CN104152179B - A kind of production method of high boiling aromatic hydrocarbon solvent oil - Google Patents
A kind of production method of high boiling aromatic hydrocarbon solvent oil Download PDFInfo
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- 238000009835 boiling Methods 0.000 title claims abstract description 46
- 150000004945 aromatic hydrocarbons Chemical class 0.000 title claims abstract description 34
- 239000002904 solvent Substances 0.000 title claims abstract description 30
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 15
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 31
- 150000001875 compounds Chemical class 0.000 claims abstract description 19
- LKTZODAHLMBGLG-UHFFFAOYSA-N alumanylidynesilicon;$l^{2}-alumanylidenesilylidenealuminum Chemical compound [Si]#[Al].[Si]#[Al].[Al]=[Si]=[Al] LKTZODAHLMBGLG-UHFFFAOYSA-N 0.000 claims abstract description 14
- 238000000926 separation method Methods 0.000 claims abstract description 14
- 229910000476 molybdenum oxide Inorganic materials 0.000 claims abstract description 12
- 229910000480 nickel oxide Inorganic materials 0.000 claims abstract description 12
- QGLKJKCYBOYXKC-UHFFFAOYSA-N nonaoxidotritungsten Chemical compound O=[W]1(=O)O[W](=O)(=O)O[W](=O)(=O)O1 QGLKJKCYBOYXKC-UHFFFAOYSA-N 0.000 claims abstract description 12
- PQQKPALAQIIWST-UHFFFAOYSA-N oxomolybdenum Chemical compound [Mo]=O PQQKPALAQIIWST-UHFFFAOYSA-N 0.000 claims abstract description 12
- GNRSAWUEBMWBQH-UHFFFAOYSA-N oxonickel Chemical compound [Ni]=O GNRSAWUEBMWBQH-UHFFFAOYSA-N 0.000 claims abstract description 12
- 229910001392 phosphorus oxide Inorganic materials 0.000 claims abstract description 12
- 239000002994 raw material Substances 0.000 claims abstract description 12
- VSAISIQCTGDGPU-UHFFFAOYSA-N tetraphosphorus hexaoxide Chemical compound O1P(O2)OP3OP1OP2O3 VSAISIQCTGDGPU-UHFFFAOYSA-N 0.000 claims abstract description 12
- 229910001930 tungsten oxide Inorganic materials 0.000 claims abstract description 12
- 239000003054 catalyst Substances 0.000 claims abstract description 11
- 238000004904 shortening Methods 0.000 claims abstract description 9
- 238000000034 method Methods 0.000 claims abstract description 6
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 4
- 239000004480 active ingredient Substances 0.000 claims abstract description 3
- 239000003921 oil Substances 0.000 claims description 69
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 21
- 229910052739 hydrogen Inorganic materials 0.000 claims description 21
- 239000001257 hydrogen Substances 0.000 claims description 21
- 238000002156 mixing Methods 0.000 claims description 11
- 238000006243 chemical reaction Methods 0.000 claims description 9
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 8
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 8
- 229910052814 silicon oxide Inorganic materials 0.000 claims description 8
- QGJOPFRUJISHPQ-UHFFFAOYSA-N Carbon disulfide Chemical compound S=C=S QGJOPFRUJISHPQ-UHFFFAOYSA-N 0.000 claims description 5
- 238000009903 catalytic hydrogenation reaction Methods 0.000 claims description 4
- 238000010792 warming Methods 0.000 claims description 4
- 230000004913 activation Effects 0.000 claims description 3
- 238000004073 vulcanization Methods 0.000 claims description 2
- 239000007788 liquid Substances 0.000 description 11
- 238000004821 distillation Methods 0.000 description 10
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 9
- 239000000047 product Substances 0.000 description 9
- 239000003039 volatile agent Substances 0.000 description 6
- 239000000470 constituent Substances 0.000 description 5
- 238000001833 catalytic reforming Methods 0.000 description 3
- 239000003502 gasoline Substances 0.000 description 3
- DSNHSQKRULAAEI-UHFFFAOYSA-N 1,4-Diethylbenzene Chemical compound CCC1=CC=C(CC)C=C1 DSNHSQKRULAAEI-UHFFFAOYSA-N 0.000 description 2
- QPUYECUOLPXSFR-UHFFFAOYSA-N 1-methylnaphthalene Chemical compound C1=CC=C2C(C)=CC=CC2=C1 QPUYECUOLPXSFR-UHFFFAOYSA-N 0.000 description 2
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 description 2
- NIQCNGHVCWTJSM-UHFFFAOYSA-N Dimethyl phthalate Chemical compound COC(=O)C1=CC=CC=C1C(=O)OC NIQCNGHVCWTJSM-UHFFFAOYSA-N 0.000 description 2
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- 239000004411 aluminium Substances 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- 229910021417 amorphous silicon Inorganic materials 0.000 description 2
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 description 2
- 229910052794 bromium Inorganic materials 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000002816 fuel additive Substances 0.000 description 2
- 239000003209 petroleum derivative Substances 0.000 description 2
- AFZZYIJIWUTJFO-UHFFFAOYSA-N 1,3-diethylbenzene Chemical compound CCC1=CC=CC(CC)=C1 AFZZYIJIWUTJFO-UHFFFAOYSA-N 0.000 description 1
- PFRUBEOIWWEFOL-UHFFFAOYSA-N [N].[S] Chemical compound [N].[S] PFRUBEOIWWEFOL-UHFFFAOYSA-N 0.000 description 1
- 239000003849 aromatic solvent Substances 0.000 description 1
- 150000001555 benzenes Chemical class 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- FBSAITBEAPNWJG-UHFFFAOYSA-N dimethyl phthalate Natural products CC(=O)OC1=CC=CC=C1OC(C)=O FBSAITBEAPNWJG-UHFFFAOYSA-N 0.000 description 1
- 229960001826 dimethylphthalate Drugs 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- SQNZJJAZBFDUTD-UHFFFAOYSA-N durene Chemical compound CC1=CC(C)=C(C)C=C1C SQNZJJAZBFDUTD-UHFFFAOYSA-N 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 239000002932 luster Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 229920000728 polyester Polymers 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 239000005060 rubber Substances 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000003245 working effect Effects 0.000 description 1
Abstract
The invention discloses a kind of production method of high boiling aromatic hydrocarbon solvent oil, with C10 aromatic hydrocarbons for raw material, after shortening lighting, carry out rectifying separation, get the cut of 150 ~ 180 DEG C or the cut of 180 ~ 215 DEG C, be high boiling aromatic hydrocarbon solvent oil; Wherein, hydrogenation catalyst adopts amorphous aluminum silicide complex carrier, and carrying active ingredients oxide compound is nickel oxide, molybdenum oxide, Tungsten oxide 99.999 and phosphorus oxide; Activeconstituents oxide compound gross weight is 20% ~ 60% of sial complex carrier weight; The weight ratio of nickel oxide, molybdenum oxide, Tungsten oxide 99.999, phosphorus oxide is: 10 ~ 30:50 ~ 85:3 ~ 20:0.5 ~ 10.Present invention process is simple, is convenient to industrial operation continuous seepage.
Description
Technical field
The present invention relates to a kind of production method of high boiling aromatic hydrocarbons oil, belong to petrochemical industry.
Background technology
As one of main petroleum products, solvent oil is together with gasoline, kerosene, diesel oil, lubricating oil and be called the large class petroleum products of China five.Solvent oil has a wide range of applications in industries such as medicine, chemical industry, macromolecular material, rubber and paint.At present, the main raw material that solvent oil is produced has three sources: crude oil straight run, and catalytic reforming is raffinated oil and condensate oil, and through refining to improve color and luster, smell, need improve stability.Divide according to boiling range scope, common are No. 6 solvent oils (boiling range 60 ~ 90 DEG C), No. 90 solvent oils (boiling range 90 ~ 120 DEG C), No. 150 solvent oils (boiling range 120 ~ 150 DEG C), No. 200 solvent oils (boiling range 140 ~ 200 DEG C), No. S-180 (boiling range 195 ~ 245 DEG C), No. S-1800 (boiling range 195 ~ 270 DEG C) etc.In general boiling range higher than 150 DEG C be referred to as high boiling point solvent oil.Current domestic solvent oil market, the trade mark is numerous, and wherein varsol oil and benzene class (aromatic hydrocarbons) compound solvent oil respectively account for about half.
C10 heavy aromatics (boiling range about 200 ~ 350 DEG C), is mainly derived from refinery catalytic reforming unit and polyester raw material factory wide fraction catalytic reforming unit.It forms complexity, and bromine number is low, and between component, boiling point difference is very little, and many is high-solidification point, and resource availability is low.The light fraction that before the most cut and extract of current domestic C10 heavy aromatics producer 250 DEG C, economic value added is higher, the C10 tail oil (boiling range about 260 ~ 380 DEG C) that residue boiling range is higher is then sold as fuel additive.
Mainly concentrating on for the comprehensive utilization report of C10 Heavy Aromatic Hydrocarbons adopts various kinds physical separation method to extract high added value industrial chemicals before boiling point 250 DEG C, as: Chinese patent CN101343207A takes dimethyl phthalate from C10 aromatic hydrocarbons, to isolate NSC 62102 and p-Diethylbenzene as extraction agent; Chinese patent CN101250078A adopts rectifier unit to extract mixed methylnaphthalene from C10 aromatic hydrocarbons; Chinese patent CN101318874A reports one and isolates naphthalene and durol from C10 heavy aromatics, simultaneously by-product aromatic solvent.
Prior art does not carry out Appropriate application to C10 aromatic hydrocarbons, and especially C10 tail oil is used as fuel additive mostly, causes the wasting of resources.
Summary of the invention
The object of the invention is to solve the defect existed in prior art, a kind of energy Appropriate application C10 aromatic hydrocarbon resource is provided, improve the method for lighting end productive rate.
In order to achieve the above object, the invention provides a kind of production method of high boiling aromatic hydrocarbon solvent oil, with C10 aromatic hydrocarbons for raw material, through shortening, carry out rectifying separation, get the cut of 150 ~ 180 DEG C or the cut of 180 ~ 215 DEG C, be high boiling aromatic hydrocarbon solvent oil.Wherein, hydrogenation catalyst adopts amorphous aluminum silicide complex carrier, and carrying active ingredients oxide compound is nickel oxide, molybdenum oxide, Tungsten oxide 99.999 and phosphorus oxide; Activeconstituents oxide compound gross weight is 20% ~ 60% of sial complex carrier weight, is preferably: 30% ~ 55%; The weight ratio of nickel oxide, molybdenum oxide, Tungsten oxide 99.999, phosphorus oxide is: 10 ~ 30:50 ~ 85:3 ~ 20:0.5 ~ 8, preferably: 12 ~ 20:65 ~ 85:3 ~ 10:0.5 ~ 5; In amorphous aluminum silicide complex carrier, silicon oxide and alumina weight are than 20 ~ 70:30 ~ 80, preferably 50 ~ 70:30 ~ 50.
Above-mentioned catalytic hydrogenation reaction condition is: hydrogen pressure 4 ~ 10MPa, temperature of reaction 300 ~ 400 DEG C, hydrogen to oil volume ratio 600 ~ 3000, volume space velocity 0.9 ~ 2.5h
-1.
The raw material that high boiling aromatic hydrocarbon solvent oil of the present invention adopts is selected from one or both mixing in C10 heavy aromatics and C10 tail oil, preferred C10 heavy aromatics and C10 tail oil mix with volume ratio 2:1, while effectively utilizing tail oil, hydrogenation lighting energy consumption can be reduced again, now catalytic hydrogenation reaction condition optimization: hydrogen pressure 4 ~ 8MPa, temperature of reaction 320 ~ 370 DEG C, hydrogen to oil volume ratio 700 ~ 1500, volume space velocity 1.0 ~ 2h
-1.
Above-mentioned hydrogenation catalyst is before carrying out shortening to C10 aromatic hydrocarbons, first through prevulcanized.Pre-vulcanization process is: hydrogen is warming up to 150 DEG C, pumps into dithiocarbonic anhydride activation oil (concentration of dithiocarbonic anhydride is 1 ~ 3wt%), is progressively warming up to 300 DEG C and activates, soak time 24h.
Above-mentioned C10 aromatic hydrocarbons is after rectifying separation, and the front-end volatiles of 137 DEG C can be used as gasoline blending oil or are separated further and obtain No. 6 solvent oils (boiling range 60 ~ 90 DEG C) and No. 90 solvent oils (90 ~ 120 DEG C); 137 ~ 143 DEG C of cuts are xylol; Main products high boiling aromatic hydrocarbon solvent oil is the cut of 150 ~ 180 DEG C and 180 ~ 215 DEG C; Boiling point is higher than the cut of 215 DEG C as raw material, and high boiling aromatic hydrocarbon solvent oil is prepared in circulation.
The present invention has the following advantages compared to existing technology:
1, C10 aromatic hydrocarbons is after hydrogenation lighting, carrying out rectifying separation, can effectively improve lighting end productive rate, and the cut of 150 ~ 180 DEG C of separation and the cut of 180 ~ 215 DEG C meet " SA1000 " data demand and " SA1500 " data demand in " high boiling aromatic hydrocarbon solvent " GB (GB/T29497-2013) respectively.
2, the rectifying still liquid of production technique mid-boiling point of the present invention more than 215 DEG C returns recycled in hydrogenator as raw material, and highway route design is reasonable, improves the utilization ratio of C10 aromatic hydrocarbon resource.
3, the little bromine number of constituent content such as C10 aromatic hydrocarbons sulphur nitrogen is low, and therefore hydrogenation lighting process hydrogen consumption is low, and pollution gas discharge is low.
4, C10 aromatic hydrocarbons of the present invention adopts C10 heavy aromatics to mix as raw material with C10 tail oil, can make full use of tail oil, and relative C10 tail oil direct hydrogenation lighting, and energy consumption is low, extending catalyst work-ing life, can effectively save production cost.
5, present invention process is simple, is convenient to industrial operation continuous seepage.
Embodiment
Below in conjunction with specific embodiment, the present invention is described in detail.
Embodiment 1
Get C10 heavy aromatics and carry out hydrogenation lighting, in hydrogenation catalyst, activeconstituents oxide compound gross weight is 25% of amorphous aluminum silicide complex carrier weight; In amorphous aluminum silicide complex carrier, silicon oxide compares 38:62 with alumina weight; In activeconstituents oxide compound, the weight ratio of nickel oxide, molybdenum oxide, Tungsten oxide 99.999, phosphorus oxide is: 10:81:8.2:0.8; Temperature of reaction 320 DEG C, hydrogen pressure 5MPa, hydrogen to oil volume ratio 600, volume space velocity 1.9h
-1.Again through rectifying separation, the front-end volatiles of 137 DEG C can be used as gasoline blending oil or be separated further obtain No. 6 solvent oils (boiling range 60 ~ 90 DEG C) and No. 90 solvent oils (90 ~ 120 DEG C), 137 ~ 143 DEG C of cuts are xylol, the cut of main products 150 ~ 180 DEG C and 180 ~ 215 DEG C and boiling point account for 7.0% respectively higher than the distillation kettle liquid of 215 DEG C, 8.0%, 15%, 45%, 25%(volume percent).Wherein, to return hydrogenator higher than the distillation kettle liquid of 215 DEG C little on oil property impact after hydrogenation for the boiling point of 25%.Physical data before and after C10 heavy aromatics shortening, sees the following form 1.
Physical data before and after table 1C10 heavy aromatics hydrogenation
Embodiment 2
C10 tail oil after cut and extract light constituent carries out hydrogenation lighting, and in hydrogenation catalyst, activeconstituents oxide compound gross weight is 50% of amorphous aluminum silicide complex carrier weight; In amorphous aluminum silicide complex carrier, silicon oxide compares 64.5:35.5 with alumina weight; In activeconstituents oxide compound, the weight ratio of nickel oxide, molybdenum oxide, Tungsten oxide 99.999, phosphorus oxide is: 22:71:3.5:3.5, temperature of reaction 385 DEG C, hydrogen pressure 9.5MPa, hydrogen to oil volume ratio 2800, volume space velocity 1.0h
-1.Go out the front-end volatiles of 137 DEG C through rectifying separation again, 137 ~ 143 DEG C of cuts are xylol, the cut of main products 150 ~ 180 DEG C and 180 ~ 215 DEG C and boiling point account for 10%, 5%, 8%, 22%, 55% respectively higher than the distillation kettle liquid of 215 DEG C.Wherein, to return hydrogenator higher than the distillation kettle liquid of 215 DEG C little on oil property impact after hydrogenation for the boiling point of 55%.Physical data before and after hydrogenation, sees the following form 2.
Physical data before and after table 2C10 tail oil hydrogenation
Embodiment 3
C10 heavy aromatics and the C10 tail oil after cut and extract light constituent are according to volume ratio 2:1 mixing, and carry out hydrogenation lighting, in hydrogenation catalyst, activeconstituents oxide compound gross weight is 32.5% of amorphous silicon aluminium complex carrier weight; In amorphous silicon aluminium complex carrier, silicon oxide compares 65.5:34.5 with alumina weight; In activeconstituents oxide compound, the weight ratio of nickel oxide, molybdenum oxide, Tungsten oxide 99.999, phosphorus oxide is: 12:78.5:4.5:5; Temperature of reaction 340 DEG C, hydrogen pressure 6MPa, hydrogen to oil volume ratio 1000, volume space velocity 1.8h
-1.Go out the front-end volatiles of 137 DEG C through rectifying separation again, 137 ~ 143 DEG C of cuts are xylol, the cut of main products 150 ~ 180 DEG C and 180 ~ 215 DEG C and boiling point account for 5%, 8%, 15%, 35%, 37% respectively higher than the distillation kettle liquid of 215 DEG C.Wherein, to return hydrogenator higher than the distillation kettle liquid of 215 DEG C little on oil property impact after hydrogenation for the boiling point of 37%.Physical data before and after hydrogenation, sees the following form 3..
Show physical data before and after 3C10 tail oil and C10 heavy aromatics mixing oil hydrogenation
Embodiment 4
C10 heavy aromatics and the C10 tail oil after cut and extract light constituent are according to volume ratio 2:1 mixing, and carry out hydrogenation lighting, in hydrogenation catalyst, activeconstituents oxide compound gross weight is 50% of amorphous aluminum silicide complex carrier weight; In amorphous aluminum silicide complex carrier, silicon oxide compares 53.6:46.4 with alumina weight; In activeconstituents oxide compound, the weight ratio of nickel oxide, molybdenum oxide, Tungsten oxide 99.999, phosphorus oxide is: 20:69:10:1; Temperature of reaction 340 DEG C, hydrogen pressure 6MPa, hydrogen to oil volume ratio 1000, volume space velocity 1.5h
-1.Again through rectifying separation, the front-end volatiles of 137 DEG C, 137 ~ 143 DEG C of cuts are xylol, the cut of main products 150 ~ 180 DEG C and 180 ~ 215 DEG C and boiling point account for 4% respectively higher than the distillation kettle liquid of 215 DEG C, 8%, 21%, 29%, 38%(volume percent).Wherein, to return hydrogenator higher than the distillation kettle liquid of 215 DEG C little on oil property impact after hydrogenation for the boiling point of 38%.Physical data before and after C10 heavy aromatics shortening, sees the following form 4.
Show physical data before and after 4C10 tail oil and C10 heavy aromatics mixing oil hydrogenation
Embodiment 5
C10 heavy aromatics and the C10 tail oil after cut and extract light constituent are according to volume ratio 2:1 mixing, and carry out hydrogenation lighting, in hydrogenation catalyst, activeconstituents oxide compound gross weight is 45% of amorphous aluminum silicide complex carrier weight; In amorphous aluminum silicide complex carrier, silicon oxide compares 60.3:39.7 with alumina weight; In activeconstituents oxide compound, the weight ratio of nickel oxide, molybdenum oxide, Tungsten oxide 99.999, phosphorus oxide is: 17:73.5:7.5:2; Temperature of reaction 340 DEG C, hydrogen pressure 6MPa, hydrogen to oil volume ratio 1000, volume space velocity 1.5h
-1.Again through rectifying separation, the front-end volatiles of 137 DEG C, 137 ~ 143 DEG C of cuts are xylol, the cut of main products 150 ~ 180 DEG C and 180 ~ 215 DEG C and boiling point account for 5% respectively higher than the distillation kettle liquid of 215 DEG C, 7%, 19%, 37%, 32%(volume percent).Wherein, to return hydrogenator higher than the distillation kettle liquid of 215 DEG C little on oil property impact after hydrogenation for the boiling point of 32%.Physical data before and after C10 heavy aromatics shortening, sees the following form 5.
Show physical data before and after 5C10 tail oil and C10 heavy aromatics mixing oil hydrogenation
In above embodiment, under rectifying separation goes out 137 ~ 143 DEG C of cut products (xylol), the analytical data of main products high boiling aromatic hydrocarbon solvent oil (150 ~ 180 DEG C and 180 ~ 215 DEG C of cuts) is shown in, all meet corresponding Standard data, refer to following table 6.
Table 6 the physical property of product and Standard data compare
note:gB data target
1adopt " 5 DEG C of xylol " data demand in " oil xylol " GB (GB/T3407-2010); GB data target
2adopt " SA1000 " data demand in " high boiling aromatic hydrocarbon solvent " GB (GB/T29497-2013); GB data target
3adopt " SA1500 " data demand in " high boiling aromatic hydrocarbon solvent " GB (GB/T29497-2013).
Claims (8)
1. the production method of a high boiling aromatic hydrocarbon solvent oil, it is characterized in that: described production method for raw material, after shortening lighting, carries out rectifying separation with C10 aromatic hydrocarbons, get the cut of 150 ~ 180 DEG C or the cut of 180 ~ 215 DEG C, be described high boiling aromatic hydrocarbon solvent oil; Wherein, hydrogenation catalyst adopts amorphous aluminum silicide complex carrier, and carrying active ingredients oxide compound is nickel oxide, molybdenum oxide, Tungsten oxide 99.999 and phosphorus oxide; In described amorphous aluminum silicide complex carrier silicon oxide with alumina weight than 20 ~ 70:30 ~ 80; Described activeconstituents oxide compound gross weight is 20% ~ 60% of sial complex carrier weight; The weight ratio of described nickel oxide, molybdenum oxide, Tungsten oxide 99.999, phosphorus oxide is: 10 ~ 30:50 ~ 85:3 ~ 20:0.5 ~ 8.
2. production method according to claim 1, is characterized in that: described catalytic hydrogenation reaction condition is: hydrogen pressure 4 ~ 10MPa, temperature of reaction 300 ~ 400 DEG C, hydrogen to oil volume ratio 600 ~ 3000, volume space velocity 0.9 ~ 2.5h
-1.
3. production method according to claim 1, is characterized in that: described raw material is selected from one or both mixing in C10 heavy aromatics and C10 tail oil.
4. production method according to claim 3, is characterized in that: described raw material is made up of with volume ratio 2:1 mixing C10 heavy aromatics and C10 tail oil; Described catalytic hydrogenation reaction condition is: hydrogen pressure 4 ~ 8MPa, temperature of reaction 320 ~ 370 DEG C, hydrogen to oil volume ratio 700 ~ 1500, volume space velocity 1.0 ~ 2h
-1.
5., according to the arbitrary described generation method of Claims 1-4, it is characterized in that: in described amorphous aluminum silicide complex carrier silicon oxide with alumina weight than 50 ~ 70:30 ~ 50; Described activeconstituents oxide compound is 30% ~ 55% of sial complex carrier weight; In described activeconstituents oxide compound, the weight ratio of nickel oxide, molybdenum oxide, Tungsten oxide 99.999, phosphorus oxide is: 12 ~ 20:65 ~ 85:3 ~ 10:0.5 ~ 5.
6. according to the arbitrary described production method of Claims 1-4, it is characterized in that: described hydrogenation catalyst is before carrying out shortening to C10 aromatic hydrocarbons, first through prevulcanized.
7. production method according to claim 6, is characterized in that: described pre-vulcanization process is: hydrogen is warming up to 150 DEG C, pumps into dithiocarbonic anhydride activation oil, is progressively warming up to 300 DEG C and activates, soak time 24h; In described dithiocarbonic anhydride activation oil, the concentration of dithiocarbonic anhydride is 1 ~ 3wt%.
8. according to the arbitrary described production method of Claims 1-4, it is characterized in that: described C10 aromatic hydrocarbons is after shortening lighting, rectifying separation, and boiling point is higher than the cut of 215 DEG C as raw material, and high boiling aromatic hydrocarbon solvent oil is prepared in circulation.
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| CN108855163A (en) * | 2017-05-16 | 2018-11-23 | 江苏华伦化工有限公司 | A kind of ten tail oil catalyst for cracking of reformation carbon and its preparation and application |
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| CN112876334B (en) * | 2021-01-15 | 2023-01-31 | 山东京博石油化工有限公司 | Production device and preparation method of high-boiling-point aromatic solvent oil |
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| CN1217370A (en) * | 1997-11-13 | 1999-05-26 | 中国石油化工集团公司 | Hydrodealkylating and alkyl transfering process for heavy aromatic hydrocarbon |
| CN1752058A (en) * | 2004-09-24 | 2006-03-29 | 中国石油化工股份有限公司 | Method of heavy arene hydrogenation dealkylation and alkylation transfer |
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