CN103805244B - A kind of production method of clean low-coagulation diesel oil - Google Patents
A kind of production method of clean low-coagulation diesel oil Download PDFInfo
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Abstract
The invention discloses a kind of production method of clean low-coagulation diesel oil.After diesel oil mixes with hydrogen, successively by the hydroconversion reaction zones of at least two series connection, comprise by the refining pour point depression catalyzer composite bed of Hydrodewaxing catalyst and Hydrobon catalyst mixed packing and catalyst for hydro-upgrading bed successively by each hydroconversion reaction zone, Flow of Goods and Materials direction; Last hydroconversion reaction zone gained reaction effluent is through being separated and after fractionation, obtaining clean low freezing point diesel fuel product, and on a small quantity light naphthar and liquefied gas.The temperature rise of the temperature drop of hydrodewaxing process and hydrofining and upgrading processes is reasonably combined utilization by the inventive method, improves the yield of diesel oil, reduce the hot(test)-spot temperature of device, extend running period while producing low solidifying low-sulfur diesel-oil; In addition reduce the consumption of cold hydrogen or the combustion gas loss of process furnace, joint has also economized process cost.
Description
Technical field
The present invention relates to a kind of production method of clean low-coagulation diesel oil, especially a kind of by catalyzer grating technology and compound filling technology, be used for producing the method for hydrotreating of clean low-coagulation diesel oil.
Background technology
Diesel oil is as the fuel of self-igniton engine, irreplaceable effect is played as Nonrenewable resources in modern productive life process, launch vehicle or other mechanical fuel such as automobile, tank, aircraft, tractor, rail vehicle can be used as, also can be used to generating, heating etc.The difference of industry and environment is used according to it, user also has very large difference for the specification of quality of diesel product, for the people at extremely frigid zones or life in winter, the demand of low freezing point diesel fuel remains high always, and traditional shape slective cracking technique can process the heavy gas oil cut of the content of wax, and pour point depression amplitude can reach 20 ~ 50 DEG C, while obtaining low freezing point diesel fuel, also can widen diesel oil distillate scope, improve productive rate, be the very useful and advanced technology solving low freezing point diesel fuel production problem.
The situation of China is also similar, particularly in recent years, along with improving constantly of the national economic development and environmental consciousness, requirement for diesel quality is more and more higher, and the popularity rate of diesel refining rises year by year, this external northern cold area, except the requirement to diesel oil regular refiner character, condensation point becomes and requisitely requires one of index, therefore, it is possible to improve the seed output and quality of low-coagulation diesel oil, the major issue becoming and pay close attention to Han Qu oil refining enterprise of meeting the need of market.And select row cracking and combination process thereof as one of Main Means reducing condensation point of diesel oil, can be used for producing low-sulfur low-coagulation diesel oil, be conducive to the economic benefit improving oil refining enterprise.
Diesel oil shape slective cracking technology, also known as hydrodewaxing, refers in the presence of hydrogen, and the diesel raw material of the content of wax by the dual-function catalyst surface containing active metal and molecular sieve, thus reduces wax molecule content wherein.Its dewaxing principle is under certain operating conditions, raw material is mixed with hydrogen contact with Hydrodewaxing catalyst, be cracked into small molecules paraffinic hydrocarbons in raw material, band short-side chain alkane, the naphthenic hydrocarbon of belt length side chain and the contour condensation point compositional selecting of aromatic hydrocarbons of belt length side chain, and other component does not change substantially, finally reach the object of the condensation point reducing oil product.Because it has that lower, the adaptability to raw material of reaction process hydrogen consumption is strong, energy consumption is lower, technical process is simple, can form the plurality of advantages such as process integration or independence use with other hydrogenation process, be therefore widely used.The a lot of oil refining enterprise of current northern China Han Qu all have employed this technology and produces low-coagulation diesel oil.
CN1257107A describes a kind of method of being produced high-grade low-freezing diesel oil by distillate.The method adopts hydrofining and hydrodewaxing one-stage serial flow process, and comprising Hydrobon catalyst and Hydrodewaxing catalyst two beds, hydrodewaxing adopts Ni/ZSM-5 catalyzer.The method is comparatively large at the temperature drop of Hydrodewaxing catalyst bed, and the yield of diesel oil distillate and the raising of depression effeCt are subject to a definite limitation, reduce the work-ing life of Hydrodewaxing catalyst.
CN102051232A describes a kind of method of diesel oil hydrogenation pour point depression, the method be by adjust catalyzer character thus make diesel oil depression effeCt good, the feature that diesel oil distillate yield is high, but owing to still adopting the combination process of hydrofining and hydrodewaxing series connection, the contradiction between depression effeCt and diesel oil distillate yield still exists.
CN102453531A describes a kind of method of diesel hydro-pour-reducing, although improve the average reaction temperature of Hydrodewaxing catalyst, utilize the temperature rise of finishing agent, increase the utilization ratio of pour point depression catalyzer, but the temperature of reaction of each bed outlet is still relatively high, and the cycle receives certain restriction.
CN01134271.4 discloses a kind of combined hydrogenation method producing high hexadecane value, low-coagulation diesel oil.The method is first contacted with catalyst for hydro-upgrading or hydrocracking catalyst stock oil, hydrogen, reaction effluent then contacts with Hydrodewaxing catalyst without separation, reaction effluent enters high-pressure separator through cooling, isolated product liquid enters fractionating system, and the gas circulation being rich in hydrogen returns reactor.The method can improve diesel-fuel cetane number simultaneously and reduce the condensation point of diesel oil in same set of device, and the cetane value of diesel product comparatively stock oil improves more than 6 units.
CN99113293.9 discloses a kind of method of being produced high-quality low-coagulation diesel oil with high hexadecane value by distillate.Hydrodewaxing is directly connected with hydrofining, hydro-upgrading by the method, realize hydrofining-hydro-upgrading-hydrodewaxing-section serial flow, what adopt is Hydrobon catalyst that anti-coking performance is strong and has stronger anti-ammonia, the hydro-upgrading of capacity antacid and Hydrodewaxing catalyst, and refining/depression effeCt is good, diesel yield is high, adaptability to raw material is strong, diesel cetane-number is high, technical process is simple and products scheme feature flexibly thus to make this technique have.
Summary of the invention
For prior art Problems existing, the invention provides a kind of production method of clean low-coagulation diesel oil.The mixed catalyst that hydrodewaxing and hydrofining compound load by the inventive method and catalyst for hydro-upgrading carry out grating, temperature rise in the temperature drop of hydrodewaxing process and unifining process is reasonably combined utilization, realize bed isothermal operation, yield and the cetane value of diesel oil is improve while producing low condensation point low-sulfur diesel-oil, reduce the hot(test)-spot temperature of device, extend running period; In addition reduce consumption or the process furnace load of cold hydrogen, save process cost, reduce device comprehensive energy consumption.
The production method of a kind of clean low-coagulation diesel oil provided by the invention, comprises following content:
After diesel raw material mixes with hydrogen, successively by the hydroconversion reaction zones of at least two series connection, comprise by the hydrodewaxing catalyzer composite bed of Hydrodewaxing catalyst and Hydrobon catalyst mixed packing and catalyst for hydro-upgrading bed successively by hydroconversion reaction zone described in Flow of Goods and Materials direction; Last hydroconversion reaction zone gained reaction effluent is through being separated and after fractionation, obtaining clean low freezing point diesel fuel product, and on a small quantity light naphthar and liquefied gas product.
According to method of the present invention, wherein in each described hydroconversion reaction zone, diesel raw material and hydrogen, first by the hydrodewaxing catalyzer composite bed by Hydrodewaxing catalyst and Hydrobon catalyst mixed packing, carry out hydrogenating desulfurization, hydrodenitrification, olefin saturated, aromatic saturation and hydroisomerizing and hydrodewaxing reaction; Reaction effluent by catalyst for hydro-upgrading bed, carries out deep hydrogenation saturated reaction and cyclic hydrocarbon ring-opening reaction etc. again.
According to method for hydrogen cracking of the present invention, described diesel raw material is conventional pour point depression raw material and high freezing point diesel fuel, and condensation point is generally all more than 0 DEG C, and preferred condensation point is more than 5 DEG C.The nitrogen content of described diesel raw material, at 2000 below μ g/g, is generally 50 ~ 1200 μ g/g, most preferably is 100 ~ 1000 μ g/g.The diesel oil distillate etc. of the various straight run that described diesel raw material can obtain for processing naphthenic base crude, intermediate base crude oil or paraffinic crude or secondary processing, preferably processes the said components that paraffinic crude obtains.The boiling range scope of diesel raw material is generally 130 ~ 440 DEG C, preferably 160 ~ 400 DEG C.As described in diesel raw material can be selected from processing the Daqing crude oil various straight-run diesel oils, coker gas oil, catalytic diesel oil etc. that obtain one or several.
Described Hydrodewaxing catalyst is the conventional pour point depression catalyzer in this area.Described catalyzer generally with shape slective cracking molecular sieve and tackiness agent for carrier, with group VIB and/or group VIII metal for hydrogenation active metals component.Described shape slective cracking molecular sieve is hydrogen type molecular sieve, described molecular sieve can be selected from Hydrogen ZSM-5, ZSM-11, ZSM-12, ZSM-22, ZSM-23, ZSM-35 and ZSM-38 molecular sieve one or more, preferred ZSM-5 molecular sieve; The silica alumina ratio of described shape slective cracking molecular sieve is generally 10 ~ 150, is preferably 20 ~ 120.Described group VIB metal is Mo and/or W, and described group VIII metal is Co and/or Ni.With the weight of catalyzer for benchmark, hydrogenation active metals component is with the content of oxide basis for 1% ~ 16%, and the content of shape slective cracking molecular sieve is 50% ~ 85%, and the content of tackiness agent is 10% ~ 40%.Described Hydrodewaxing catalyst can select existing various commercial catalysts, the Hydrodewaxing catalysts such as FDW-1, FDW-3 that such as Fushun Petrochemical Research Institute (FRIPP) develops; Also can be prepared by the general knowledge of this area as required, such as, can prepare satisfactory Hydrodewaxing catalyst with reference to content disclosed in CN1952074A, CN1352231A, CN101143333A, CN102451748A.
Described Hydrobon catalyst can be diesel oil hydrofining catalyst, also can be hydrocracking pre-refining catalyzer, the highly effective hydrogenation catalyst for refining of the high metal content that body phase legal system also can be used standby.Described Hydrobon catalyst mainly comprises hydrogenation active metals and modified aluminium oxide supports component etc.General Hydrobon catalyst is made up of hydrogenation active metals component and various modified aluminium oxide supports etc. such as W, Mo, Co, Ni, Fe, and with the weight of catalyzer for benchmark, the content of hydrogenation component is 15% ~ 80%.Conventional hydro catalyst for refining can select existing various commercial catalysts, FHUDS diesel oil hydrofining catalyst series, FF hydrocracking pre-refining catalyst series and FTX body phase method highly effective hydrogenation that such as FRIPP develops refine catalyst series, and the UF series hydrofining catalyzer of the UOP of offshore company, the diesel oil hydrofining catalysts such as Albemarle Corporation KF757.Also can be prepare the close Hydrobon catalyst of selectivity by the general knowledge of this area as required.
Catalyst for hydro-upgrading described in the present invention is the hydrogenation conversion catalyst containing molecular sieve, and especially a kind of hydrogenation catalyst being exclusively used in diesel modifying is the conventional hydro conversion catalyst in this area.Described catalyst for hydro-upgrading is a kind of dual function hydrogenation catalyst, with aluminum oxide and Y zeolite for carrier, containing at least one VI B race's metal and at least one VIII race metal, it is characterized in that support of the catalyst consists of aluminum oxide 40w% ~ 80w%, amorphous aluminum silicide 0 ~ 20w%, molecular sieve 5w% ~ 30w%, the wherein pore volume 0.40 ~ 0.52mL/g of Y molecular sieve, specific surface 750 ~ 900m
2/ g, lattice constant 2.420 ~ 2.500nm, SiO
2/ Al
2o
3molecular ratio is 7 ~ 15, and in catalyzer, VI B family metal oxide content is 10w% ~ 30w%, and VIII family metal oxide content is 2w% ~ 15w%.
VI wherein said B race metal can be Mo or W, and preferably select W, VIII race's metal can be Ni or Co, preferably selects Ni.Conventional hydro modifying catalyst can select existing various commercial catalysts, such as FRIPP develop 3963, the catalyzer such as FC-18.Also specific catalyst for hydro-upgrading can be prepared by the general knowledge of this area as required, such as, satisfactory hydro-upgrading (conversion) catalyzer can be prepared with reference to content disclosed in CN1184843A, CN1178238A.
According to method of the present invention, in each hydroconversion reaction zone, described catalyst for hydro-upgrading bed is generally 1:10 ~ 10:1, preferred 1:5 ~ 5:1 with the admission space ratio of hydrodewaxing catalyzer composite bed.
The operational condition of the pour point depression catalyzer composite bed that described hydrodewaxing and Hydrobon catalyst form is: reaction pressure 6.0 ~ 20.0MPa, hydrogen to oil volume ratio 200:1 ~ 1500:1, and volume space velocity is 0.1 ~ 10.0h
-1, temperature of reaction 270 DEG C ~ 460 DEG C; Preferred operations condition is reaction pressure 6.0 ~ 15.0MPa, hydrogen to oil volume ratio 300:1 ~ 1000:1, volume space velocity 0.3 ~ 8.0h
-1, temperature of reaction 315 DEG C ~ 427 DEG C.
In described pour point depression catalyzer composite bed, Hydrodewaxing catalyst and Hydrobon catalyst compound are loaded, and admission space is than being 1:10 ~ 10:1, preferred 1:5 ~ 5:1.
The operational condition of described catalyst for hydro-upgrading bed is: reaction pressure 6.0 ~ 20.0MPa, hydrogen to oil volume ratio 200:1 ~ 1500:1, and volume space velocity is 0.1 ~ 10.0h
-1, temperature of reaction 260 DEG C ~ 455 DEG C; Preferred operations condition is reaction pressure 7.0 ~ 15.0MPa, hydrogen to oil volume ratio 300:1 ~ 1000:1, volume space velocity 0.3 ~ 8.0h
-1, temperature of reaction 310 DEG C ~ 410 DEG C.
For described at least two hydroconversion reaction zones, wherein said hydrodewaxing catalyzer composite bed and catalyst for hydro-upgrading bed, can be separately positioned in the two or more bed of a reactor; Or can be separately positioned in the hydrogenator of two or more series connection.
Compared with prior art, the inventive method has the following advantages:
1, in the inventive method, in each hydroconversion reaction zone, stock oil is first by hydrofining and Hydrodewaxing catalyst mixing bed, and because the saturated reaction of the unsaturated hydrocarbons of hydrofining reaction and the reaction of deviating from of impurity all show as thermopositive reaction, this process catalyst bed produces temperature rise; And hydrodewaxing reaction is for selecting type molecular sieve cracking and isomerization reaction, heat effect shows as thermo-negative reaction, and process produces temperature drop; These two kinds of catalyzer are carried out grating mixed packing, its respective heat release and thermo-negative reaction feature can be made full use of, the comprehensive utilization of the heat of realization response process, obvious temperature rise and temperature drop effect can not be produced, and affect depression effeCt, thus make the reaction of composite catalyst bed can realize the reaction process of isothermal, obtain desirable reaction effect, both can ensure the yield of diesel oil, also achieve better depression effeCt, be more conducive to the long-term operation of device.After hydrofining and hydrodewaxing mixed catalyst bed, again by catalyst for hydro-upgrading bed, carry out aromatic saturation and cyclic hydrocarbon ring-opening reaction, advanced treatment is continued to diesel component, reaction process shows as exothermic effect, the temperature of charge making reaction outlet final is higher, thus obtains good heat transfer effect, is conducive to saving energy and reduce the cost.
2, at process aspect, in each hydroconversion reaction zone, substantially identical effect is all shown.Thus at least two hydroconversion reaction zones of series connection, described hydrogenation reaction shows as comprehensive cumulative effect of optimization.Compared with prior art, the present invention is on the basis of not changing device flow process, load by means of only the grading composition of catalyzer and Homogeneous phase mixing, from local by the high temperature dot of device and the effective Appropriate application of low warm spot, reduce the hot(test)-spot temperature of device, reasonably decrease the bulk temperature gradient of device, give full play of the catalytic performance of catalyzer the best, extend the work-ing life of catalyzer.In addition this combination is compared with the hydrodewaxing combination process of routine, heat due to reaction process obtains and more reasonably utilizes, can beat less between two reaction zones or not liquid hydrogen injection, therefore consumption and the process furnace load of cold hydrogen is also reduced, save process cost, reduce device comprehensive energy consumption.
Accompanying drawing explanation
Fig. 1 is the grading loading schematic diagram of a kind of embodiment of the inventive method; Single reactor layering is selected to load the operating method of two hydroconversion reaction zones.
Embodiment
Be described in detail below in conjunction with the production method of accompanying drawing to a kind of clean low-coagulation diesel oil of the present invention.
As shown in Figure 1, the flow process of clean low-coagulation diesel oil production method of the present invention is as follows:
Stock oil 1 enters reactor 3 with hydrogen 2 after reactor inlet mixes, from top to bottom successively by hydrodewaxing and hydrorefined composite catalyst bed 4, catalyst for hydro-upgrading bed 5, hydrodewaxing and hydrorefined composite bed 6 and the catalyst for hydro-upgrading bed 7 of connecting step by step, obtain reaction effluent 8 and discharge from reactor bottom enter into high-pressure separator 10 after water filling 9, high-pressure separator 10 top obtains gas 11 by circulating hydrogen compressor 12, and hydrogen or cold hydrogen use as a supplement to obtain recycle hydrogen 14 after mixing with new hydrogen 13; The liquid phase that high-pressure separator 10 middle and lower part obtains enters light pressure separator 17, and light pressure separator 17 top is discharged low point of gas 18 and gone subsequent disposal, and light pressure separator 17 middle and lower part obtains liquid phase 20 and enters subsequent fractionation system; The sour water 15 of discharging bottom high-pressure separator 10 mixes rear disacidify water treatment device with the sour water 19 of discharging bottom light pressure separator 17 and carries out following process.
Next by specific embodiment, clean low-coagulation diesel oil production method of the present invention is further described.
Comparative example 1
Comparative example 1 is the device adopting hydrofining, hydrodewaxing and hydro-upgrading one-stage serial flow process to produce clean low freezing point diesel fuel.Comparative example 1 comprises two reaction zones, each reaction zone includes the pour point depression beds and catalyst for hydro-upgrading bed that are loaded by Hydrobon catalyst and Hydrodewaxing catalyst layering, the catalyst loading ratio of two reaction zones is identical, and the catalyzer composition of single reaction zone is in table 2.Comparative example 1 produces the low-coagulation diesel oil of the identical trade mark with embodiment 1.The catalyzer used, stock oil and diesel product condensation point are all identical with embodiment 1.Operation result lists in table 2.
Comparative example 2
Comparative example 2 is the device adopting hydrofining, hydrodewaxing and hydro-upgrading one-stage serial flow process to produce low freezing point diesel fuel.Control substantially identical diesel yield with embodiment 1, produce the low-coagulation diesel oil of the different trade mark.The catalyzer that comparative example uses, stock oil and diesel product yield are all identical with embodiment 1, and catalyst loading is with comparative example 1.Operation result lists in table 2.
Embodiment 1
Adopt the technical process shown in Fig. 1, utilize grating to connect and load in mixture flow process and produce low freezing point diesel fuel.Embodiment 1 comprises the hydroconversion reaction zone of two series connection, and in the pour point depression catalyzer composite bed of each reaction zone, Hydrodewaxing catalyst is 2:1 with the mixed volume ratio of Hydrobon catalyst.The Hydrobon catalyst used in embodiment 1 is FF-46 catalyzer, and Hydrodewaxing catalyst is FDW-3 catalyzer, and catalyst for hydro-upgrading agent is 3963 catalyzer, and described catalyzer is the commercial catalyst of Fushun Petrochemical Research Institute's development and production.
Operational condition and test-results list in table 2.
Table 1 stock oil property list.
| Project | Stock oil |
| Source | Atmosphere 3rd side cut+catalytic diesel oil |
| Ratio | 1:1 |
| Density (20 DEG C)/gcm -3 | 0.8642 |
| Boiling range scope/DEG C | 160～385 |
| Nitrogen/μ gg -1 | 241 |
| Sulphur/μ gg -1 | 3420 |
| Condensation point/DEG C | 1 |
| Cetane index | 43 |
Table 2 process conditions and result.
| Comparative example 1 | Comparative example 2 | Embodiment 1 | |
| Catalyzer forms | (FDW-3/FF-46)/3963 | (FDW-3/FF-46)/3963 | (FDW-3+FF-46)/3963 |
| Reaction pressure/MPa | 9.0 | 9.0 | 9.0 |
| Average reaction temperature/DEG C | 377*/379/378*/380 | 376*/385/377*/389 | 378*/379/379*/386 |
| LHSV/h -1 | 5.0**/6.0/5.0**/6.0 | 5.0**/6.0/5.0**/6.0 | 5.0**/6.0/5.0**/6.0 |
| Entrance hydrogen to oil volume ratio | 600:1 | 600:1 | 600:1 |
| Diesel product condensation point/DEG C | -38 | -22 | -37 |
| Diesel yield, wt% | 73.9 | 81.2 | 80.8 |
| Bed vertex temperature/DEG C | 399 | 390 | 389 |
| Cold hydrogen consumption/benchmark | 1.1 | 1.9 | 1.0 |
| Diesel oil density/gcm -3 | 0.8345 | 0.8364 | 0.8246 |
| Diesel fuel cetane index | 49 | 48 | 52 |
| Diesel oil sulphur content/μ gg -1 | 34 | 24 | 12 |
* average reaction temperature is the weighted mean temperature of pour point depression beds;
* volume space velocity is the volume space velocity of pour point depression beds.
As can be seen from above embodiment, the maximum feature of the inventive method is, producing low solidifying product for processing diesel raw material, product cetane value can be improved, the condensation point of raw material can be reduced simultaneously when ensureing certain diesel yield to greatest extent; In addition also to have hot(test)-spot temperature low for the inventive method, and running period is long, the feature that cold hydrogen consumption is low; For enterprise, while completing quality products production task, human and material resources and energy consumption have very large advantage.
Claims (11)
1. a production method for clean low-coagulation diesel oil, comprises following content:
After diesel raw material mixes with hydrogen, successively by the hydroconversion reaction zone of at least two series connection, by Flow of Goods and Materials direction, each described hydroconversion reaction zone comprises by the hydrodewaxing catalyzer composite bed of Hydrodewaxing catalyst and Hydrobon catalyst mixed packing and catalyst for hydro-upgrading bed successively; Last hydroconversion reaction zone gained reaction effluent is through being separated and after fractionation, obtaining clean low freezing point diesel fuel product, and on a small quantity light naphthar and liquefied gas product;
Wherein, in each hydroconversion reaction zone, described catalyst for hydro-upgrading bed is 1:10 ~ 10:1 with the admission space ratio of hydrodewaxing catalyzer composite bed; In described hydrodewaxing catalyzer composite bed, Hydrobon catalyst is 1:10 ~ 10:1 with the admission space ratio of Hydrodewaxing catalyst.
2. in accordance with the method for claim 1, it is characterized in that, the condensation point of described diesel raw material is more than 0 DEG C, and nitrogen content is at 2000 below μ g/g.
3. according to the method described in claim 1 or 2, it is characterized in that, the condensation point of described diesel raw material is more than 5 DEG C, and nitrogen content is 50 ~ 1200 μ g/g.
4. in accordance with the method for claim 1, it is characterized in that, the nitrogen content in described diesel raw material is at 2000 more than μ g/g, and diesel raw material is before the hydrodewaxing catalyzer composite bed by the first hydroconversion reaction zone, in advance by a Hydrobon catalyst bed, carry out part denitrogenation.
5. in accordance with the method for claim 1, it is characterized in that, doing of described diesel raw material is 350 ~ 440 DEG C.
6. in accordance with the method for claim 1, it is characterized in that, described catalyst for hydro-upgrading with aluminum oxide, amorphous aluminum silicide and Y zeolite for carrier, containing at least one VI B race's metal and at least one VIII race metal, support of the catalyst consists of aluminum oxide 40w% ~ 80w%, amorphous aluminum silicide 0w% ~ 20w%, Y zeolite 5w% ~ 30w%, wherein the pore volume 0.40 ~ 0.52mL/g of Y zeolite, specific surface 750 ~ 900m
2/ g, lattice constant 2.420 ~ 2.500nm, SiO
2/ Al
2o
3molecular ratio 7 ~ 15; In catalyzer, VI B family metal oxide content is 10w% ~ 30w%, and VIII family metal oxide content is 2w% ~ 15w%.
7. in accordance with the method for claim 1, it is characterized in that, described Hydrodewaxing catalyst with shape slective cracking molecular sieve and tackiness agent for carrier, with group VIB and/or group VIII metal for hydrogenation active metals component, with the weight of catalyzer for benchmark, hydrogenation active metals component is with the content of oxide basis for 1% ~ 16%, and the content of shape slective cracking molecular sieve is 50% ~ 85%, and the content of tackiness agent is 10% ~ 40%.
8. in accordance with the method for claim 7, it is characterized in that, one or more in Hydrogen ZSM-5, ZSM-11, ZSM-12, ZSM-22, ZSM-23, ZSM-35 and ZSM-38 molecular sieve of described shape slective cracking molecular screening, the silica alumina ratio of shape slective cracking molecular sieve is 10 ~ 150.
9. in accordance with the method for claim 1, it is characterized in that, described Hydrobon catalyst comprises hydrogenation active metals and modified aluminium oxide supports component, with the weight of catalyzer for benchmark, the content of hydrogenation active metals with oxide basis for 15% ~ 80%.
10. in accordance with the method for claim 1, it is characterized in that, the operational condition of described catalyst for hydro-upgrading bed is: reaction pressure 6.0 ~ 20.0MPa, hydrogen to oil volume ratio 200:1 ~ 1500:1, and volume space velocity is 0.1 ~ 10.0h
-1, temperature of reaction 260 DEG C ~ 455 DEG C.
11. in accordance with the method for claim 1, it is characterized in that, the operational condition of the described hydrodewaxing catalyzer composite bed be made up of hydrodewaxing and Hydrobon catalyst is: reaction pressure 6.0 ~ 20.0MPa, hydrogen to oil volume ratio 200:1 ~ 1500:1, volume space velocity is 0.1 ~ 10.0h
-1, temperature of reaction 270 DEG C ~ 460 DEG C.
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