CN1493667A - Hydrocracking process for maximally producing middle distillate - Google Patents
Hydrocracking process for maximally producing middle distillate Download PDFInfo
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Abstract
A hydrocracking process for increasing the output of intermediate fractional oil to maximum features that the hydrorefined heavy petroleum hydrocarbon is contacted first with the beta-zeolite hydrocracking catalyst for cracking the most of raw material and then with the Y-zeolite hydrocracking catalyst for cracking the rest of raw material. Its advantages are high selectivity and low content of olefin in intermediate fractional oil.
Description
Technical field
The present invention relates to a kind of one-stage serial hydrocracking technology, produce the one-stage serial technology of intermediate oil especially for maximum.
Background technology
Hydrocracking process is a kind of important processing means of heavy feed stock lighting, particularly obtains the main method of cleaning boat coal and diesel oil from inferior raw material.The process from the amorphous type hydrocracking catalyst to the zeolite type hydrocracking catalyst has been experienced in the development of hydrocracking catalyst.
The zeolite that hydrocracking catalyst is commonly used at present mainly is a y-type zeolite.Y zeolite type hydrocracking catalyst has good open loop activity, is particularly suitable for handling high aromatic hydrocarbons heavy feed stock, products obtained therefrom quality height.But Y zeolite type hydrocracking catalyst is on certain activity level, the raising of middle distillates oil selectivity is limited, because though the supercage structure of Y zeolite helps cyclic hydrocarbon and polycyclic aromatic hydrocarbons open loop cracking, also can make the further cracking of chain hydrocarbon of opening and produce too much small molecules and suppressed middle distillates oil selectivity further raising.
An other class zeolite such as β zeolite have begun to use on hydrocracking catalyst at present.The duct characteristics of β zeolite make it to paraffinic hydrocarbons to select the shape selectivity outstanding relatively, thereby in scission reaction, mainly finish fracture, its straight hole road reactant is in time shifted out and suppressed the excessive fragmentation of reaction and improved middle distillates oil selectivity simultaneously to the chain hydrocarbon.But because the pore structure of β zeolite restriction, the open loop of aromatic hydrocarbons or polynuclear hydrocarbon is active, and Y zeolite is low relatively, thereby when handling high aromaticity content raw material inferior, its quality product is good not as Y zeolite type hydrocracking catalyst, shows that the aromatic hydrocarbons of cut products in boat coal, the diesel oil etc. is higher relatively.
US4820402 discloses a kind of hydrocracking catalyst, has mentioned the β zeolite, and this patent thinks, in order to improve middle distillates oil selectivity and to reduce the hydrogen consumption, and the silica molecular ratio at least 50: 1 of catalyzer mesolite component, general 100: 1, even 200: 1.This patent catalyzer is used to handle Arabic VGO, and under the situation that control 60v% transforms, middle distillates oil selectivity is 45～65v%.This patent has adopted high silica alumina ratio β zeolite, thereby has drawn different high silica alumina ratio zeolite (SiO
2: Al
2O
3=200: 1) middle distillates oil selectivity that is used for this catalyzer is in proper order: ZSM-20＞β＞Y type.Obviously select the shape zeolite for what have a straight hole road, here the hydroisomerizing performance of β zeolite is not well utilized, and the aromaticity content of product is higher, is not suitable for the requirement of environmental regulation.
US6261441 discloses a kind of hydrotreatment flow process that adopts isolation cycle, this flow process is at first depressed at 7000kPa hydrogen branch and is adopted a kind of zeolite type hydrocracking catalyst cracking high to aromatic hydrocarbons cracking selectivity, Y zeolite type hydrocracking catalyst for example, fractionation then, at the bottom of the separation column of hydrocracking section oil enter dewaxing section adopt a kind of have hydroisomerizing and or the catalyst treatment of shape slective cracking, and then fractionation, oil or loop back the hydrocracking section at the bottom of the separation column of dewaxing section is not if circulate just as lubricant base.Wherein dewaxing section use a kind of to normal paraffin have hydroisomerizing and to a certain degree cracking performance the β zeolite or a kind ofly have the catalyzer of selecting the shape selective cracking process or both use jointly.Though used Y and beta-zeolite catalyst respectively in front and back, the cracking load is born by the Y zeolite catalyzer substantially, and the raising of middle oily productive rate is restricted, and has adopted the complicated and two sections higher flow processs of running cost of flow process.
US5536687 discloses a kind of hydrocracking catalyst that is used for producing from heavy feed stock light ends such as gasoline and intermediate oil, and the characteristics of this catalyzer have been to use the composite zeolite that comprises β and Y zeolite as its cracking component.Because β zeolite and Y zeolite respectively have its suitable reactive material kind, strong as Y zeolite to the open loop ability of aromatic hydrocarbons, the β zeolite is strong to the selective cracking function of the isomery of the disconnected side chain of aromatic hydrocarbons, chain hydrocarbon and long carbochain hydrocarbon, and along the reagent flow direction, the relative concentration of the dissimilar materials of different axial locations is different, thereby plural components can not make different components be in the peak concentration place of its suitable reactive material, reduced the utilising efficiency of catalyzer.
Summary of the invention
At the deficiencies in the prior art, the invention provides the raising hydrocracking middle distillates oil selectivity that a kind of technology is simple, adaptation is strong and improve the particularly hydrogenated oil cracking technological process of the maximum production middle runnings of diesel oil cold flow properties of product property.
Technological process of the present invention is: the heavy crude hydro carbons at first contacts with Hydrobon catalyst under the hydrofining condition with hydrogen, effluent contacts with hydrocracking catalyst under hydrocracking condition then, and the hydrocracking reaction product obtains petroleum naphtha, middle runnings and unconverted tail oil after fractionation.Wherein hydrocracking catalyst comprises two types of catalyzer: contain first hydrocracking catalyst and second hydrocracking catalyst that contains Y zeolite of β zeolite, unconverted tail oil circulation contacts with hydrocracking catalyst.The volume ratio of first hydrocracking catalyst and second hydrocracking catalyst is 1～5: 1, is preferably 1～3: 1.
The β zeolite content of first hydrocracking catalyst of the above-mentioned β of containing zeolite is 10-40wt%, and other component and content technology are routinely determined.The β zeolite has following feature: SiO
2/ Al
2O
3Mol ratio is 20-150, and the secondary pore pore volume of 2～10nm accounts for 30%～60% of total pore volume, specific surface 500-750m
2/ g, infrared acidity 0.25-0.50mmol/g.
The above-mentioned Y zeolite content that contains second hydrocracking catalyst of Y zeolite is 5-30wt%, and other component and content technology are routinely determined.Y zeolite has following feature: SiO
2/ Al
2O
3Mol ratio is 5-20, and the secondary pore pore volume of 2～10nm accounts for 30%～60% of total pore volume, specific surface 500-750m
2/ g, infrared acidity 0.25-0.50mmol/g.
Technology of the present invention is according to heavy crude hydro carbons hydrocracking reaction characteristics, and β zeolite and Y zeolite catalysis characteristics, the suitable hydrocracking catalyst that contains β zeolite and Y zeolite respectively is used to select two kinds of character for use, finish the most cracking of hydrocarbon material by the β zeolite catalyst that occupies the majority, guaranteed the selectivity of intermediate oil, finish the cracking of small part then by the low acidity Y zeolite catalyst contact that occupies the minority, particularly carry out the ring-opening reaction of aromatic hydrocarbons, compensate the deficiency of beta-zeolite catalyst open-loop performance, reduced the aromaticity content of the finished product.The catalyzer that contains Y zeolite places and contains after the β zeolite, makes it to be in the range of profitability of aromatic hydrocarbons competitive adsorption, has improved the utilization ratio of catalyzer.Technology of the present invention has not only improved the selectivity of intermediate oil, and the aromaticity content that has also improved product property, particularly intermediate oil greatly reduces greatly, meets the requirement of increasingly stringent environmental regulation.In addition, the present invention adopts one-stage serial extinction recycle operation flow process, and process is simple, and running cost is low, purpose product yield height.
Embodiment
The inventive method adopts one-stage serial recycle to extinction hydrocracking process, comprises two reactors, i.e. hydrofining reactor and hydrocracking reactor.Hydrofining reactor filling Hydrobon catalyst is used for removing most sulphur, nitrogen poisonous substance before material enters cracking zone.Hydrocracking reactor filling β zeolite type first hydrocracking catalyst and second kind of hydrocracking catalyst of Y zeolite type, the method for filling are included in the branch bed filling in the reactor and are seated in two respectively independently in the cracking case.
The handled petroleum hydrocarbon material of hydrocracking process is boiling range 250-600 ℃ heavy crude hydrocarbon material, for example VGO, CGO, HGO, LGO or their mixture.
The hydrofining section can be selected common hydrorefining catalyst for heavy oil for use, 3936 catalyzer of producing as the Fushun Petrochemical Company catalyst plant, 3996 catalyzer etc., and the hydrofining operational condition is conventional hydrofining condition.
Hydrocracking condition belongs to the routine operation condition of hydrocracking, in the presence of hydrogen, stock oil is contacted with catalyzer, system response pressure 5～20MPa, hydrogen-oil ratio 100～5000,340～420 ℃ of cracking zone temperature of reaction, cracking cumulative volume air speed is generally 0.6-3.0hr
-1, best 0.8-2.0hr
-1Hydrocracking catalyst of the present invention is used for the oil type hydrocracking process, be particularly suitable for treatment of heavy hydrocarbon material, the boiling range scope of heavy hydrocarbon material is at 200-600 ℃, generally at 250-550 ℃, hydrocracking catalyst of the present invention is when handling common VGO, reaction conditions is pressure 7～18MPa preferably, hydrogen-oil ratio 500～2500,350～400 ℃ of cracking zone temperature of reaction.
According to the difference of filling ratio, β zeolite type first hydrocracking catalyst is born 50-90wt% petroleum hydrocarbon material cracking load, and Y zeolite type second hydrocracking catalyst is only born 10-50wt% cracking load.Per pass conversion is 50-80wt%.
First hydrocracking catalyst is formed and is comprised: (a) β zeolite 10-40wt%; (b) macropore refractory oxide 10-70wt%; (c) aperture aluminum oxide 0-30wt%; (d) group vib metal oxide 10-40wt%; (e) VIII metal oxide 1-10wt%.Second hydrocracking catalyst is formed and is comprised: (a) Y zeolite 5-30wt%; (b) macropore refractory oxide 10-80wt%; (c) aperture aluminum oxide 0-30wt%; (d) group vib metal oxide 10-40wt%; (e) VIII metal oxide 1-10wt%.The group vib metal oxide mainly comprises the oxide compound of tungsten, molybdenum, and the VIII family metal oxide mainly comprises the oxide compound of nickel, cobalt.The macropore refractory oxide mainly comprises macroporous aluminium oxide (pore volume 0.8～1.5ml/g, specific surface 300～500m
2/ g), macropore sial (pore volume 0.8～1.5ml/g, specific surface 350～600m
2/ g, silica weight content 20%～60%) etc., the pore volume 0.4～0.8ml/g of little porous aluminum oxide, specific surface 150～300m
2/ g.Catalyzer adopts conventional immersion process for preparing.Catalyst specific surface 180-300m
2/ g, pore volume 0.25-0.45ml/g.
In industrial production, the operating method of one-stage serial technology mainly can be divided into recycle to extinction and once pass through.One-through design is that unconverted tail oil is got rid of raw material as downstream unit outward.Generally speaking, unconverted tail oil mainly is used as the charging of lubricant base and preparing ethylene by steam cracking.The recycle to extinction mode is that maximum obtains intermediate oil by hydrocracking reactor is squeezed in unconverted tail oil circulation.
Embodiment
This process program is handled a kind of heavy vacuum gas oil VGO, and this petroleum hydrocarbon material main character is: proportion 0.9021cm
3/ g, 380 ℃-550 ℃ of boiling ranges, carbon residue 0.20wt%, sulphur 1.6wt%, nitrogen 1800 μ g/g.
This programme has two reactors, comprises hydrofining reactor R1 and hydrocracking reactor R2, two reactors in series uses and a shared cover recycle hydrogen system, adopt one-stage serial recycle to extinction technical process.The 3996 heavy-oil hydrogenation catalyst for refining that hydrofining reactor R1 filling Fushun Petrochemical Company catalyst plant is produced.The hydrofining operational condition is: pressure 15MPa, 375 ℃ of average bed temperatures, volume space velocity 0.8hr during feeding liquid
-1, hydrogen to oil volume ratio 800.The treated oil nitrogen content is generally at 3～8 μ g/g.
The composition and the character that contain first hydrocracking catalyst of β zeolite: A1, A2, A3.
A1：
Get β zeolite (SiO
2/ Al
2O
3The secondary pore pore volume that is 40,2～10nm accounts for 35% of total pore volume, specific surface 580m2/g, infrared acidity 0.21mmol/g) 5.6g, amorphous aluminum silicide (specific surface 450m
2/ g, SiO
255wt%, pore volume 0.9ml/g) 53.8g mixes, and adds molten little porous aluminum oxide (the specific surface area 240m of 42.9g of dilute nitric acid solution glue by the concentration 3.3% of 160ml
2/ g, pore volume are 0.42ml/g) tackiness agent that obtains, continue to mix and pinch up to becoming paste, extruded moulding, institute's moulding bar that obtains be 110 ℃ of dryings 12 hours down, 500 ℃ activate 4 hours and make activated carrier after.Flood the carrier of above-mentioned preparation again with the W-Ni co-impregnated solution, again 110 ℃ of dryings 8 hours, and 500 ℃ of activation 3 hours.Catalyzer finally consists of: β zeolite 10wt%, amorphous aluminum silicide 35wt%, aluminum oxide 30wt%, nickel oxide 7.5wt%, Tungsten oxide 99.999 22.5wt%.Catalyst specific surface 205m
2/ g, pore volume 0.34ml/g.
A2：
Get β zeolite (SiO
2/ Al
2O
3The secondary pore pore volume that is 60,2～10nm accounts for 51% of total pore volume, specific surface 600m
2/ g, infrared acidity 0.19mmol/g) 11.1g, amorphous aluminum silicide (specific surface 490m
2/ g, SiO
245wt%, pore volume 1.0ml/g) 69.2g mixes, and slowly adds molten little porous aluminum oxide (the specific surface area 240m of 21.4g of dilute nitric acid solution glue by the concentration 3.3% of 110ml under the situation that continues to roll
2/ g, pore volume are 0.42ml/g) tackiness agent that obtains, continue to mix and pinch up to becoming paste, extruded moulding, institute's moulding bar that obtains be 110 ℃ of dryings 12 hours down, 500 ℃ activate 4 hours and make activated carrier after.Again with W-Ni co-impregnated solution dipping, again 110 ℃ of dryings 8 hours, and 500 ℃ of activation 3 hours.Catalyzer finally consists of: β zeolite 15wt%, amorphous aluminum silicide 45wt%, aluminum oxide 15wt%, nickel oxide 7.5wt%, Tungsten oxide 99.999 22.5wt%.Catalyst specific surface 230m
2/ g, pore volume 0.33ml/g.
A3：
Get β zeolite (SiO
2/ Al
2O
3The secondary pore pore volume that is 30,2～10nm accounts for 38% of total pore volume, specific surface 600m
2/ g, infrared acidity 0.31mmol/g) 33.3g, amorphous aluminum silicide (specific surface 490m
2/ g, SiO
245wt%, pore volume 1.0ml/g) 38.5g mixes, and slowly adds molten little porous aluminum oxide (the specific surface area 240m of 21.4g of dilute nitric acid solution glue by the concentration 3.3% of 90ml under the situation that continues to roll
2/ g, pore volume are 0.42ml/g) tackiness agent that obtains, continue to mix and pinch up to becoming paste, extruded moulding, institute's moulding bar that obtains be 110 ℃ of dryings 12 hours down, 500 ℃ activate 4 hours and make activated carrier after.Again with W-Ni co-impregnated solution dipping, again 110 ℃ of dryings 8 hours, and 500 ℃ of activation 3 hours.Catalyzer finally consists of: β zeolite 30wt%, amorphous aluminum silicide 25wt%, aluminum oxide 15wt%, nickel oxide 7.5wt%, Tungsten oxide 99.999 22.5wt%.Catalyst specific surface 235m
2/ g, pore volume 0.32ml/g.
The composition and the character that contain second hydrocracking catalyst of Y zeolite: B1, B2, B3.
B1：
Take by weighing amorphous aluminum silicide (specific surface 520m
2/ g, SiO
235wt%, pore volume 1.2ml/g) 102.6g and Y zeolite 33.5g (SiO
2/ Al
2O
3Be 9, specific surface 650m
2/ g, infrared acidity 0.45mmol/g, the secondary pore pore volume of 2～10nm account for total pore volume 42%), add behind the mixing 200g (adding rare nitric acid peptization preparation) tackiness agent by the little porous aluminum oxide of 71.4g pore volume 0.42ml/g roll agglomerating after, put into the banded extruder extruded moulding after, 110 ℃ of dryings 10 hours, 500 ℃ of activation made carrier in 4 hours, again with Mo-Ni steeping fluid dipping altogether, then 110 ℃ of dryings 12 hours, and 500 ℃ of activation 3 hours.Catalyzer finally consists of: amorphous aluminum silicide 35wt%, zeolite 5wt%, aluminum oxide 25wt%, nickel oxide 5wt%, molybdenum oxide 20wt%.Catalyst specific surface 210m
2/ g, pore volume 0.32ml/g.
B2：
Take by weighing amorphous aluminum silicide (specific surface 490m
2/ g, SiO
245wt%, pore volume 1.0ml/g) 88.7g and Y zeolite 45.4g (SiO
2/ Al
2O
3Be 12, specific surface 680m
2/ g, infrared acidity 0.41mmol/g, the secondary pore pore volume of 2～10nm account for total pore volume 44%), the tackiness agent that adds 160g (adding the preparation of rare nitric acid peptization by the little porous aluminum oxide of 57.1g pore volume 0.42ml/g) behind the mixing roll agglomerating after, put into the banded extruder extruded moulding after, 110 ℃ of dryings 10 hours, after 500 ℃ of activation made carrier S B in 4 hours, again with W-Ni steeping fluid dipping altogether, then 110 ℃ of dryings 12 hours, and 500 ℃ of activation 3 hours.Catalyzer finally consists of: sial 30wt%, zeolite 10wt%, aluminum oxide 20wt%, nickel oxide 7.5wt%, Tungsten oxide 99.999 22.5wt%.Catalyst specific surface 210m
2/ g, pore volume 0.31ml/g.
B3：
Take by weighing amorphous aluminum silicide (specific surface 450m
2/ g, SiO
255wt%, pore volume 0.9ml/g) 64.7g and Y zeolite 80.5g (SiO
2/ Al
2O
3Be 15, specific surface 690m
2/ g, infrared acidity 0.40mmol/g, the secondary pore pore volume of 2～10nm account for total pore volume 45%), the tackiness agent that adds 120g (adding the preparation of rare nitric acid peptization by the little porous aluminum oxide of 42.0g pore volume 0.42ml/g) behind the mixing roll agglomerating after, put into the banded extruder extruded moulding after, 110 ℃ of dryings 10 hours, after 500 ℃ of activation made carrier S C in 4 hours, again with W-Ni steeping fluid dipping altogether, then 110 ℃ of dryings 12 hours, and 500 ℃ of activation 3 hours.Catalyzer finally consists of: sial 20wt%, zeolite 30wt%, aluminum oxide 15wt%, nickel oxide 7.5wt%, Tungsten oxide 99.999 22.5wt%.Catalyst specific surface 240m
2/ g, pore volume 0.30ml/g.
Example 1～4: this process program operational condition: reaction pressure 15MPa, hydrogen-oil ratio 1200 adopts＞370 ℃ of extinction recycle operation modes.Control＜350 ℃ of about 70wt% of cut per pass conversion.It is to obtain divided by the liquid yield that has transformed (100 deduct tail oil) by intermediate oil (rocket engine fuel and/or diesel oil distillate) yield that middle distillates oil selectivity calculates.
Comparative example
Comparative example is a kind of typical one-stage serial hydrocracking technology, and the hydrocracking reactor filling is with a kind of hydrocracking reactor of A2 catalyzer in other words.The raw material of handling is the same with example with the basic technology operational condition.
The scheme ground of technology of the present invention and single β zeolite type hydrocracking catalyst is right, and the aromaticity content of intermediate oil reduces greatly, has improved quality product.
| Scheme | Comparative example | Example 1 | Example 2 | Example 3 | Example 4 |
| Catalyst type | ????A2 | ????A3∶B1 | ????A2∶B2 | ????A2∶B3 | ????A1∶B3 |
| Catalyst proportion | ????/ | ????1∶1 | ????2∶1 | ????3∶1 | ????4∶1 |
| Hydrocracking section cumulative volume air speed, hr -1 | ????1.3 | ????1.3 | ????1.3 | ????1.3 | ????1.3 |
| The cracking zone medial temperature, ℃ | ????384 | ????376 | ????380 | ????378 | ????382 |
| Middle distillates oil selectivity, % | ????72.1 | ????66.8 | ????68.2 | ????69.6 | ????71.0 |
| The rocket engine fuel smoke point, mm | ????25 | ????29 | ????29 | ????27 | ????27 |
| Rocket engine fuel aromatic hydrocarbons, wt% | ????9.1 | ????4.4 | ????5.6 | ????6.1 | ????7.5 |
| Condensation point of diesel oil, ℃ | ????-28 | ????-19 | ????-21 | ????-24 | ????-26 |
| Arylhydrocarbon in diesel oil, wt% | ????32 | ????22 | ????25 | ????26 | ????28 |
Claims (10)
1, a kind of maximum is produced the hydrocracking process of intermediate oil, the heavy crude hydro carbons at first contacts with Hydrobon catalyst under the hydrofining condition with hydrogen, effluent contacts with hydrocracking catalyst under hydrocracking condition then, the hydrocracking reaction product obtains petroleum naphtha after fractionation, middle runnings and unconverted tail oil, it is characterized in that described hydrocracking catalyst comprises two types of catalyzer: first hydrocracking catalyst and second hydrocracking catalyst that contains Y zeolite that contain the β zeolite, unconverted tail oil circulation contacts with hydrocracking catalyst, and the volume ratio of first hydrocracking catalyst and second hydrocracking catalyst is 1～5: 1.
2, according to the described hydrocracking process of claim 1, the volume ratio that it is characterized in that described first hydrocracking catalyst and second hydrocracking catalyst is 1～3: 1.
3, according to the described hydrocracking process of claim 1, the β zeolite content that it is characterized in that described first hydrocracking catalyst is 10-40wt%, and the β zeolite has following feature: SiO
2/ Al
2O
3Mol ratio is 20-150, and the secondary pore pore volume of 2～10nm accounts for 30%～60% of total pore volume, specific surface 500-750m
2/ g, infrared acidity 0.25-0.50mmol/g.
4, according to the described hydrocracking process of claim 1, the Y zeolite content that it is characterized in that described second hydrocracking catalyst is 5-30wt%, and Y zeolite has following feature: SiO
2/ Al
2O
3Mol ratio is 5-20, and the secondary pore pore volume of 2～10nm accounts for 30%～60% of total pore volume, specific surface 500-750m
2/ g, infrared acidity 0.25-0.50mmol/g.
5,, it is characterized in that described heavy crude hydro carbons is boiling range 250-600 ℃ a heavy crude hydrocarbon material according to the described hydrocracking process of claim 1.
6,, it is characterized in that described first hydrocracking catalyst composition comprises: (a) β zeolite 10-40wt% according to the described hydrocracking process of claim 1; (b) macropore refractory oxide 10-70wt%; (c) aperture aluminum oxide 0-30wt%; (d) group vib metal oxide 10-40wt%; (e) VIII metal oxide 1-10wt%.
7,, it is characterized in that described second hydrocracking catalyst composition comprises: (a) Y zeolite 5-30wt% according to the described hydrocracking process of claim 1; (b) macropore refractory oxide 10-80wt%; (c) aperture aluminum oxide 0-30wt%; (d) group vib metal oxide 10-40wt%; (e) VIII metal oxide 1-10wt%.
8, according to claim 6 or 7 described hydrocracking process, it is characterized in that described group vib metal oxide comprises the oxide compound of tungsten, molybdenum, the VIII family metal oxide comprises the oxide compound of nickel, cobalt, and the macropore refractory oxide comprises aluminum oxide, sial, catalyst specific surface 180-300m
2/ g, pore volume 0.25-0.45ml/g.
9, according to the described hydrocracking process of claim 1, it is characterized in that described hydrocracking condition is in the presence of hydrogen, stock oil is contacted with catalyzer, system response pressure 5～20MPa, hydrogen-oil ratio 100～5000,340～420 ℃ of temperature of reaction, cracking cumulative volume air speed is 0.6-3.0hr
-1
10, according to the described hydrocracking process of claim 1, when it is characterized in that described heavy crude class class is VGO, the hydrocracking reaction condition is pressure 7～18MPa, hydrogen-oil ratio 500～2500,350～400 ℃ of temperature of reaction, cracking cumulative volume air speed is 0.8-2.0hr
-1
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| CN100345945C (en) * | 2004-10-29 | 2007-10-31 | 中国石油化工股份有限公司 | Two-stage hydrocracking method for increasing yield of middle distillate oil |
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- 2002-11-02 CN CN 02144546 patent/CN1202216C/en not_active Expired - Lifetime
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| CN101395253B (en) * | 2006-03-06 | 2013-03-13 | 新日本石油株式会社 | Method of wax hydrocracking |
| CN103429709A (en) * | 2011-03-23 | 2013-12-04 | 沙特***石油公司 | Cracking system and process integrating hydrocracking and fluidized catalytic cracking |
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| CN115646540A (en) * | 2022-10-24 | 2023-01-31 | 山东公泉化工股份有限公司 | Composite hydrocracking catalyst, preparation method thereof and preparation method of transformer oil |
| CN115646540B (en) * | 2022-10-24 | 2023-08-11 | 山东公泉化工股份有限公司 | Composite hydrocracking catalyst, preparation method thereof and preparation method of transformer oil |
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