CN1417301A - Method of desulfurizing and dearomatizing diesel oil deeply - Google Patents
Method of desulfurizing and dearomatizing diesel oil deeply Download PDFInfo
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- CN1417301A CN1417301A CN 01134272 CN01134272A CN1417301A CN 1417301 A CN1417301 A CN 1417301A CN 01134272 CN01134272 CN 01134272 CN 01134272 A CN01134272 A CN 01134272A CN 1417301 A CN1417301 A CN 1417301A
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Abstract
During the deeply diesel oil desulfurizing and dearomatizing process, raw material oil and hydrogen are mixed and contacted with hydroupgrading catalyst, hydrocracking catalyst or hydrofining catalyst in the first reactor; the reaction effluent is stripped at high temperature and high pressure in a hydrogen stripping tower and contacted with conventional hydrofining catalyst in the second reactor; the effluent from the second reactor is passed through high pressure separator, low pressure separator and fractionating tower successively; the reaction product is divided into naphtha and diesel oil fraction in the fractionating tower; the hydrogen-rich gas separated from the high pressure separator and the stripping tower is mixed with fresh hydrogen and the mixed gas is separated into two parts to the first reactor and the second reactor separately.
Description
Technical field
The invention belongs to a kind ofly in the method that has under the situation of hydrogen refining hydrocarbon ils, more particularly, is a kind of method of desulfurizing and dearomatizing diesel oil deeply.
Background technology
Because the cry of environment protection increases day by day, countries in the world have been revised their diesel oil specification one after another, to require oil refining enterprise production environment close friend's fuel.In new diesel oil specification, changing bigger is sulphur content, aromaticity content and these several indexs of cetane value.1998, by " world's fuel oil standard " that the U.S., European Union and Japan three big Automobile Associationss initiate to formulate the diesel product standard is divided for 1 class, 2 classes, 3 classes, increased 4 classes recently again newly.Wherein 2 class diesel oil require: sulphur content is not more than 300ppm, and total aromaticity content is not higher than 25m%, and polycyclic aromatic hydrocarbon content is not higher than 5m%, and cetane index is not less than 50; 3 class diesel oil require: sulphur content is not more than 30ppm, and total aromaticity content is not higher than 15m%, and polycyclic aromatic hydrocarbon content is not higher than 2m%, and cetane index is not less than 52.This specification is as world's standard, and the formulation of the new diesel oil standard in various countries is being produced deep effect.
Produce above-mentioned new spec diesel oil from straight-run diesel oil or catalytic diesel oil, by transforming existing hydro-refining unit (5.0～6.0MPa pressure rating), can make sulphur content reach requirement as the higher means such as catalyst for refining of activity that reduce air speed or raising temperature of reaction, more renew.But the reduction of aromatic hydrocarbons is an a great problem.Cetane value in fact also is that the aromatic hydrocarbons character with oil product matters a lot, and high aromaticity content causes low cetane value, thus hydrofining to improve cetane value also be limited in one's ability.Aromatic hydrogenation saturated very difficult under common hydrofining condition be because its thermodynamic property decision.
In order to solve the problem that diesel oil deep takes off aromatic hydrocarbons, each major company starts with from the response characteristic of aromatic hydrogenation and has proposed two big methods.A kind of method is to improve reaction pressure, the hydrogen dividing potential drop is risen to more than the 10.0MPa, utilize existing sulphided state hydrogenation catalyst can reach 50～60% aromatic hydrocarbons saturation exponent like this, reduce aromaticity content, be expected to produce aromatic hydrocarbons and the qualified diesel oil fuel of cetane value by regulating other operational condition again; Another kind method is to adopt new Technology, under the pressure rating of existing apparatus, utilize the active next saturated aromatic hydrocarbons of low temperature hydrogenation of noble metal catalyst, the aromatic hydrogenation temperature of reaction is not carried out in the thermodynamics equilibrium limit district, thereby reduce aromaticity content in the oil effectively.
USP5,114,562 disclose a kind of technology of utilizing two-stage hydrogenation technology to produce the low fragrant product of low-sulfur from intermediate distillates.This technological process is removed H for the liquid product that comes out from first section reactor through hydrogen stripped
2S and NH
3After, heat up through heat exchange again, enter into second section reactor.Load finishing agent in first section reactor, filling is to H in second section reactor
2The noble metal catalyst that S concentration is very sensitive.Compare with first section, second section pressure and air speed are higher, and temperature is lower.
USP5,183,556 have announced a kind of two-stage hydrogenation technology of producing fine-quality diesel oil from diesel oil distillate, reactor is placed in-line in this technology.During operation, hydrogen and liquid phase feeding also flow to into first section reactor, and the liquid-phase product that comes out from first section reactor contacts with hydrogen is reverse second section reactor.The used reactor of this technology is fixed-bed reactor, and first section is base metal catalysts, and second section can be noble metal catalyst, also the available bases metal catalyst.
" Upgrading Light Cycle Oil to Diesel Using the Engelhard-WashingtonREDAR Process " (calendar year 2001 NPRA meeting AM-01-23) has been introduced the technology of utilizing REDAR technology catalytic cracking light cycle oil upgrading to be become diesel oil.This technology realizes in the two reactor system, and what first section hydrofining reactor used is base metal catalysts, and what second section reforming reactor used is the noble metal catalyst of anti-sulphur and nitrogen.In the middle of two reactors, the hydrogen stripped tower is set, to take off the hydrogen sulfide (H of first reactor effluent
2S) and ammonia (NH
3), the gas phase series connection of second section and first section, the gas after refining no longer directly enters first section through handling earlier by second section from second section gas that comes out, and makes the hydrogen dividing potential drop of upgrading section be higher than hydrogen dividing potential drop 15 crust (213psi) of refining section.
CN1156752A discloses a kind of two-stage hydrogenation technology of producing fine-quality diesel oil with diesel oil distillate, and this technology has added water washing device between two reactor, remove one section H in the effluent
2S and NH
3First section is base metal catalysts, and second section for containing the base metal catalysts of zeolite.But this method energy consumption is higher, and the washing between two sections easily causes environmental pollution.
The operational path of raising reaction pressure that prior art is mentioned or employing noble metal catalyst, the subject matter of existence is the increase greatly of tooling cost.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology a kind of method of desulfurizing and dearomatizing diesel oil deeply cheaply.
Method provided by the invention comprises: stock oil and hydrogen are mixed into first reactor, contact with catalyst for hydro-upgrading, hydrocracking catalyst or Hydrobon catalyst, and the effluent of first reactor is removed H through hydrogen stripped tower stripping under High Temperature High Pressure
2S, NH
3, the liquid stream behind the stripping is mixed into second reactor with hydrogen again, contacts with conventional Hydrobon catalyst, and the effluent of second reactor enters high-pressure separator, light pressure separator and separation column successively; Separation column is divided into petroleum naphtha and diesel oil distillate with reaction product; With after fresh hydrogen is mixed, separated into two parts is delivered to first reactor and second reactor respectively from high-pressure separator and the isolated hydrogen rich stream of stripping tower.
Method provided by the invention adopts non-precious metal catalyst to remove sulphur, the aromaticity content of diesel raw material under middle pressure, so its cost is lower.
Description of drawings
Accompanying drawing is the methodological principle schematic flow sheet of desulfurizing and dearomatizing diesel oil deeply provided by the present invention.
Embodiment
Method provided by the invention comprises:
(1), stock oil and hydrogen are mixed into first section hydro-upgrading or hydrocracking reactor, contact the hydro-upgrading reaction or the hydrocracking reaction that comprise hydrogenating desulfurization, hydrodenitrification, hydrogenation of olefins are saturated, aromatic hydrogenation is saturated and selective opening reacts with catalyst for hydro-upgrading, hydrocracking catalyst or Hydrobon catalyst;
(2), the effluent of first section reactor is removed H through hydrogen stripped tower stripping under High Temperature High Pressure
2S, NH
3,
(3), the liquid stream behind the stripping is mixed into second section hydrofining reactor with hydrogen again, contact with Hydrobon catalyst, second section refining reaction device effluent enters high-pressure separator, light pressure separator and separation column successively, and separation column is divided into petroleum naphtha and diesel oil distillate with reaction product;
(4), mix with fresh hydrogen, separated into two parts is delivered to first section hydro-upgrading or hydrocracking reactor and second section hydrofining reactor respectively and is proceeded reaction from high-pressure separator and the isolated hydrogen rich stream of stripping tower.
Stock oil in the step (1) is selected from one or more the mixture in catalytic cracking diesel oil, straight-run diesel oil, coker gas oil, the visbreaking diesel oil, its boiling range scope is 180～390 ℃, sulphur content is not more than 3 heavy % in the raw material, and nitrogen content is not more than 0.2 heavy %.
Catalyst for hydro-upgrading in the step (1) is VIB or the VIII family base metal catalysts that contains on unformed aluminum oxide of loading on of a certain amount of zeolite or the silica-alumina supports.Specifically, this catalyzer contains a kind of carrier and the molybdenum and/or tungsten and nickel and/or the cobalt that load on this carrier.In oxide compound and with the catalyzer total amount is benchmark, and the content of molybdenum and/or tungsten is 10～35 heavy % preferred 18～32 heavy % in this hydrogenation catalyst, and the content of nickel and/or cobalt is 1～15 heavy % preferred 3～12 heavy %.Described carrier is made up of aluminum oxide and zeolite, the weight ratio of aluminum oxide and zeolite be 90: 10～50: 50 preferred 90: 10～60: 40.Described aluminum oxide is the aluminum oxide that is composited according to 75: 25～50: 50 weight ratio by little porous aluminum oxide and macroporous aluminium oxide, to be diameter account for the aluminum oxide of total pore volume more than 95% less than the pore volume in 80 holes to wherein little porous aluminum oxide, and macroporous aluminium oxide is that the pore volume in diameter 60～600 holes accounts for the aluminum oxide of total pore volume more than 70%.Described zeolite is selected from one or more in faujusite, mordenite, erionite zeolite, zeolite L, omega zeolite, ZSM-4 zeolite, the Beta zeolite, preferred y-type zeolite, particularly preferred zeolite is that total acid content is 0.02 to less than 0.5 mmole/gram, the y-type zeolite of preferred 0.05～0.2 mmole/gram.
Hydrocracking catalyst in the step (1) is to be carrier with the zeolite, and VIB or VIII family basic metal load on the carrier.
Operational condition in step (1) and (3) is: hydrogen dividing potential drop 2.0～12.0MPa; 300～450 ℃ of temperature of reaction; Liquid hourly space velocity 0.1～20h
-1, hydrogen-oil ratio 300～2000v/v.
Hydrobon catalyst in the step (3) can be conventional diesel oil hydrofining catalyst, and this catalyzer can be VIB or the VIII family base metal catalysts that loads on unformed aluminum oxide or the silica-alumina supports.
Below in conjunction with accompanying drawing method provided by the present invention is further detailed, but not thereby limiting the invention.Accompanying drawing is the methodological principle schematic flow sheet of desulfurizing and dearomatizing diesel oil deeply provided by the present invention, many essential equipment, facility have been omitted among the figure, as process furnace, pump and the gas sweetening measure of high-pressure stripper top etc., but this is known to those of ordinary skills.
The method of hydrotreating flow process of reduction aromatic content of diesel oil provided by the present invention is as follows:
Diesel raw material is after pipeline 1 incoming stock pump 2 boosts to reaction pressure, through pipeline 36 with after hydrogen-rich gas from pipeline 25 mixes, enter first section hydro-upgrading reactor 4 through pipeline 3, by contacting with the catalyst for hydro-upgrading bed, remove impurity such as sulphur in the stock oil and nitrogen, in desulfurization, denitrogenation, the saturated of aromatic ring takes place, and very important saturated back aromatic ring selective opening reaction, this reaction is strong exothermal reaction, need to inject cold hydrogen from pipeline 26, with the conditioned reaction temperature distribution at the reactor beds interlayer.
The effluent of hydro-upgrading reactor 4 is through pipeline 5, with from logistics behind the stripping of pipeline 9 in interchanger 6 after the heat exchange, enter the hydrogen stripped tower 8 of High Temperature High Pressure through pipeline 7, hydrogen enters from 8 ends of hydrogen stripped tower through pipeline 35, logistics behind the stripping through pipeline 9 with from the logistics of pipeline 5 in interchanger 6 after the heat exchange, through pipeline 10 with after hydrogen-rich gas from pipeline 28 mixes, enter second section hydrofining reactor 12 through pipeline 11, the effluent of reactor 12 through pipeline 13 with enter high-pressure separator 14 after water from pipeline 38 mixes, in high-pressure separator, be separated into two bursts of logistics, one is a hydrogen-rich stream, wherein be mainly hydrogen, comprise partial vulcanization hydrogen simultaneously, ammonia and because the light hydrocarbon that cracking produces.The gas on high-pressure stripper top successively through pipeline 30, digester 39 desulfurization after pipeline 40 with after hydrogen-rich stream from pipeline 31 mixes, enter recycle compressor 33 compressions through pipeline 32, and then mix respectively with fresh hydrogen and to loop back reactor 4 through pipeline 25,26 successively, loop back reactor 12 through pipeline 34,37,28,11 and 34,37,29 successively; Another burst logistics enters light pressure separator 16 through pipeline 15 and further removes light hydrocarbon, and the effluent of light pressure separator bottom enters separation column 18 through pipeline 17, and the gas that fractionates out, petroleum naphtha and diesel oil distillate are respectively through pipeline 19,20,21 caterpillars.Because second section what mainly carry out is aromatic hydrogenation reaction, belongs to strong exothermal reaction, needs to inject cold hydrogen to second section reactor beds interlayer from pipeline 29, to improve reaction temperature profile.
The fresh hydrogen of replenishing is after pipeline 22 enters compressor 23 and boosts, and with after loop compression hydrogen from pipeline 34 mixes, separated into two parts is distinguished Returning reactor 4 and reactor 12 through pipeline 24.
The present invention proposes a new operational path, to reach the purpose of under low tooling cost, producing 2 classes or 3 class fine-quality diesel oils.In the new operational path technical process be two sections integrated, set up the High Temperature High Pressure stripping towers in the middle of two reactors; First section employing contains catalyst for hydro-upgrading, hydrocracking catalyst or the Hydrobon catalyst of zeolite, finish the part open loop of the above cyclic hydrocarbon of dicyclo, to improve the speed of second section aromatic hydrogenation, enter high-pressure stripper then and remove hydrogen sulfide and ammonia, with the disadvantageous effect of removal of hydrogen sulfide competitive adsorption to aromatic hydrogenation, thereby for second section aromatic hydrogenation provides The optimum reaction conditions, therefore second section conventional Hydrobon catalyst of employing can reduce aromaticity content significantly in this operational path.Adopt the two-stage process of noble metal catalyst to compare with second section, two sections of this technologies all with the base metal catalysts of routine and simple technical flow more, have advantages such as production cost is low, insensitive to impurity, easy handling.
This technology can in depress, processing catalytic diesel oil, straight-run diesel oil, coker gas oil, visbreaking diesel oil and mix the wet goods raw material are produced the fine-quality diesel oil product that satisfies world's fuel oil standard 2 classes or 3 class diesel oil specification requirements.In addition, because first section employing of this technology is the modifying catalyst that contains zeolite, so doing of charging can suitably relax to about 390 ℃, thereby reach the purpose of increasing output of diesel oil.
The following examples will give further instruction to present method, but therefore not limit present method.
Embodiment 1
Test raw material is catalytic diesel oil A, and first section used catalyst for hydro-upgrading is RIC-1, and second section used Hydrobon catalyst is RN-10, produces by Changling Refinery Chemical Industry Co., Ltd. of China Petrochemical Industry catalyst plant.Stock oil character, processing condition and product property are listed in table 1, table 2 respectively.By table 2 as seen, under than the demulcent operational condition, the product sulphur content is low, can satisfy world's fuel oil standard 2 class diesel oil and 3 class diesel oil specification requirements, and the density of product, aromaticity content and cetane index all satisfy the specification requirement of world's fuel oil standard 2 class diesel oil.
Test raw material is catalytic diesel oil B, and first section used catalyst for hydro-upgrading is RIC-1, and second section used Hydrobon catalyst is RN-10, produces by Changling Refinery Chemical Industry Co., Ltd. of China Petrochemical Industry catalyst plant.Stock oil character, processing condition and product property are listed in table 1, table 2 respectively.By table 2 as seen, the operational condition that this raw material needs is comparatively harsh, and the product sulphur content is low, can satisfy 2 class diesel oil and 3 class diesel oil specification requirements, and the density of product, aromaticity content and cetane index all satisfy the specification requirement of 2 class diesel oil.
Test raw material is catalytic diesel oil C, and first section used hydrocracking catalyst is RT-1, and second section used Hydrobon catalyst is RN-10, produces by Changling Refinery Chemical Industry Co., Ltd. of China Petrochemical Industry catalyst plant.Stock oil character, processing condition and product property are listed in table 3, table 4 respectively.By table 4 as seen, under harsh relatively operational condition, the product sulphur content is low, can satisfy world's fuel oil standard 2 class diesel oil and 3 class diesel oil specification requirements, and the density of product, aromaticity content and cetane index all can satisfy the requirement of world's fuel oil standard 2 class diesel oil.
Test raw material is the mixing oil of catalytic diesel oil and straight-run diesel oil, and first section used hydrocracking catalyst is RT-1, and second section used Hydrobon catalyst is RN-10, produces by Changling Refinery Chemical Industry Co., Ltd. of China Petrochemical Industry catalyst plant.Stock oil character, processing condition and product property are listed in table 3, table 4 respectively.By table 4 as seen, under than the demulcent operational condition, product sulphur content, density, aromaticity content and cetane index all can satisfy the requirement of world's fuel oil standard 3 class diesel oil.
Test raw material and embodiment 1 are all catalytic diesel oil A, and first section used catalyst for hydro-upgrading is RN-10, and second section used Hydrobon catalyst is RN-10, produce by Changling Refinery Chemical Industry Co., Ltd. of China Petrochemical Industry catalyst plant.Processing condition and product property are listed in table 5.By table 5 as seen, under than the demulcent operational condition, the product sulphur content is low, can satisfy world's fuel oil standard 2 class diesel oil and 3 class diesel oil specification requirements, and the density of product, aromaticity content and cetane index all satisfy the specification requirement of world's fuel oil standard 2 class diesel oil.
Table 1
| Embodiment 1 | | |
| Catalytic diesel oil A | Catalytic diesel oil B | |
| Density (20 ℃), g/cm 3 | ????0.8828 | ????0.9130 |
| S，m％ | ????0.64 | ????0.55 |
| N，ppm | ????452 | ????632 |
| Total aromaticity content, m% | ????57.1 | ????63.2 |
| Polycyclic aromatic hydrocarbon content, m% | ????32.2 | ????47.3 |
| Boiling range ASTM D-86, ℃ | ||
| Initial boiling point/10% | ????189/216 | ????215/245 |
| 50％/90％ | ????276/361 | ????294/351 |
| Do | ????383 | ????372 |
| Cetane index D4737 | ????38 | ????32.2 |
Table 2
| Embodiment 1 | | |
| Processing condition | ||
| The hydrogen dividing potential drop, MPa | ????6.4 | ????7.0 |
| Temperature of reaction (first section/second section), ℃ | ????350/350 | ????359/355 |
| Volume space velocity (first section/second section), h -1 | ????1.5/1.5 | ????1.0/1.0 |
| Hydrogen-oil ratio (first section/second section), Nm 3/m 3 | ????500/500 | ????600/600 |
| Diesel product yield, m% | ????95 | ????96 |
| Diesel product character | ||
| Density (20 ℃), g/cm 3 | ????0.8370 | ????0.8450 |
| S，ppm | ????6 | ????21 |
| Total aromaticity content, m% | ????21 | ????24 |
| Polycyclic aromatic hydrocarbon content, m% | ????1.5 | ????2.5 |
| Boiling range ASTM D-86, ℃ | ||
| Initial boiling point/10% | ????194/210 | ????206/229 |
| 50％/90％ | ????268/352 | ????274/343 |
| Do | ????375 | ????369 |
| Cetane index D4737 | ????51 | ????50.4 |
Table 3
| | | |
| Catalytic diesel oil C | Catalytic diesel oil+straight-run diesel oil | |
| Density (20 ℃), g/cm 3 | ????0.9097 | ?0.8660 |
| ?S，m％ | ????0.54 | ?0.47 |
| ?N，ppm | ????1019 | ?270 |
| Total aromaticity content, m% | ????56.6 | ?44.6 |
| Polycyclic aromatic hydrocarbon content, m% | ????45.3 | ?24.3 |
| Boiling range ASTM D-86, ℃ | ||
| Initial boiling point/10% | ????226/259 | ?193/221 |
| 50％/90％ | ????311/359 | ?275/339 |
| Do | ????374 | ?362 |
| Cetane index D4737 | ????34.8 | ?43.1 |
Table 4
| | | |
| Processing condition | ||
| The hydrogen dividing potential drop, MPa | ????7.8 | ????5.0 |
| Temperature of reaction (first section/second section), ℃ | ????364/355 | ????350/350 |
| Volume space velocity (first section/second section), h -1 | ????1.0/1.0 | ????2.0/1.5 |
| Hydrogen-oil ratio (first section/second section), Nm 3/m 3 | ????600/600 | ????500/600 |
| Diesel product yield, m% | ????97 | ????92 |
| Diesel product character | ||
| Density (20 ℃), g/cm 3 | ????0.8490 | ????0.8240 |
| S，ppm | ????15 | ????12 |
| Total aromaticity content, m% | ????20 | ????13.6 |
| Polycyclic aromatic hydrocarbon content, m% | ????1.5 | ????0.9 |
| Boiling range ASTM D-86, ℃ | ||
| Initial boiling point/10% | ????210/238 | ????189/205 |
| 50％/90％ | ????289/350 | ????254/332 |
| Do | ????370 | ????360 |
| Cetane index D4737 | ????51.9 | ????52.5 |
Table 5
| | |
| Processing condition | |
| The hydrogen dividing potential drop, MPa | ????6.4 |
| Temperature of reaction (first section/second section), ℃ | ????350/350 |
| Volume space velocity (first section/second section), h -1 | ????1.0/1.0 |
| Hydrogen-oil ratio (first section/second section), Nm 3/m 3 | ????500/500 |
| Diesel product yield, m% | ????98 |
| Diesel product character | |
| Density (20 ℃), g/cm 3 | ????0.8288 |
| S，ppm | ????12 |
| Total aromaticity content, m% | ????16.9 |
| Polycyclic aromatic hydrocarbon content, m% | ????1.5 |
| Boiling range ASTM D-86, ℃ | |
| Initial boiling point/10% | ????159/208 |
| 50％/90％ | ????257/350 |
| Do | ????381 |
| Cetane index D4737 | ????51.5 |
Claims (7)
1, a kind of method of desulfurizing and dearomatizing diesel oil deeply comprises:
(1), stock oil and hydrogen is mixed into first reactor, contact with catalyst for hydro-upgrading, hydrocracking catalyst or Hydrobon catalyst;
(2), the effluent of first reactor is removed H through hydrogen stripped tower stripping under High Temperature High Pressure
2S, NH
3,
(3), the liquid stream behind the stripping is mixed into second reactor with hydrogen again, contact with Hydrobon catalyst, the effluent of second reactor enters high-pressure separator, light pressure separator and separation column successively, and separation column is divided into petroleum naphtha and diesel oil distillate with reaction product;
(4), mix with fresh hydrogen, separated into two parts is delivered to first reactor respectively and second reactor is proceeded reaction from high-pressure separator and the isolated hydrogen rich stream of stripping tower.
2, according to the method for claim 1, it is characterized in that stock oil in the step (1) is selected from one or more the mixture in catalytic cracking diesel oil, straight-run diesel oil, coker gas oil, the visbreaking diesel oil, its boiling range scope is 180～390 ℃, sulphur content is not more than 3 heavy % in the raw material, and nitrogen content is not more than 0.2 heavy %.
3,, it is characterized in that the catalyst for hydro-upgrading in the step (1) is VIB or the VIII family base metal catalysts that contains on unformed aluminum oxide of loading on of zeolite or the silica-alumina supports according to the method for claim 1.
4, according to the method for claim 3, it is characterized in that in oxide compound and be benchmark that the content of described catalyst for hydro-upgrading molybdenum and/or tungsten is 10～35 heavy % with the catalyzer total amount, the content of nickel and/or cobalt is 1～15 heavy %; Described carrier is made up of aluminum oxide and zeolite, the weight ratio of aluminum oxide and zeolite is 90: 10～50: 50, described aluminum oxide is the aluminum oxide that is composited according to 75: 25～50: 50 weight ratio by little porous aluminum oxide and macroporous aluminium oxide, to be diameter account for the aluminum oxide of total pore volume more than 95% less than the pore volume in 80 holes to wherein little porous aluminum oxide, and macroporous aluminium oxide is that the pore volume in diameter 60～600 holes accounts for the aluminum oxide of total pore volume more than 70%.
5, according to the method for claim 1, it is characterized in that the hydrocracking catalyst in the step (1) is to be carrier with the zeolite, VIB or VIII family basic metal load on the carrier.
6, according to the method for claim 1, it is characterized in that the Hydrobon catalyst in the step (3) can be conventional diesel oil hydrofining catalyst, this catalyzer can be VIB or the VIII family base metal catalysts that loads on unformed aluminum oxide or the silica-alumina supports.
7,, it is characterized in that the operational condition in step (1) and (3) is: hydrogen dividing potential drop 2.0～12.0MPa according to the method for claim 1; 300～450 ℃ of temperature of reaction; Liquid hourly space velocity 0.1～20 hour
-1, hydrogen-oil ratio 300～2000v/v.
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