CN106675644B - A kind of production method of low-sulfur, low-coagulation diesel oil - Google Patents
A kind of production method of low-sulfur, low-coagulation diesel oil Download PDFInfo
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Abstract
The invention discloses the production method of a kind of low-sulfur, low-coagulation diesel oil, including herein below：（1）Poor ignition quality fuel raw material is sufficiently mixed in a mixer with powdered Mo Co types Hydrobon catalyst, obtains the mixed feeding of catalyst and feedstock oil；（2）Mixed feeding enters fluidized bed reactor with hydrogen from the reactor bottom equipped with Hydrodewaxing catalyst and Mo Ni type Hydrobon catalysts, carries out hydrogenation reaction；（3）Logistics, into reactor is stablized, carries out supplement hydrofinishing through being discharged at the top of fluidized bed reactor after reaction comprising powdered Mo Co Hydrobon catalysts；（4）Step（3）For the material of acquisition through separation of solid and liquid, liquid phase enters fractionating system, obtains low-sulfur, low-coagulation diesel oil product.The inventive method carries out the temperature drop of hydro dewaxing process with the temperature rise in hydrogenation process reasonably to combine utilization, and the hot(test)-spot temperature of device is reduced while low condensation point, ultra-low-sulphur diesel is produced, extends service cycle, saves operating cost.
Description
Technical field
It is especially a kind of to pass through fluidized bed reactor next life the present invention relates to the production method of a kind of low-sulfur, low-coagulation diesel oil
Produce high-quality low-sulfur, the production method of low-coagulation diesel oil.
Background technology
Fuel of the diesel oil as compression ignition engine, risen during the production and living of modernization as non-renewable resources
Irreplaceable effect, the delivery vehicles such as automobile, tank, aircraft, tractor, rolling stock or other can be used as
The fuel of machinery, it is also possible to generate electricity, warm oneself.According to it using industry and the difference of environment, user is for diesel product
Quality requirement also have very big difference, for extremely frigid zones or winter life people for, low freezing point diesel fuel
Demand remains high always, and traditional shape slective cracking technique can process the heavy diesel fuel cut of the content of wax, pour point depression amplitude up to 20~
50 DEG C, while obtaining low freezing point diesel fuel, diesel oil distillate scope can be also widened, improves yield, be to solve low freezing point diesel fuel production
The highly useful and advanced technology of problem.
The situation in China is also similar, particularly in recent years, right with the national economic development and the continuous improvement of environmental consciousness
In the requirement more and more higher of diesel quality, the popularity rate of diesel refining rises year by year, in addition in northern cold area, except normal to diesel oil
Outside the requirement of the refined property of rule, condensation point becomes one of essential requirement index, therefore can improve the production of low-coagulation diesel oil
Amount and quality, meet that the market demand has turned into Han Qu oil refining enterprise major issue of interest.And shape slective cracking and combinations thereof work
Skill can be used for producing low-sulfur low-coagulation diesel oil, be advantageous to improve oil refining enterprise as one of Main Means for reducing condensation point of diesel oil
Economic benefit.
Diesel oil shape slective cracking technology is also known as hydro dewaxing, refers in the presence of hydrogen, and the diesel raw material of the content of wax is led to
The bifunctional catalyst surface containing active metal and molecular sieve is crossed, so as to reduce wax molecule content therein.Its principle that dewaxes
It is under certain operating conditions, to mix raw material and hydrogen and contacted with Hydrodewaxing catalyst, alkane in raw material, with short
It is cracked into small molecule the aromatic hydrocarbons of side chain alkane, the cycloalkane of belt length side chain and belt length side chain grade high condensation point compositional selecting, and
Other components do not change substantially, are finally reached the purpose for the condensation point for reducing oil product.Due to its have course of reaction hydrogen consumption compared with
It is low, adaptability to raw material is strong, energy consumption is relatively low, technological process is simple, can form and process integration or independently makes with other hydrogenation processes
With many advantages, such as, therefore be widely used.The many oil refining enterprise of northern China Han Qu employ this technology at present
Produce low-coagulation diesel oil.
CN1257107A describes a kind of method that high-grade low-freezing diesel oil is produced by distillate.This method uses hydrofinishing
With hydro dewaxing one-stage serial flow, including two beds of Hydrobon catalyst and Hydrodewaxing catalyst,
Hydro dewaxing uses Ni/ZSM-5 catalyst.This method is larger in the temperature drop of Hydrodewaxing catalyst bed, the receipts of diesel oil distillate
The raising of rate and depression effeCt is reduced the service life of Hydrodewaxing catalyst by a definite limitation.
CN102051232A describes a kind of method of diesel oil hydrogenation pour point depression, this method by adjust the property of catalyst from
And there is the characteristics of diesel oil depression effeCt is good, diesel oil distillate high income, but due to still using hydrofinishing and hydro dewaxing to connect
Group technology, between depression effeCt and diesel oil distillate yield contradiction still exist.
CN102453531A describes a kind of method of diesel hydro-pour-reducing, although improving the flat of Hydrodewaxing catalyst
Equal reaction temperature, using the temperature rise of refining agent, the utilization rate of pour point depression catalyst is increased, still
The reaction temperature of each bed outlet is still of a relatively high, and the cycle receives certain limitation.
CN01134271.4 discloses a kind of combined hydrogenation method for producing high cetane number, low-coagulation diesel oil.This method is
Feedstock oil, hydrogen are first contacted with catalyst for hydro-upgrading or hydrocracking catalyst, reaction effluent without isolation then with
Hydrodewaxing catalyst contacts, and reaction effluent enters high-pressure separator through cooling, and the product liquid isolated enters fractionation train
System, the gas circulation rich in hydrogen return reactor.This method can improve the Cetane number and drop of diesel oil simultaneously in same covering device
The condensation point of low diesel oil, the Cetane number of diesel product improve more than 6 units compared with feedstock oil.
CN99113293.9 discloses a kind of method that high-quality low-coagulation diesel oil with high hexadecane value is produced by distillate.This method
Hydro dewaxing is directly connected with hydrofinishing, hydro-upgrading, realizes hydrofinishing-hydro-upgrading-hydro dewaxing-section series connection
Flow, using the strong Hydrobon catalyst of anti-coking performance and with relatively strong anti-ammonia, capacity antacid hydro-upgrading and
Hydrodewaxing catalyst so that the technique have it is refined/depression effeCt is good, diesel yield is high, adaptability to raw material is strong, diesel oil
The characteristics of Cetane number is high, technological process is simple and products scheme is flexible.
The content of the invention
The problem of existing for prior art, the present invention provide a kind of low-sulfur, the production method of low-coagulation diesel oil.Present invention side
Method makes full use of the characteristics of fluidized bed reactor back-mixing, and the temperature rise in the temperature drop and hydrogenation process of hydro dewaxing process is closed
The combination of reason is utilized, and the hot(test)-spot temperature of device is reduced while low condensation point, ultra-low-sulphur diesel is produced, extends service cycle；
In addition the combustion gas loss of the consumption or heating furnace of cold hydrogen is reduced, saves operating cost.
A kind of low-sulfur provided by the invention, the production method of low-coagulation diesel oil, including herein below：
（1）Poor ignition quality fuel raw material is sufficiently mixed in a mixer with powdered Mo-Co types Hydrobon catalyst, is urged
The mixed feeding of agent and feedstock oil；
（2）Mixed feeding and hydrogen are from the reactor equipped with Hydrodewaxing catalyst and Mo-Ni type Hydrobon catalysts
Bottom enters fluidized bed reactor, carries out hydrogenation reaction；Wherein described hydrogenation reaction includes hydro dewaxing and reacts and be hydrogenated with essence
System reaction；
（3）Logistics is entered through being discharged at the top of fluidized bed reactor after reaction comprising powdered Mo-Co Hydrobon catalysts
Enter stable reactor, carry out supplement hydrofinishing；
（4）Step（3）For the material of acquisition through separation of solid and liquid, liquid phase enters fractionating system, obtains high-quality low-sulfur, low-coagulation diesel oil
Product.
In the inventive method, described poor ignition quality fuel raw material is high freezing point diesel fuel for conventional pour point depression raw material inferior, condensation point
Typically all more than 0 DEG C, preferably condensation point is more than 5 DEG C.Can be processing naphthene base crude, intermediate base crude or paraffinic base crude oil
Obtained various straight-run diesel oils, secondary processing diesel oil（Coker gas oil, catalytic diesel oil etc.）In one or several kinds, preferably process
The said components that paraffinic base crude oil obtains.The diesel raw material does generally 350~440 DEG C, preferably 370~400 DEG C.
In production method of the present invention, described powdered Mo-Co types Hydrobon catalyst can be that this area generally makes
Powdered Hydrobon catalyst, its granularity are generally 50~2000 μm, preferably 500~1500 μm, described powder
Shape catalyst can flow with oil product.Typically using group vib and/or group VIII metal as active component, with aluminum oxide or siliceous
Aluminum oxide is carrier, and vib metals Mo, group VIII metal is Co.On the basis of the weight of catalyst, vib gold
Category content is calculated as 8wt%~28wt% with oxide, and group VIII tenor is calculated as the wt% of 2wt%~15 with oxide, and surplus is
Aluminum oxide or silicon-containing alumina carrier.
Production method step of the present invention（1）Mixed feeding in, powdered Mo-Co types Hydrobon catalyst addition with
Metal is calculated as 20~200 μ g/g.
In production method of the present invention, described blender can use multistage shear pump, can also use static mixer,
The mixing arrangement commonly used in the art such as ultrasonic oscillator.
In the inventive method, described Hydrodewaxing catalyst is the conventional pour point depression catalyst in this area.Described urges
Agent includes silica-alumina supports and hydrogenation active metals containing shape slective cracking molecular sieve.Described shape slective cracking molecular sieve is Hydrogen
Molecular sieve, the molecular sieve can be selected from Hydrogen ZSM-5, ZSM-11, ZSM-12, ZSM-22, ZSM-23, ZSM-35 and ZSM-38
One or more in molecular sieve, preferably ZSM-5 molecular sieve；The silica alumina ratio of the shape slective cracking molecular sieve is generally 10~
150, preferably 20~120.Hydrogenation active metals described in Hydrodewaxing catalyst can be in the periodic table of elements
VIII and/or group vi metallic element, wherein group VIII active metal can be Ni and/or Co, group vi active metal
It is W and/or Mo.On the basis of the weight of catalyst, hydrogenation active metal component contains using the content that oxide is counted as 10%~30%
The silica-alumina supports content for having shape slective cracking molecular sieve is 70%~90%, and wherein shape slective cracking molecular sieve content in silica-alumina supports is
10%~40%, remaining is aluminum oxide.Described Hydrodewaxing catalyst can select existing various commercial catalysts, such as comfort
Along Petroleum Chemical Engineering Institute（FRIPP）The Hydrodewaxing catalysts such as FDW-1, FDW-3 of development；It can also press as needed
It is prepared by the general knowledge of this area, for example, be referred to CN1952074A, CN1352231A, CN101143333A,
Content disclosed in CN102451748A prepares satisfactory Hydrodewaxing catalyst.
Mo-Ni types Hydrobon catalyst described in the inventive method is the conventional catalyst in this area, is boiled to coordinate
The fluid form of bed is risen, catalyst appearance is spherical, and its catalyst composition and property are developed with Fushun Petrochemical Research Institute and opened
The FHUDS-6 of hair is consistent.
In production method of the present invention, in described fluidized bed reactor, powdered Mo-Co types Hydrobon catalyst is with facing
The volume ratio of hydrogen pour point depression catalyst and Mo-Ni type Hydrobon catalysts is 1：10~10：1, preferably 1：5~5：1；Wherein face hydrogen
The volume ratio of pour point depression catalyst and Mo-Ni type Hydrobon catalysts is 1：5~5：1, preferably 1：3~3：1.
In production method of the present invention, the hydrogenation conditions in described fluidized bed reactor are：Reaction pressure 6.0 ~
30.0MPa, reaction temperature are 270 ~ 500 DEG C, and air speed is 0.1 ~ 5.0h-1, hydrogen to oil volume ratio 400：1~2000:1.
In production method of the present invention, in boiling bed hydrogenation reactor, diesel raw material, hydrogen and powdered Mo-Co types add
Hydrogen catalyst for refining, Mo-Ni types Hydrobon catalyst and Hydrodewaxing catalyst contact, carry out hydrodesulfurization, denitrogenation, aromatic hydrocarbons
Saturation and pour point depression reaction etc..
In production method of the present invention, described stable reactor is used for the post-refining of upper reaction member generation oil, by
It is selectively strong to linear paraffin hydrocracking in the characteristics of Hydrodewaxing catalyst, and the hydrocracking processes of linear paraffin are abided by
Carbonium ion reaction mechanism is followed, during the course of the reaction the unsaturated hydro carbons such as generating portion alkene, reduce the stability of oil product.This
Invention makes full use of the hydrogen partial dissolved in the reaction heat and generation oil of last action unit, is mended in reactor is stablized
Hydrofinishing is filled, while unsaturated hydro carbons is removed, further reduces the sulfur content of oil product.
In production method of the present invention, described stable reactor exit sets separating and filtering equipment, adds for powdered
The separation of solid and liquid of hydrogen catalyst for refining and generation oil product, the solid phase powder shape Hydrobon catalyst for separating acquisition recycle.
In production method of the present invention, described fractionating system is conventional oil product separation fractionation well known to those skilled in the art
System, for obtaining the purpose product of appropriate cut.
Compared with prior art, the inventive method has advantages below：
1st, the present invention makes full use of back-mixing " boiling " feature of fluidized bed reactor and the heat release effect of hydrofining reaction
The endothermic effect that should be reacted with hydro dewaxing, realizes the comprehensive utilization of course of reaction heat, at utmost reduces temperature rise and temperature
Effect is dropped so that isothermal operation is realized in hydrocracking pretreatment reaction, so as to improve hydro-upgrading depression effeCt, can both ensure bavin
The quality and yield of oil, the depression effeCt achieved again.
2nd, the present invention makes full use of the high hydrodenitrogenationactivity activity of Mo-Ni type Hydrobon catalysts, Mo-Co type hydrofinishings to urge
The strong hydrogen sulfide tolerance of agent, the coupling advantage of catalyst can be given full play to, effectively reduce nitride to transalkylation desulfurization
The inhibitory action of reaction, realize 4,6-DMDBT efficient removal.
3rd, temperature and the hydrogen partial that wherein dissolves of the present invention using fluidized bed reactor reaction effluent, it is and powdered
Hydrobon catalyst carries out supplement hydrofinishing in reactor is stablized, and reduces unsaturated hydrocarbons content and sulphur in generation oil product
Content, improves the stability and quality of diesel product, while improves the utilization rate of hydrogen resources.
4th, the present invention has by reactant motion violent in reactor from part by the high temperature dot of device and low temperature point
Effect eliminates, and reduces the hot(test)-spot temperature of device, extends the service life of catalyst.
5th, powdered Hydrobon catalyst travels up to fluidized bed reactor without catalyst with generation oil in the present invention
Fluid zone, the polycondensation coking reaction of area's liquid under the high temperature conditions in the presence of without Hydrodewaxing catalyst can be prevented
Occur.
Brief description of the drawings
Fig. 1 is a kind of low-sulfur of the present invention, the schematic flow sheet of the production method of low-coagulation diesel oil.
Embodiment
A kind of low-sulfur to the present invention, the production method of low-coagulation diesel oil are described in detail below in conjunction with the accompanying drawings.
As shown in figure 1, the low-sulfur of the present invention, low-coagulation diesel oil production method flow are as follows：By poor ignition quality fuel 1 with it is powdered
Mo-Co type Hydrobon catalysts（Including supplementing new agent 2 and recycling catalyst 12）It is sufficiently mixed, obtains equal in blender 3
Even charging 4, enter fluidized bed reactor through delivery pump, high pressure hydrogen 8 is in a manner of upper feeding from the bottom of fluidized bed reactor 5
Catalyst is set to keep boiling into the fluidized bed reactor equipped with Hydrodewaxing catalyst 6 and Mo-Ni types Hydrobon catalyst 7
Shape, under suitable reaction condition, add with Hydrodewaxing catalyst and powdered Mo-Co types Hydrobon catalyst, Mo-Ni types
Hydrogen catalyst for refining contacts, and carries out catalytic hydrogenation reaction, and reacted logistics 9 is discharged into stable reaction at the top of reactor
Device 10, supplement hydrofinishing is carried out using the hydrogen partial and logistics self heat that wherein dissolve, will be generated by separator 11
Oil 12 separates with powdered Hydrobon catalyst 13, and powdered Hydrobon catalyst recycles, and generates oil and enters separation
Fractionating system 14, fractionate out gas, light distillate and high-grade low-freezing diesel product 15.
Low-sulfur of the invention, low-coagulation diesel oil production method are further described followed by specific embodiment.
Embodiment 1~5
The present embodiment is to be hydrogenated with using Hydrodewaxing catalyst, Mo-Ni types Hydrobon catalyst and powdered Mo-Co types
The boiling bed hydrogenation experiment of catalyst for refining.Concrete operations flow is shown in accompanying drawing 1.Powdered Mo-Co hydrogenation essence in embodiment 1~2
Catalyst processed is 1 with the volume ratio of Hydrodewaxing catalyst and Mo-Ni type Hydrobon catalysts:8, Hydrodewaxing catalyst and
The volume ratio of Mo-Ni type Hydrobon catalysts is 4:1；In embodiment 3~4 powdered Mo-Co types Hydrobon catalyst with
The volume ratio of Hydrodewaxing catalyst and Mo-Ni type Hydrobon catalysts is 9:1.Wherein Hydrodewaxing catalyst and Mo-Ni
The volume ratio of type Hydrobon catalyst is 1:5.Powdered Mo-Co types Hydrobon catalyst and hydro dewaxing in embodiment 5
The volume ratio of catalyst and Mo-Ni type Hydrobon catalysts is 1:1.Wherein Hydrodewaxing catalyst and Mo-Ni types hydrogenation essence
The volume ratio of catalyst processed is 1:2.Poor ignition quality fuel and powdered Mo-Co types Hydrobon catalyst is fully mixed in a mixer
Close, obtain uniform charging, enter fluidized bed reactor through delivery pump, high pressure hydrogen is in a manner of upper feeding from ebullating bed reactor
Device bottom, which enters the fluidized bed reactor equipped with Hydrodewaxing catalyst and Mo-Ni type Hydrobon catalysts, keeps catalyst
Boiling-like, under suitable reaction condition, while and/or priority and Hydrodewaxing catalyst, Mo-Ni type Hydrobon catalysts
Contacted with powdered Mo-Co types Hydrobon catalyst, carry out catalytic hydrogenation reaction, reacted logistics is from the top of reactor
Be discharged into stable reactor, supplement hydrofinishing carried out using the hydrogen partial of dissolving and the self heat of material, by point
From device will generate it is oily separated with powdered Mo-Co types Hydrobon catalyst, the circulation of powdered Mo-Co types Hydrobon catalyst
Use, generate oil and enter separation fractionating system, fractionate out gas, light distillate and high-grade low-freezing diesel product.Make in embodiment
Hydrodewaxing catalyst is the spheric catalyst of special preparation, the catalyst component property and Fushun petrochemical industry research
The commercial catalyst FDW-3 of institute's development and production is consistent.The Mo-Ni types Hydrobon catalyst used is that the spherical of special preparation is urged
Agent, the catalyst component property are consistent with the commercial catalyst FHUDS-6 of Fushun Petrochemical Research Institute's development and production.Make
Powdered Mo-Co types catalyst, its granularity are 1000~1200 μm, and active component is contained in catalyst（In terms of metal）Molybdenum is
20%, cobalt 8%, the commercial catalyst FHUDS-6 of the catalyst component property and Fushun Petrochemical Research Institute's development and production
Unanimously.
Raw material oil nature is shown in Table 1, and catalyst fundamental property is shown in Table 2, process condition and the results are shown in Table 3.
Comparative example 1 ~ 2
Comparative example 1 ~ 2 is conventional hydro dewaxing technological process, and reactor types are fixed bed, after feedstock oil is heated,
Hydrobon catalyst and Hydrodewaxing catalyst are passed sequentially through, the oil product of generation obtains corresponding product through separating fractionating system.
The Mo-Co types Hydrobon catalyst used is that shape size is different with embodiment 1（It is shown in Table 2）, Hydrodewaxing catalyst,
Mo-Ni types Hydrobon catalyst, feedstock oil are same as Example 1.The product property of comparative example 1 ~ 2 is shown in Table 4.Comparative example 1
Mo-Co types Hydrobon catalyst is 1 with the volume ratio of Hydrodewaxing catalyst and Mo-Ni type Hydrobon catalysts:8, face
The volume ratio of hydrogen pour point depression catalyst and Mo-Ni type Hydrobon catalysts is 4:1；The Mo-Co types hydrofinishing of comparative example 2 is catalyzed
Agent is 1 with the volume ratio of Hydrodewaxing catalyst and Mo-Ni type Hydrobon catalysts:1.Wherein Hydrodewaxing catalyst and
The volume ratio of Mo-Ni type Hydrobon catalysts is 1:2.
The feedstock oil property list of table 1.
The catalyst fundamental property of table 2
The embodiment process condition of table 3 and result.
The comparative example process condition of table 4 and result.
Embodiment is compared with comparative example, in catalyst proportion under the same conditions, product quality be improved significantly, technology
It is with the obvious advantage.
Claims (10)
1. a kind of production method of low-coagulation diesel oil, it is characterised in that including herein below：（1）Poor ignition quality fuel raw material with it is powdered
Mo-Co type Hydrobon catalysts are sufficiently mixed in a mixer, obtain the mixed feeding of catalyst and feedstock oil；（2）Mixing
Charging enters with hydrogen from the reactor bottom of mixed packing Hydrodewaxing catalyst and Mo-Ni type Hydrobon catalysts seethes with excitement
Bed reactor, carries out hydrogenation reaction；Wherein described hydrogenation reaction includes hydro dewaxing reaction and hydrofining reaction；（3）Bag
Logistics is through discharging at the top of fluidized bed reactor after reaction containing powdered Mo-Co Hydrobon catalysts, into stablizing reactor,
Carry out supplement hydrofinishing；（4）Step（3）For the material of acquisition through separation of solid and liquid, liquid phase enters fractionating system, obtains high-quality low
Sulphur, low-coagulation diesel oil product.
2. according to the production method described in claim 1, it is characterised in that：The condensation point of described poor ignition quality fuel raw material 0 DEG C with
On, in the various straight-run diesel oils that are obtained selected from processing naphthene base crude, intermediate base crude or paraffinic base crude oil, secondary processing diesel oil
One or several kinds.
3. according to the production method described in claim 1, it is characterised in that：Described powdered Mo-Co types hydrofinishing catalysis
The granularity of agent is 50~2000 μm, and on the basis of the weight of catalyst, Mo is calculated as 8wt%~28wt% with oxide, and Co is to aoxidize
Thing is calculated as 2wt%~15wt%, and surplus is aluminum oxide or silicon-containing alumina carrier.
4. according to the production method described in claim 1, it is characterised in that：Step（1）Mixed feeding in, powdered Mo-Co
Type Hydrobon catalyst addition is calculated as 20~200 μ g/g with metal.
5. according to the production method described in claim 1, it is characterised in that：Described Hydrodewaxing catalyst is included containing shape-selective
The silica-alumina supports and hydrogenation active metals of cracking molecular sieve；Described shape slective cracking molecular sieve is hydrogen type molecular sieve, the molecule
Screened from one kind or more in Hydrogen ZSM-5, ZSM-11, ZSM-12, ZSM-22, ZSM-23, ZSM-35 and ZSM-38 molecular sieve
Kind；The silica alumina ratio of the shape slective cracking molecular sieve is 10~150；Described hydrogenation active metals element is in periodic table
Group VIII and/or vib metals element, wherein group VIII active metal are Ni and/or Co, vib active metal
It is W and/or Mo；On the basis of the weight of catalyst, hydrogenation active metal component contains using the content that oxide is counted as 10%~30%
The silica-alumina supports content for having shape slective cracking molecular sieve is 70%~90%, and wherein shape slective cracking molecular sieve content in silica-alumina supports is
10%~40%, remaining is aluminum oxide.
6. according to the production method described in claim 1, it is characterised in that：Described Mo-Ni types Hydrobon catalyst is this
The conventional catalyst in field, to coordinate the fluid form of ebullated bed, catalyst appearance be it is spherical, its catalyst composition and property with
The FHUDS-6 that Fushun Petrochemical Research Institute develops is consistent.
7. according to the production method described in claim 1, it is characterised in that：In described fluidized bed reactor, powdered Mo-Co
The volume ratio of the Hydrodewaxing catalyst and Mo-Ni type Hydrobon catalysts of type Hydrobon catalyst and mixed packing is 1：
10~10：1；Wherein the volume ratio of Hydrodewaxing catalyst and Mo-Ni type Hydrobon catalysts is 1：5~5：1.
8. according to the production method described in claim 1, it is characterised in that：Hydrogenation reaction bar in described fluidized bed reactor
Part is：6.0 ~ 30.0MPa of reaction pressure, reaction temperature are 270 ~ 500 DEG C, and air speed is 0.1 ~ 5.0h-1, hydrogen to oil volume ratio 400：
1~2000：1.
9. according to the production method described in claim 1, it is characterised in that：In boiling bed hydrogenation reactor, diesel raw material, hydrogen
Gas contacts with powdered Mo-Co types Hydrobon catalyst, Mo-Ni types Hydrobon catalyst and Hydrodewaxing catalyst, enters
Row hydrodesulfurization, denitrogenation, aromatic hydrocarbons saturation and pour point depression reaction.
10. according to the production method described in claim 1, it is characterised in that：Described stable reactor exit sets separation
Filter plant, for the separation of solid and liquid of powdered Hydrobon catalyst and generation oil product, the solid phase powder shape for separating acquisition adds
Hydrogen catalyst for refining recycles.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1326495A (en) * | 1998-11-13 | 2001-12-12 | 埃克森研究工程公司 | Small catalyst particle addition to slurry reaction |
| CN102264871A (en) * | 2008-12-31 | 2011-11-30 | 埃克森美孚研究工程公司 | Integrated hydrocracking and dewaxing of hydrocarbons |
| CN104611033A (en) * | 2013-11-05 | 2015-05-13 | 中国石油化工股份有限公司 | Method for producing hydrogenated diesel oil with low freezing point |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2772170C (en) * | 2009-10-08 | 2018-03-06 | IFP Energies Nouvelles | Method for hydroconverting heavy carbonaceous loads, including a bubbling bed technology and slurry technology |
| US9650312B2 (en) * | 2013-03-14 | 2017-05-16 | Lummus Technology Inc. | Integration of residue hydrocracking and hydrotreating |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1326495A (en) * | 1998-11-13 | 2001-12-12 | 埃克森研究工程公司 | Small catalyst particle addition to slurry reaction |
| CN102264871A (en) * | 2008-12-31 | 2011-11-30 | 埃克森美孚研究工程公司 | Integrated hydrocracking and dewaxing of hydrocarbons |
| CN104611033A (en) * | 2013-11-05 | 2015-05-13 | 中国石油化工股份有限公司 | Method for producing hydrogenated diesel oil with low freezing point |
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