CN103805263B - A kind of method of producing high-grade low-freezing diesel oil - Google Patents
A kind of method of producing high-grade low-freezing diesel oil Download PDFInfo
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Abstract
The invention discloses a kind of method of producing high-grade low-freezing diesel oil.After diesel raw material mixes with hydrogen, successively by the hydroconversion reaction zones of at least two series connection, comprise by the refining pour point depression composite catalyst bed of Hydrodewaxing catalyst and Hydrobon catalyst mixed packing and hydro-upgrading isomerization-visbreaking beds 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 low freezing point diesel fuel.Hydrofining and the temperature rise of upgrading and pour point reducing process and the temperature drop of hydrodewaxing process are reasonably combined utilization by the inventive method, yield and the cetane value of diesel oil is improve while producing low solidifying low-sulfur diesel-oil, reduce the hot(test)-spot temperature of device, extend running period; 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 method of producing high-grade low-freezing diesel oil, especially a kind of by catalyzer grating technology and compound filling technology, be used for producing the method for hydrotreating of 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 shape slective cracking and combination process thereof are 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 is by the character of adjustment catalyzer thus to have 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, between depression effeCt and diesel oil distillate yield, contradiction still exists.
CN102453531A describes a kind of method of diesel hydro-pour-reducing, although improve the average reaction temperature of Hydrodewaxing catalyst, utilizes the temperature rise of finishing agent, increases the utilization ratio of pour point depression catalyzer,
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 method of producing high-grade low-freezing diesel oil.The mixed catalyst that hydrofining and hydrodewaxing compound are loaded by the inventive method and hydro-upgrading isomerization-visbreaking catalyzer carry out grating, temperature rise in the temperature drop of hydrodewaxing process and hydrogenation process is reasonably combined utilization, 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 the consumption of cold hydrogen or the combustion gas loss of process furnace, save process cost.
A kind of method of producing high-grade low-freezing 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 refining pour point depression catalyzer composite bed of Hydrobon catalyst and Hydrodewaxing catalyst mixed packing and hydro-upgrading isomerization-visbreaking beds 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 low-sulfur, low freezing point diesel fuel product.
According to method of the present invention, wherein in each described hydroconversion reaction zone, diesel raw material and hydrogen, first by the refining pour point depression catalyzer composite bed by Hydrobon catalyst and Hydrodewaxing catalyst mixed packing, carry out hydrogenating desulfurization, denitrogenation and pour point depression reaction; By hydro-upgrading isomerization-visbreaking beds, further there is the reactions such as hydrogenating desulfurization, denitrogenation, aromatic saturation and pour point depression again in reaction effluent.
According to method of hydrotreating 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 ~ 500 μ g/g.If the nitrogen content in diesel raw material is too high, if nitrogen content is when 2000 more than μ g/g, before the refining pour point depression beds of diesel raw material by the first hydroconversion reaction zone, in advance by a hydrofining or hydrodenitrogenation catalyst bed, part denitrogenation can be carried out.The various straight-run diesel oil that described diesel raw material can obtain for processing naphthenic base crude, intermediate base crude oil or paraffinic crude or secondary processing diesel oil, preferably process the said components that paraffinic crude obtains.Doing of described diesel raw material is generally 350 ~ 440 DEG C, best 370 ~ 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.
Hydrobon catalyst of the present invention can adopt conventional diesel oil hydrofining catalyst, generally with VI B race and/or group VIII metal for active ingredient, with aluminum oxide or silicon-containing alumina for carrier, group VIB metal is generally Mo and/or W, and group VIII metal is generally Co and/or Ni.With the weight of catalyzer for benchmark, group VIB metal content take oxide basis as 8wt% ~ 28wt%, and group VIII metal content take oxide basis as 2wt% ~ 15wt%, and its character is as follows: specific surface is 100 ~ 650m
2/ g, pore volume is 0.15 ~ 0.8mL/g, and alternative commercial catalysts is of a great variety, the Hydrobon catalysts such as FH-98, FH-UDS that such as Fushun Petrochemical Research Institute (FRIPP) develops; Also can as required by the hydrotreatment oxidized catalyst that the general knowledge preparation of this area is conventional.
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 hydro-upgrading isomerization-visbreaking catalyzer is the conventional catalyst in this area.Described hydro-upgrading pour point depression catalyzer generally comprises amorphous aluminum silicide, the beta-molecular sieve of modification, porous refractory oxide, VI B race and VIII family metal oxide.With the weight ratio of catalyzer for benchmark, in catalyzer, the content of each component is generally: amorphous aluminum silicide 29w% ~ 50w%, modified beta molecular sieve 1w% ~ 9%, group VIB metal is with oxide basis 15w% ~ 35w%, group VIII metal take oxide basis as 3w% ~ 9w%, porous refractory oxide 0w% ~ 45w%; The wherein SiO of modified beta molecular sieve
2/ Al
2o
3weight ratio is 50 ~ 90, and average grain size is 0.1 ~ 0.5 micron, infrared acidity 0.1 ~ 0.4mmol/g.
Described porous refractory oxide, can be selected from one or more in aluminum oxide, titanium oxide, zirconium white, boron oxide and above-mentioned element (aluminium, titanium, zirconium, boron) composite oxides etc., preferential oxidation aluminium.As contained macroporous aluminium oxide and aperture alumina adhesive, macroporous aluminium oxide is generally 0w% ~ 22w%; Little porous aluminum oxide is generally 0w% ~ 23w%.The specific surface area of catalyzer is generally 160 ~ 230m
2/ g, pore volume is 0.32 ~ 0.45mL/g.The character of described modified beta molecular sieve is generally: its SiO
2/ Al
2o
3weight ratio is generally 50 ~ 90, and degree of crystallinity is generally 90 ~ 110, and average grain size is generally 0.1 ~ 0.5 micron, specific surface area 400 ~ 750m
2/ g, pore volume 0.25 ~ 0.50mL/g, Na
2o content is less than 0.10w%, and the secondary pore pore volume of infrared acidity 0.1 ~ 0.4mmol/g, 2 ~ 10nm accounts for 30% ~ 60% of total pore volume.
SiO in described amorphous aluminum silicide
2content be generally 20w% ~ 75w%, be preferably 35w% ~ 60w%.The pore volume of amorphous aluminum silicide is 0.5 ~ 1.1mL/g, is preferably 0.6 ~ 0.8mL/g; Specific surface area is 200 ~ 500m
2/ g, is preferably 280 ~ 500m
2/ g.
Macroporous aluminium oxide pore volume is 0.6 ~ 1.2mL/g, is preferably 0.8 ~ 1.2mL/g, and specific surface area is 200 ~ 550m
2/ g, is preferably 300 ~ 500m
2/ g.Aperture aluminum oxide pore volume is 0.3 ~ 0.5mL/g, and specific surface area is 180 ~ 350m
2/ g.Group VIB metal is generally W and/or Mo, and group VIII metal is generally Ni and/or Co.
Conventional hydro upgrading isomerization-visbreaking catalyzer can select existing various commercial catalysts, the catalyzer such as FC-14, FC-20 that such as FRIPP develops.Also specific hydro-upgrading isomerization-visbreaking catalyzer can be prepared by the general knowledge of this area as required, such as, satisfactory hydro-upgrading isomerization-visbreaking catalyzer can be prepared with reference to content disclosed in CN1712498A.
The operational condition of the refining pour point depression catalyzer composite bed of described hydrofining and Hydrodewaxing catalyst composition 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; 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 315 DEG C ~ 415 DEG C.
The operational condition of described hydro-upgrading isomerization-visbreaking beds is generally: 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.
According to method of the present invention, wherein in each hydroconversion reaction zone, described hydro-upgrading isomerization-visbreaking beds is 1:10 ~ 10:1 with the admission space ratio of hydrocracking pretreatment catalyzer composite bed, is preferably 1:5 ~ 5:1.
In described hydrocracking pretreatment catalyzer composite bed, Hydrobon catalyst loads with Hydrodewaxing catalyst compound (mixing), and the admission space of two kinds of catalyzer is than being 1:10 ~ 10:1, preferred 1:5 ~ 5:1.
For described at least two hydroconversion reaction zones, wherein said hydro-upgrading isomerization-visbreaking beds and hydrocracking pretreatment catalyzer composite bed, can be separately positioned in the different beds 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 composite bed, carry out hydrogenating desulfurization, hydrodenitrification and pour point depression reaction, improve the adaptability of stock oil, because hydrofining reaction shows as thermopositive reaction, this process produces temperature rise; And hydrodewaxing reaction is for selecting the reaction of type molecular sieve cracking, 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 endothermic effect 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 the reaction of composite catalyst bed is made substantially to realize the reaction process of isothermal.Raw material after the process of hydrocracking pretreatment composite bed is again by hydro-upgrading isomerization-visbreaking beds, diesel raw material is processed further, obtain the diesel product of more high-quality, while the quality that the present invention can ensure diesel oil and yield, obtain better depression effeCt.
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 compound, 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, 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 also reduce the consumption of cold hydrogen and the combustion gas loss of process furnace, save process cost.
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
Below in conjunction with accompanying drawing, a kind of method of producing high-grade low-freezing diesel oil of the present invention is described in detail.
As shown in Figure 1, the method flow of production high-grade low-freezing diesel oil of the present invention is as follows: stock oil 1 enters reactor 3 with hydrogen 2 after reactor inlet mixes, pass through the composite catalyst bed 4 of hydrofining and the hydrodewaxing of connecting step by step from top to bottom successively, hydro-upgrading isomerization-visbreaking beds 5, the composite bed 6 of hydrofining and hydrodewaxing and hydro-upgrading isomerization-visbreaking beds 7, obtain reaction effluent 8 and after water filling 9, enter into high-pressure separator 10 from reactor bottom discharge, high-pressure separator 10 top obtains gas 11 by circulating hydrogen compressor 12, 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, production high-grade low-freezing diesel oil method of the present invention is further described.
Embodiment 1
Adopt the technical process shown in Fig. 1, utilize grating and load in mixture serial flow and produce low condensation point fine-quality diesel oil.Embodiment 1 comprises the hydroconversion reaction zone of two series connection, and in the upgrading and pour point reducing catalyzer composite bed of each reaction zone, Hydrobon catalyst is 1:4 with the mixed volume ratio of Hydrodewaxing catalyst.The Hydrobon catalyst used in embodiment 1 is FH-98 catalyzer, hydro-upgrading isomerization-visbreaking catalyzer is FC-14 catalyzer, Hydrodewaxing catalyst is FDW-3 catalyzer, and described catalyzer is the commercial catalyst of Fushun Petrochemical Research Institute's development and production.
Comparative example 1
Comparative example 1 is the device adopting hydrodewaxing and hydrofining, hydro-upgrading isomerization-visbreaking one-stage serial flow process to produce low-sulfur, low freezing point diesel fuel.Comparative example 1 comprises two reaction zones, and first reaction zone is the refining pour point depression beds loaded by Hydrodewaxing catalyst and Hydrobon catalyst layering, and filling ratio is 1:1, and second hydroconversion reaction zone is hydro-upgrading isomerization-visbreaking catalyzer.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 hydrodewaxing and hydrofining, hydro-upgrading isomerization-visbreaking one-stage serial flow process to produce low-sulfur, 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.
Operational condition and test-results list in table 2.
Table 1 stock oil property list.
| Project | Stock oil |
| Density (20 DEG C)/gcm -3 | 0.8688 |
| Boiling range scope/DEG C | 270～380 |
| Nitrogen/μ gg -1 | 86 |
| Sulphur/μ gg -1 | 900 |
| Condensation point/DEG C | 12 |
| Cetane value | 27 |
Table 2 process conditions and result.
| Comparative example 1 | Comparative example 2 | Embodiment 1 | |
| Catalyzer forms | (FH-98/FDW-3)/FC-14 | (FH-98/FDW-3)/FC-14 | (FDW-3+FH-98)/FC-14 |
| Reaction pressure/MPa | 9.0 | 9.0 | 9.0 |
| Average reaction temperature/DEG C | 381*/377 | 379*/368 | 382*/377/383*/376 |
| LHSV/h -1 | 2.5**/3.0 | 2.5**/3.0 | 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 | -37 | -23 | -38 |
| Diesel oil sulphur content/μ gg -1 | 12 | 52 | 9 |
| Diesel yield, wt% | 73.76 | 82.8 | 83.4 |
| Diesel cetane-number | 45 | 39 | 48 |
| Bed vertex temperature/DEG C | 392 | 384 | 387 |
| Cold hydrogen consumption/benchmark | 0.92 | 1.75 | 1.0 |
* average reaction temperature is the weighted mean temperature of refining pour point depression beds;
* volume space velocity is the volume space velocity of refining pour point depression beds.
As can be seen from above embodiment, the inventive method can reduce product foreign matter content, improve product cetane value, when ensureing certain diesel yield, can reduce the condensation point of raw material to greatest extent again; In addition also to have bed 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 (10)
1. produce a method for high-grade low-freezing diesel oil, comprise following content:
After diesel raw material mixes with hydrogen, successively by the hydroconversion reaction zones of at least two series connection, comprise by the refining pour point depression composite catalyst bed of Hydrobon catalyst and Hydrodewaxing catalyst mixed packing and hydro-upgrading isomerization-visbreaking beds successively by each described hydroconversion reaction zone, Flow of Goods and Materials direction; Last hydroconversion reaction zone gained reaction effluent is through being separated and after fractionation, obtaining low freezing point diesel fuel product;
Wherein, in each described hydroconversion reaction zone, be 1:10 ~ 10:1 by Hydrobon catalyst and the refining pour point depression composite catalyst bed of Hydrodewaxing catalyst mixed packing and the admission space ratio of hydro-upgrading isomerization-visbreaking beds; In described refining pour point depression composite catalyst 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. in accordance with the method for claim 1, 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 of described diesel raw material is at 2000 more than μ g/g, before diesel raw material is by the refining pour point depression composite catalyst bed of the first hydroconversion reaction zone, in advance by a hydrofining or hydrodenitrogenation 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, the described operational condition by the refining pour point depression composite catalyst bed of Hydrobon catalyst and Hydrodewaxing catalyst mixed packing 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 260 DEG C ~ 455 DEG C.
7. in accordance with the method for claim 1, it is characterized in that, the operational condition of described hydro-upgrading isomerization-visbreaking beds 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.
8. in accordance with the method for claim 1, it is characterized in that, described Hydrobon catalyst adopts conventional diesel oil hydrofining catalyst, with VI B race and/or group VIII metal for active ingredient, with aluminum oxide or silicon-containing alumina for carrier, with the weight of catalyzer for benchmark, group VIB metal content take oxide basis as 8wt% ~ 28wt%, and group VIII metal content take oxide basis as 2wt% ~ 15wt%.
9. 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 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%.
10. in accordance with the method for claim 1, it is characterized in that, described hydro-upgrading isomerization-visbreaking catalyzer comprises amorphous aluminum silicide, modified beta molecular sieve, porous refractory oxide, VI B race and VIII family metal oxide, with the weight ratio of catalyzer for benchmark, the content of each component is: amorphous aluminum silicide 29w% ~ 50w%, modified beta molecular sieve 1w% ~ 9%, group VIB metal is with oxide basis 15w% ~ 35w%, group VIII metal take oxide basis as 3w% ~ 9w%, porous refractory oxide 0w% ~ 45w%; The wherein SiO of modified beta molecular sieve
2/ Al
2o
3weight ratio is 50 ~ 90, and average grain size is 0.1 ~ 0.5 micron, infrared acidity 0.1 ~ 0.4mmol/g.
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