunsaturated polycarboxylic acid（Linoleic acid, leukotrienes）, vegetable oil is based on a unsaturated diluted acid and dienoic acid, tallow
Then based on saturated fatty acid.Generation oil of these vegetable and animals oils after adding hydrogen is exactly diesel component, is mainly straight chain
Alkane, therefore, condensation point are higher, cannot meet the requirement of condensation point of diesel oil, but Cetane number is very high.Meanwhile vegetable and animals oils add hydrogen to obtain
The greasy property of the diesel oil arrived is relatively low, causes its wearability also poor.
Hydrocracking unit one-time investment is bigger, and operating cost is also relatively high.Therefore, the major research in countries in the world is public
Department is all largely studied positive to reduce the cost being hydrocracked, and makes great progress.In terms of catalyst：
The major patent quotient in the world had all in recent years constantly been catalyzed the emphasis that the update of catalyst develops as oneself technology
The material of agent, activity, service life, stability and reduction catalyst cost of catalyst etc. have done a large amount of work.In work
In terms of skill：Distillate hydrocracking technology is quite ripe, and each major oil companies are advanced optimizing the same of hydrocracking operation
When, innovative point is placed on and is hydrocracked on relevant group technology, cost is reduced by optimum organization technique；In addition, logical
The further investigation to being hydrocracked is crossed, the inherent connection between catalyst performance and feedstock property and purpose product quality is sought
System establishes suitable catalyst grade and matches the emphasis that system is also the current area research.
The processing technology of existing animal and plant fat hydrogenation method production automotive fuel, US20060186020, EP1693432,
CN201110217561.3、CN101321847A、CN200710012090.6、CN200680045053.9、
CN200710065393.4, CN200780035038.0, CN200710012208.5, CN200780028314.0 and
The patents such as CN101029245A disclose vegetable oil hydroconversion process, using coker naphtha, diesel oil distillate（Straight run bavin
Oil, LCO and coker gas oil）, the petroleum hydrocarbons such as wax oil fraction fraction and bio-oil be mixed into hydrogenation catalyst bed,
Produce diesel product or preparing ethylene by steam cracking raw material etc..US5705722 is disclosed containing plants such as unsaturated fatty acid, fat
The diesel oil blending component of oil and animal oil mixing back end hydrogenation production diesel oil distillate range.EP1741767 and EP1741768 are disclosed
A kind of method producing diesel oil distillate with animal and plant fat, predominantly animal and plant fat first pass around hydrotreating, then lead to
Isomerization catalyst bed layer is crossed, low freezing point diesel fuel component is obtained.
US 4676887 discloses a kind of technique producing high-knock rating gasoline.It is first by catalytic cracking diesel oil (LCO) etc.
It first passes through refining reaction area and carries out imurity-removal, and carry out aromatic moiety saturation, enter the progress open loop of cracking reaction area later and split
Change reaction, the diesel oil distillate being hydrocracked later enters catalyst cracker and handled, the essence which uses
Catalyst processed is also the catalyst for refining of existing commercialization.The technology refining stage severe reaction conditions, polycyclic aromatic hydrocarbon can be supersaturated, difficult
To achieve the purpose that produce high-knock rating gasoline.
Invention content
In view of the deficiencies of the prior art, the present invention provides one kind with high arene content poor-quality diesel-oil by cut fraction and vegetable and animals oils
For raw material, produce high-knock rating gasoline and fine-quality diesel oil is hydrocracked combined method.The method of the present invention has given full play to beta molecule
Sieve and Y molecular sieve type hydrocracking catalyst coupling advantage can produce high-octane rating vapour while scientific utilization reaction heat
The oil diesel oil good with super-low sulfur, high cetane number, greasy property.
The present invention it is a kind of produce high-knock rating gasoline and fine-quality diesel oil be hydrocracked combined method, including it is following interior
Hold：
（1）Vegetable and animals oils and hydrogen are mixed into vegetable and animals oils hydrofining reactor, and poor ignition quality fuel is mixed into hydrogen
Enter poor ignition quality fuel hydrofining reactor, contacted with Hydrobon catalyst, carries out hydrofining reaction respectively；
（2）Vegetable and animals oils hydrofinishing effluent is after dehydration, together with hydrogen, enters from reactor head plus hydrogen is split
Change reactor, contacted first with the hydrocracking catalyst I containing beta-molecular sieve, under the conditions of hydroisomerizing, carries out isomerization-visbreaking
Reaction；
（3）Step（2）Gained reaction product, then the poor ignition quality fuel hydrofinishing product with the introducing of reactor middle and upper part
It after mixing, is contacted with the hydrocracking catalyst II containing Y molecular sieve, under hydrocracking condition, carries out hydroconversion reactions；
（4）Step（3）Obtained reaction effluent carries out gas-liquid separation, obtains hydrogen-rich gas and fluid product；Hydrogen rich gas
Body can be recycled after purification by circulating hydrogen compressor, fluid product be fractionated to obtain gas, gasoline, diesel oil and
A small amount of tail oil fraction.
In the method for the present invention, the vegetable and animals oils include vegetable oil and/or animal fat.The vegetable oil is selected from big
Soya-bean oil, peanut oil, castor oil, rapeseed oil, corn oil, olive oil, palm oil, coconut oil, tung oil, linseed oil, sesame oil, cottonseed
One or more of one group of substances of compositions such as oil, sunflower oil and rice bran oil, animal fat are selected from butter, lard, sheep oil
One or more of with one group of substance of compositions such as fish oil.The poor ignition quality fuel is catalytic diesel oil and/or coker gas oil etc..
Arene content in poor ignition quality fuel is generally 70 w% or more, preferably 80w% or more, and Cetane number is generally 30 hereinafter, being
The unmanageable inferior raw material of commonsense method, common hydrofining technology or hydrogenation modifying process are difficult to be processed as qualification
Diesel product or diesel oil blending component.
In the method for the present invention, the hydrogenation metal component of the Hydrobon catalyst and hydrocracking catalyst is using
It is sulphided state under state.Hydrogenation metal component is generally one or more of W, Mo, Ni and Co.In terms of oxide weight
The content of hydrogenation metal component is generally 15wt%~45wt% in Hydrobon catalyst and hydrocracking catalyst.Catalyst exists
Vulcanized before use and convert hydrogenation metal component to sulphided state, vulcanization process is well known to those skilled in the art.
In the method for the present invention, the Hydrobon catalyst is generally using aluminium oxide as carrier, or with the oxygen containing auxiliary agent
Change aluminium is carrier, and auxiliary agent is generally one or more of silicon, phosphorus, boron, fluorine, titanium, zirconium etc., and auxiliary agent can be in carrier preparation process
Middle introducing can also introduce in hydrogenation metal component loading process.Loaded in vegetable and animals oils hydrofining reactor plus hydrogen
Catalyst for refining, main function are unsaturated fatty acid plus hydrogen saturations in vegetable and animals oils, hydrogenation deoxidation plus hydrogen decarboxylation, add
Hydrogen decarboxylation reaction etc..Hydrobon catalyst can select suitable commercial catalyst, can also commonly be known according to this field
Knowledge prepares suitable catalyst.
The Hydrobon catalyst loaded in poor ignition quality fuel hydrofining reactor, main function add poor ignition quality fuel
The reactions such as hydrogen desulfurization, hydrodenitrogeneration.Hydrobon catalyst can be conventional for handling diesel oil distillate or heavy oil fraction
Hydrobon catalyst can such as select suitable commercial catalyst, can also be prepared according to this field general knowledge.
In the method for the present invention, molecular sieve and/or amorphous silica-alumina are contained in the carrier of the hydrocracking catalyst, point
Son sieve is generally one or both of Y molecular sieves, beta-molecular sieve, general in hydrocracking catalyst to contain aluminium oxide etc. simultaneously
Inorganic refractory oxide.
In the hydrocracking catalyst I weight content of beta-molecular sieve be 3~50 wt%, preferably 10~25 wt%,
The acid amount of beta-molecular sieve is generally 0.1~0.4mmol/g.In the hydrocracking catalyst II containing Y molecular sieve 3~
The lattice constant of 50wt%, preferably 15~25wt%, Y molecular sieve are generally 2.425~2.435nm, the SiO of Y molecular sieve2/
Al2O3Molar ratio is general 5.0~50.0, and relative crystallinity is generally 80%~130%.Hydrocracking catalyst I and plus hydrogen split
Suitable commercial catalyst can be selected as needed by changing catalyst II, can also be prepared according to this field general knowledge.
In the method for the present invention, the volume ratio of hydrocracking catalyst I and hydrocracking catalyst II is generally 1:5~5:
1, preferably 1:3~3:1.
In the method for the present invention, the operating condition of hydrogenation reaction is generally：Reaction pressure 3.0MPa~20.0MPa, hydrogen oil body
Product is than being 200:1~3000:1, volume space velocity is 0.1h when the liquid of feedstock oil-1~6.0h-1, 180 DEG C of average reaction temperature~
465℃；Preferred operating condition is reaction pressure 4.0MPa~18.0MPa, hydrogen to oil volume ratio 300:1~2500:1.
Hydrocracking catalyst I containing beta-molecular sieve should be reacted under conditions of relative low temperature, large volume air speed, be subtracted
Few raw material hydro carbons avoids the excessive second pyrolysis of vegetable and animals oils, to ensure animals and plants in the time of contact of catalyst active center
Either shallow cracking only occurs for oil, while depth isomerization reaction occurs.The condition of hydroisomerizing is preferably, and volume space velocity is when liquid
2.0h-1~4.0h-1, average reaction temperature is 340 DEG C~385 DEG C.
The effect of hydrocracking catalyst II containing Y molecular sieve is so that most of aromatic hydrocarbons is converted into mononuclear aromatics and be distributed to
In gasoline fraction, and retain simultaneously a certain amount of（Generally ≮ 1.0wt%）Polycyclic aromatic hydrocarbon in diesel oil distillate.Inventor is grinding
Study carefully middle discovery, when polycyclic aromatic hydrocarbon content is more than 1.0% in diesel oil distillate, the abrasion resistance enhancing of diesel oil.The big bavin inferior of molecular weight
Oily raw material is on hydrocracking catalyst containing Y molecular sieve II, at a relatively high temperature（The balance controlled area of aromatic hydrogenation reaction）
It is preferential that cracking reaction occurs, so that most of aromatic hydrocarbons orientation is transformed into gasoline fraction.Laboratory and Commercial application show when
When the poor ignition quality fuel of arene content > 70wt% is more than 210 DEG C of yield > 50wt%, polycyclic aromatic hydrocarbon content can in diesel oil distillate product
To be more than 1.0wt%.To make up the deficiency of vegetable and animals oils hydrogenated diesel oil product greasy property difference, it is contemplated that vegetable and animals oils are hydrogenated
A small amount of either shallow cracking can occur for Cracking catalyst I and hydrocracking catalyst II, generate the fraction of 210 DEG C of a small amount of <, this
The reactive moieties of invention control hydrocracking catalyst containing Y molecular sieve II, vegetable and animals oils are more than with catalytic diesel oil miscella inferior
210 DEG C of yield ≮ 60wt%, preferably 65~75 wt%.Volume space velocity is 0.8h when preferred raw material fluid-1~1.5h-1,
Preferred 390 DEG C~435 DEG C of average reaction temperature.
The processing capacity of vegetable and animals oils and poor ignition quality fuel can arbitrarily determine according to actual needs in principle, and preferably 1:3
~3:1.
Compared with prior art, method for hydrogen cracking of the invention has the following advantages：
1, the present invention has fully considered the reapective features of vegetable and animals oils hydro-upgrading and poor ignition quality fuel hydroconversion process, closes
Reason is effectively combined two kinds of techniques：After the hydrogenated pretreatment of vegetable and animals oils, into hydrocracking reactor, split with hydrogen is added
Change the haptoreaction under relative low temperature, large volume space velocities of catalyst I, while reducing condensation point improves product quality, generates
Reaction heat generates oil and is mixed again with poor ignition quality fuel hydrofinishing generation oil, and with II haptoreaction of hydrocracking catalyst, science has
The reaction heat that vegetable and animals oils hydro-upgrading and poor ignition quality fuel hydrofinishing is utilized of effect.
2, the beta molecule sieve-type hydrocracking catalyst of hydrocracking reactor top filling, due to ten binary of beta-molecular sieve
The straight pore passage structure of ring is conducive to shape-selective isomery and the cracking of alkane, be also beneficial to reaction generate small molecule hydro carbons quickly from
It opens, while reducing vegetable and animals oils condensation point, avoids unnecessary second pyrolysis to greatest extent, reduce dry gas yield；
The Y molecular sieve type hydrocracking catalyst of reactor lower part filling contributes to polycyclic ring since Y molecular sieve is supercage structure
The selective opening of shape hydrocarbon and aromatic hydrocarbons cracks, and by the suitable acidity of control, as far as possible retains mononuclear aromatics to gasoline component,
The method of the present invention can produce high octane gasoline products and high cetane number, ultra-low-sulphur diesel product simultaneously.
3, in hydrocracking reactor, be hydrocracked by the either shallow of top vegetable and animals oils/isomery after, atmosphere is reacted in lower part
The hydrogen partial pressure enclosed reduces, and is conducive to inhibit aromatic hydrogenation in poor ignition quality fuel to be saturated, to make more aromatic hydrocarbons remain into gasoline production
In product.
4, the diesel oil that the present invention solves the generation of vegetable and animals oils hydro-upgrading wears no resistance and poor ignition quality fuel hydro-conversion
The exceeded problem low with Cetane number of high-knock rating gasoline by-product diesel oil sulfur content is produced, in production high cetane number, super-low sulfur
While diesel oil, arene content in diesel product is suitably increased, to improve the greasy property of diesel product.
5, two kinds of technology depth couplings share a hydrocracking reactor, a set of separation, fractionation and recycle hydrogen
System, technical process is simple, and equipment investment and operating cost are low, and operation is flexible, good economy performance.
Description of the drawings
Fig. 1 is a kind of principle process flow diagram of the method for the present invention.
Specific implementation mode
The method of the present invention is described in detail below in conjunction with the accompanying drawings.
As shown in Figure 1, a kind of technological process for the method for hydrogen cracking producing premium and diesel oil of the present invention is as follows：It is dynamic
Vegetable oil 1 is mixed into vegetable and animals oils hydrofining reactor 2 with hydrogen 12, carries out adding hydrogen saturation, adding for unsaturated fatty acid
Hydrogen deoxidation plus the reactions such as hydrogen decarboxylation plus hydrogen dehydroxylation, generate oil 5 after dehydration, anti-into being hydrocracked together with hydrogen 12
Device 6 is answered, carrying out modification under conditions of relative low temperature, large volume air speed with hydrocracking catalyst I 7 reacts；Poor ignition quality fuel 3 with
After hydrogen mixing, into poor ignition quality fuel hydrofining reactor 4, the reactions such as hydrodesulfurization, hydrodenitrogeneration, reaction effluent occurs
8 directly enter reactor from the middle and upper part of hydrocracking reactor 6 without isolation, mixed with vegetable and animals oils hydroisomerizing product
It closes, is obtained by piece-rate system 11 with II 9 haptoreaction of hydrocracking catalyst, reaction effluent 10 after obtaining certain heat
Gas it is purified after recycled with new hydrogen, the fluid product 13 of acquisition enters fractionating system 14, obtains gas 15, gasoline
16, diesel oil 17 and a small amount of hydrogenation tail oil 18.
A kind of method for hydrogen cracking producing premium and diesel oil of the present invention is made followed by specific embodiment
Further instruction.
Embodiment 1-2 is the embodiment of the method for the present invention, the weight ratio of vegetable and animals oils and catalytic diesel oil inferior in embodiment
Example is 1:1.Reference Example 1 is the implementation result of catalytic diesel oil hydro-conversion technology, and Reference Example 2 is vegetable and animals oils hydro-upgrading technology
Implementation result.Table 1 is feedstock property, and the property of hydrocracking catalyst used is listed in table 2, operation is classified as in table 3
Condition and result.
1 raw material oil nature of table.
2 hydrocracking catalyst property of table.
3 operating condition of table and result.
* the lubricity in derv fuel quality standard is generally characterized with 60 DEG C of grinding defect diameter of correction, it is desirable that it is not more than
460μm。
The present invention has fully considered the reapective features of vegetable and animals oils hydro-upgrading and poor ignition quality fuel hydroconversion process, rationally
Two kinds of techniques are effectively combined.Embodiment 1 is 385 DEG C in the reaction temperature of catalyst I, and the reaction temperature of catalyst II is
Under conditions of 400 DEG C, while obtaining the gasoline products and Cetane number is 59, sulfur content is 8 μ gg that octane number is 93.8-1's
Diesel product；Embodiment 2 is 365 DEG C in the reaction temperature of catalyst I, under conditions of the reaction temperature of catalyst II is 425 DEG C,
Obtain the gasoline products and Cetane number is 63, sulfur content is 7 μ gg that octane number is 94.4 simultaneously-1Diesel product, effect is aobvious
It writes, realizes the purpose of this technology invention.
In addition, the correction grinding defect diameter of the diesel product of embodiment and comparative example statistics indicate that, the present invention solves dynamic plant
The problem of diesel oil that object oil hydro-upgrading generates wears no resistance.
Claims (13)
1. it is a kind of produce high-knock rating gasoline and fine-quality diesel oil be hydrocracked combined method, including the following contents：
（1）Vegetable and animals oils and hydrogen are mixed into vegetable and animals oils hydrofining reactor, and poor ignition quality fuel is mixed into bad with hydrogen
Matter diesel oil hydrofining reactor, contacts with Hydrobon catalyst, carries out hydrofining reaction respectively；
（2）Vegetable and animals oils hydrofinishing effluent is after dehydration, together with hydrogen, enters from reactor head and is hydrocracked instead
Device is answered, is contacted first with the hydrocracking catalyst I containing beta-molecular sieve, under the conditions of hydroisomerizing, it is anti-to carry out isomerization-visbreaking
It answers；
（3）Step（2）Gained reaction product, then the poor ignition quality fuel hydrofinishing product introduced with reactor middle and upper part mix
Afterwards, it is contacted with the hydrocracking catalyst II containing Y molecular sieve, under hydrocracking condition, carries out hydroconversion reactions；
（4）Step（3）Obtained reaction effluent carries out gas-liquid separation, obtains hydrogen-rich gas and fluid product；Fluid product into
Row fractionation obtains gas, gasoline, diesel oil and tail oil fraction；
Wherein, the arene content of the poor ignition quality fuel is 80w% or more.
2. according to the method for claim 1, which is characterized in that the vegetable and animals oils include vegetable oil and/or animal oil
Fat.
3. according to the method for claim 2, which is characterized in that the vegetable oil is selected from soybean oil, peanut oil, castor-oil plant
Oil, rapeseed oil, corn oil, olive oil, palm oil, coconut oil, tung oil, linseed oil, sesame oil, cottonseed oil, sunflower oil and rice
One group of substance that oil extracted from rice husks is constituted, the animal fat includes one or more of butter, lard, sheep oil and fish oil.
4. according to the method for claim 1, which is characterized in that arene content in the poor ignition quality fuel be 80w% with
On.
5. according to the method described in claim 1 or 4, which is characterized in that the poor ignition quality fuel is catalytic diesel oil and/or coking
Diesel oil.
6. according to the method for claim 1, which is characterized in that the weight of beta-molecular sieve in the hydrocracking catalyst I
Content is 3~50 wt%, and the acid amount of beta-molecular sieve is 0.1~0.4 mmol/g.
7. according to the method described in claim 1 or 6, which is characterized in that contain Y molecules in the hydrocracking catalyst II
3~50 wt% are sieved, the lattice constant of Y molecular sieve is 2.425~2.435nm, the SiO of Y molecular sieve2/Al2O3Molar ratio be 5.0~
50.0, relative crystallinity is 80%~130%.
8. according to the method for claim 1, which is characterized in that the hydrocracking catalyst I and hydrocracking catalyst
The volume ratio of agent II is 1:5~5:1.
9. according to the method for claim 1, which is characterized in that the hydroisomerizing and the operating condition being hydrocracked
For：Reaction pressure 3.0MPa~20.0MPa, hydrogen to oil volume ratio 200:1~3000:1, volume space velocity is when the liquid of feedstock oil
0.1h-1~6.0h-1, 180 DEG C~465 DEG C of average reaction temperature.
10. according to the method for claim 9, which is characterized in that the condition of the hydroisomerizing is, volume space velocity when liquid
For 2.0h-1~4.0h-1, average reaction temperature is 340 DEG C~385 DEG C.
11. according to the method described in claim 9 or 10, which is characterized in that the process conditions being hydrocracked are, when liquid
Volume space velocity is 0.8h-1~1.5h-1, 390 DEG C~435 DEG C of average reaction temperature.
12. according to the method for claim 11, which is characterized in that step（3）Middle control vegetable and animals oils are mixed with poor ignition quality fuel
Close yield ≮ 60wt% that oil is more than 210 DEG C.
13. according to the method for claim 1, which is characterized in that the weight ratio of the vegetable and animals oils and poor ignition quality fuel is
1:3~3:1.
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Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101724423A (en) * | 2008-10-28 | 2010-06-09 | 中国石油化工股份有限公司 | Method for processing ethylene tar |
| CN103374405A (en) * | 2012-04-29 | 2013-10-30 | 中国石油化工股份有限公司 | Hydrogenation combination method for producing high-quality low-condensation-point diesel oil with biolipid |
| CN103374403A (en) * | 2012-04-29 | 2013-10-30 | 中国石油化工股份有限公司 | Hydrogenation combination method for producing low-condensation-point diesel oil |
| CN103374399A (en) * | 2012-04-29 | 2013-10-30 | 中国石油化工股份有限公司 | Hydrogenation combination method for producing high-quality low-condensation-point diesel oil |
| CN103374404A (en) * | 2012-04-29 | 2013-10-30 | 中国石油化工股份有限公司 | Hydrogenation combination method for producing high-quality diesel oil |
| CN103374396A (en) * | 2012-04-29 | 2013-10-30 | 中国石油化工股份有限公司 | Hydrogenation combination method for producing low-condensation-point diesel oil |
| CN103374397A (en) * | 2012-04-29 | 2013-10-30 | 中国石油化工股份有限公司 | Hydrogenation combination method for producing low-condensation-point diesel oil |
| CN103773461A (en) * | 2012-10-24 | 2014-05-07 | 中国石油化工股份有限公司 | Hydrocracking method used for producing high-quality jet fuel |
| CN103773456A (en) * | 2012-10-24 | 2014-05-07 | 中国石油化工股份有限公司 | Animal and vegetable oil-catalytic diesel oil combined hydrogenation method |
| CN104611046A (en) * | 2013-11-05 | 2015-05-13 | 中国石油化工股份有限公司 | Low energy-consumption two-stage hydrocracking method |
-
2015
- 2015-11-19 CN CN201510797913.5A patent/CN106479566B/en active Active
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101724423A (en) * | 2008-10-28 | 2010-06-09 | 中国石油化工股份有限公司 | Method for processing ethylene tar |
| CN103374405A (en) * | 2012-04-29 | 2013-10-30 | 中国石油化工股份有限公司 | Hydrogenation combination method for producing high-quality low-condensation-point diesel oil with biolipid |
| CN103374403A (en) * | 2012-04-29 | 2013-10-30 | 中国石油化工股份有限公司 | Hydrogenation combination method for producing low-condensation-point diesel oil |
| CN103374399A (en) * | 2012-04-29 | 2013-10-30 | 中国石油化工股份有限公司 | Hydrogenation combination method for producing high-quality low-condensation-point diesel oil |
| CN103374404A (en) * | 2012-04-29 | 2013-10-30 | 中国石油化工股份有限公司 | Hydrogenation combination method for producing high-quality diesel oil |
| CN103374396A (en) * | 2012-04-29 | 2013-10-30 | 中国石油化工股份有限公司 | Hydrogenation combination method for producing low-condensation-point diesel oil |
| CN103374397A (en) * | 2012-04-29 | 2013-10-30 | 中国石油化工股份有限公司 | Hydrogenation combination method for producing low-condensation-point diesel oil |
| CN103773461A (en) * | 2012-10-24 | 2014-05-07 | 中国石油化工股份有限公司 | Hydrocracking method used for producing high-quality jet fuel |
| CN103773456A (en) * | 2012-10-24 | 2014-05-07 | 中国石油化工股份有限公司 | Animal and vegetable oil-catalytic diesel oil combined hydrogenation method |
| CN104611046A (en) * | 2013-11-05 | 2015-05-13 | 中国石油化工股份有限公司 | Low energy-consumption two-stage hydrocracking method |
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