CN1450146A - Method for producing kerosene type solvent oil and catalyst thereof - Google Patents
Method for producing kerosene type solvent oil and catalyst thereof Download PDFInfo
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- CN1450146A CN1450146A CN 03126138 CN03126138A CN1450146A CN 1450146 A CN1450146 A CN 1450146A CN 03126138 CN03126138 CN 03126138 CN 03126138 A CN03126138 A CN 03126138A CN 1450146 A CN1450146 A CN 1450146A
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- kerosene
- oil
- carrier
- catalyst
- hydrogenation
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- 239000003350 kerosene Substances 0.000 title claims abstract description 40
- 239000003054 catalyst Substances 0.000 title claims abstract description 38
- 239000002904 solvent Substances 0.000 title claims abstract description 20
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 13
- 238000000034 method Methods 0.000 claims abstract description 24
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 17
- 239000001257 hydrogen Substances 0.000 claims abstract description 12
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 12
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 7
- 238000006243 chemical reaction Methods 0.000 claims abstract description 6
- 229910017318 Mo—Ni Inorganic materials 0.000 claims abstract description 4
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims description 11
- 229910052751 metal Inorganic materials 0.000 claims description 9
- 239000002184 metal Substances 0.000 claims description 9
- OGIDPMRJRNCKJF-UHFFFAOYSA-N titanium oxide Inorganic materials [Ti]=O OGIDPMRJRNCKJF-UHFFFAOYSA-N 0.000 claims description 9
- 229910052721 tungsten Inorganic materials 0.000 claims description 8
- 238000004517 catalytic hydrocracking Methods 0.000 claims description 7
- 229910052759 nickel Inorganic materials 0.000 claims description 7
- 150000002431 hydrogen Chemical class 0.000 claims description 5
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 4
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 229910052750 molybdenum Inorganic materials 0.000 claims description 4
- 239000004408 titanium dioxide Substances 0.000 claims description 4
- QGJOPFRUJISHPQ-UHFFFAOYSA-N Carbon disulfide Chemical group S=C=S QGJOPFRUJISHPQ-UHFFFAOYSA-N 0.000 claims description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 20
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 10
- 231100000252 nontoxic Toxicity 0.000 abstract description 8
- 230000003000 nontoxic effect Effects 0.000 abstract description 8
- 150000004945 aromatic hydrocarbons Chemical class 0.000 abstract description 5
- 239000002994 raw material Substances 0.000 abstract description 4
- 229910003076 TiO2-Al2O3 Inorganic materials 0.000 abstract 2
- 239000003921 oil Substances 0.000 description 30
- KBJMLQFLOWQJNF-UHFFFAOYSA-N nickel(ii) nitrate Chemical compound [Ni+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O KBJMLQFLOWQJNF-UHFFFAOYSA-N 0.000 description 12
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 9
- 239000005864 Sulphur Substances 0.000 description 9
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 8
- 238000012545 processing Methods 0.000 description 7
- 239000002253 acid Substances 0.000 description 6
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 230000009967 tasteless effect Effects 0.000 description 6
- -1 polyoxyethylene Polymers 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 4
- 150000001412 amines Chemical class 0.000 description 4
- 238000009835 boiling Methods 0.000 description 4
- 239000008367 deionised water Substances 0.000 description 4
- 229910021641 deionized water Inorganic materials 0.000 description 4
- 238000001035 drying Methods 0.000 description 4
- 239000010742 number 1 fuel oil Substances 0.000 description 4
- 239000000843 powder Substances 0.000 description 4
- 238000011156 evaluation Methods 0.000 description 3
- 238000011835 investigation Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 2
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 2
- 229920003171 Poly (ethylene oxide) Polymers 0.000 description 2
- 241000219782 Sesbania Species 0.000 description 2
- XFBXDGLHUSUNMG-UHFFFAOYSA-N alumane;hydrate Chemical compound O.[AlH3] XFBXDGLHUSUNMG-UHFFFAOYSA-N 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 238000007598 dipping method Methods 0.000 description 2
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 229910017604 nitric acid Inorganic materials 0.000 description 2
- 231100000989 no adverse effect Toxicity 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- 230000006641 stabilisation Effects 0.000 description 2
- 150000003464 sulfur compounds Chemical class 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- 229910010413 TiO 2 Inorganic materials 0.000 description 1
- 241000219793 Trifolium Species 0.000 description 1
- 239000000443 aerosol Substances 0.000 description 1
- 239000005030 aluminium foil Substances 0.000 description 1
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 1
- 229910021502 aluminium hydroxide Inorganic materials 0.000 description 1
- 239000002199 base oil Substances 0.000 description 1
- 239000012459 cleaning agent Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 239000006071 cream Substances 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 239000008157 edible vegetable oil Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000004898 kneading Methods 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 238000007747 plating Methods 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 235000013599 spices Nutrition 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000004753 textile Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Abstract
The present invention discloses a production method of kerosene solvent naphtha and its catalyst for said method. In said method the raw material oil is straight-run kerosene or hydrocracked kerosene fraction with 130-300 deg.c, and a hydrogenation method is adopted to produce high-quality kerosene solvent naphtha. Said used hydrogenation catalyst is W-Ni-TiO2-Al2O3 or W-Mo-Ni/TiO2-Al2O3, and the hydrogen fractional pressure required for hydrogenation is 6.0-15.0 MPa, reaction temp. is 220-360 deg.C, and the volume space velocity is 0.3-2.0 h(-1), and the hydrogen-oil volume ratio is 300-800. The product produced by using said invented mether is white in colour, and is non-toxic, harmless and smelless, its sulful and nitrogen contents are less than 1 microgram/g, and its arene content is less than 200 microgram/g.
Description
Technical field
The present invention relates to a kind of production method of solvent oil, especially relate to production method and the used catalyzer of this method that solvent oil is produced in a kind of kerosene(oil)fraction hydrofining.
Background technology
The kerosene raffinate end-use is very extensive.It mainly as metal rolled oily base oils such as high-quality aerosol solvent and aluminium foils, also can be used for field of fine chemical such as high-quality electronics wash oil, industrial white oil and edible oil processing, food product pack, makeup mediation, spices extracting.In addition, at low-temperature grease, printing ink solvent, non-water power plating solvent, textile auxiliary, lustering agent, industrial cleaning agent and wash in the process of producing product of daily clean-out systems such as neck agent, hair cream, makeup and all will add kerosene type solvent naphtha.According to the market requirement, kerosene raffinate can obtain multiple kerosene type specialty oil products after cutting through rectifying.
The traditional method of producing special solvent oil with kerosene(oil)fraction is the clay-filtered method of soda acid, but quality product is not high, and yield is low, and produces a large amount of acid sludges, alkaline residue and waste water in the production process, and equipment corrosion is serious.The patent CN1157847A of Xingda Petro-chemical Science and Technology Industry and Trade Corp. Nanjing's invention adopts hydrogenation method to make with extra care, stock oil and hydrogen react under nickel catalyzator, this method condition relaxes, liquid is received high, it is nontoxic to generate oil, and do not have environmental issues such as the three wastes, its deficiency can not guarantee that for this technology product does not have smell.Patent CN1258720A carries out hydrofining to kerosene(oil)fraction through the liquid wax that dewaxing by molecular sieve makes, and product is nontoxic tasteless, and aromaticity content is less than 0.1%, but the kerosene(oil)fraction palpus earlier can be as stock oil through dewaxing by molecular sieve, and the stock oil scope of application is too narrow.
Summary of the invention
The present invention be directed to the deficiency that prior art exists, provide a kind of hydrogenation method to produce the method for kerosene type solvent naphtha, product with this method production, color water-white, nontoxic tasteless not only, and sulphur, nitrogen content are all less than 1 μ g/g, aromaticity content all has no adverse effect to HUMAN HEALTH and environment less than 200 μ g/g.
The present invention also provides this kerosene type solvent naphtha production method used catalyzer in addition.
The invention provides a kind of solvent oil production method, stock oil is 130～300 ℃ virgin kerosene or hydrocracking kerosene(oil)fraction in the method, adopt hydrogenation method to produce fat coal oil type solvent oil, it is characterized in that: the used hydrogenation catalyst of this method is W-Ni/TiO
2-Al
2O
3Or W-Mo-Ni/TiO
2-Al
2O
3, the required hydrogen dividing potential drop of hydrogenation is 6.0～15.0MPa, and temperature of reaction is 220～360 ℃, and volume space velocity is 0.3～2.0h
-1, hydrogen to oil volume ratio is 300～800.
In method provided by the present invention, when making spent hydroprocessing catalyst, preferably catalyzer is carried out prevulcanized, vulcanizing agent recommends to use dithiocarbonic anhydride.
It is carrier that the used hydrogenation catalyst of production method of the present invention adopts titanium dioxide, aluminium sesquioxide, W, Ni or W, Mo, Ni are reactive metal, wherein titanium dioxide accounts for 10～60% of total weight of carrier, aluminium sesquioxide accounts for 40%～90% of total weight of carrier, above percentage number average is in oxide dry basis, when adopting W, Ni to be reactive metal, catalyzer consist of WO
3Account for 5～35% of total catalyst weight, NiO accounts for 1～20% of total catalyst weight, and surplus is a carrier; When adopt W, Mo, when Ni is reactive metal, catalyzer consist of WO
3Account for 5～35% of total catalyst weight, NiO accounts for 1～20% of total catalyst weight, MoO
3Account for 1～25% of total catalyst weight, surplus is a carrier.
The used W-Ni/TiO of the present invention
2-Al
2O
3, W-Mo-Ni/TiO
2-Al
2O
3The Preparation of catalysts method is:
(1) hydrous titanium oxide, aluminium hydroxide are mixed, add kneading and compactings such as sesbania powder, nitric acid, citric acid and polyoxyethylene glycol then, carry out drying then under 50～180 ℃ of temperature, be 1～15 hour time of drying.Carry out roasting again under 350～750 ℃ of temperature afterwards and make carrier, roasting time is 1～15 hour;
(2) with amine molybdate, ammonium metawolframate and nickelous nitrate, or ammonium metawolframate and nickelous nitrate add in the deionized water at ambient temperature, makes metallic solution, under 15～90 ℃ of temperature, uses this solution dipping carrier, and soak time is 1～15 hour.Also can leave standstill under the room temperature 2～25 hours with solution with after spraying the saturation method impregnated carrier, then it is carried out drying under 50～180 ℃ of temperature, be 1～15 hour time of drying.Roasting is carried out in dry good back under 300～600 ℃ of temperature, roasting time is 1～15 hour, can make catalyst system therefor of the present invention.
Compared with prior art, product solvability and the volatility of using the inventive method to produce are good, and its every index all is in the leading level in the world, fully can import substitutes.And product colour water-white, nontoxic tasteless, and sulphur, nitrogen content is all less than 1 μ g/g, and aromaticity content all has no adverse effect to HUMAN HEALTH and environment less than 200 μ g/g.
Embodiment
Further specify effect of the present invention with specific embodiment below, but embodiment does not limit the scope of the invention.
Embodiment 1
Industry hydrous titanium oxide 34g, SB aluminium hydrate powder 120g, after mixing, add 8g sesbania powder, the 24g polyoxyethylene glycol, the 5g citric acid, the nitric acid of 30ml 65% and appropriate amount of deionized water, mixed pinching becomes the bar of Φ 1.6mm, dry 4h under 110 ℃ of temperature, in 550 ℃ of roasting temperature 4h, make carrier again.
Add metatungstic acid amine, nickelous nitrate in deionized water, solution composition is 80g metatungstic acid amine/100ml, nickelous nitrate 12g/100ml.The 100g carrier is immersed in the above-mentioned solution of 200ml, under 40 ℃ of temperature, soak 2h, filter back dry 4h under 110 ℃ of temperature, at 500 ℃ of roasting temperature 4h, make catalyst A afterwards.The character of catalyst A sees Table 1.
Embodiment 2
Industry hydrous titanium oxide 34g, SB aluminium hydrate powder 120g makes carrier by the method for embodiment 1.Add metatungstic acid amine, amine molybdate, nickelous nitrate in deionized water, solution composition is metatungstic acid amine 90g/100ml, amine molybdate 25g/100ml, nickelous nitrate 22g/100ml.The 100g carrier is carried out saturated spray dipping.Leave standstill 10h under the room temperature, dry 4h under 110 ℃ of temperature at 500 ℃ of roasting temperature 4h, makes catalyst B afterwards.The character of catalyst B sees Table 1.
Embodiment 3
With virgin kerosene I is raw material, on the medium-sized fixed bed hydrogenation device of 100ml above-mentioned catalyst A has been carried out the processing condition investigation.At first the kerosene with sulfur compound carries out prevulcanized to catalyzer, and the reactive metal on the catalyzer is converted into sulphided state by oxidation state.After a period of stabilisation, begin that it is carried out activity and investigate test.The character of virgin kerosene I sees Table 2.
Adopt the virgin kerosene I shown in the table 2, under the effect of the catalyst A shown in hydrofining technology condition shown in the table 3 and the table 1, virgin kerosene I is carried out hydrofining, the character of products obtained therefrom is as shown in table 3.
As can be seen from Table 3, adopt catalyst A, can produce fat coal oil type special solvent oil by hydrofining, its product colour water-white, nontoxic tasteless, sulphur, nitrogen content are all less than 1 μ g/g, and aromaticity content can be less than 200 μ g/g.
Table 1 catalyzer main physical and chemical
| Project | Catalyst A | Catalyst B |
| Chemical constitution, % | ||
| ??WO 3 | ??28.5 | ??20.5 |
| ??MoO 3 | ??/ | ??6.8 |
| ??NiO | ??2.5 | ??3.0 |
| ??TiO 2 | ??15.3 | ??15.3 |
| ??Al 2O 3 | Surplus | Surplus |
| Physical properties | ||
| Specific surface, m 2/g | ??110 | ??121 |
| Pore volume, ml/g | ??0.23 | ??0.23 |
| Bulk density, kg/m 3 | ??1150 | ??1100 |
| Profile | Trifolium | Cylinder |
Table 2 stock oil character
| Project | Virgin kerosene I | Virgin kerosene II | Hydrocracking kerosene |
| Density, kg/m 3 | ??810.1 | ??807.5 | ??789.3 |
| Color (Saybolt colour number) | ??21 | ??17 | ??20 |
| Sulphur, μ g/g | ??805.1 | ??2220 | ??＜2 |
| Nitrogen, μ g/g | ??5.0 | ??12 | ??＜2 |
| Aromatic hydrocarbons, % | ??10.5 | ??17.5 | ??6.3 |
| Smell | Irritating smell | Irritating smell | Irritating smell |
| Boiling range, ℃ | |||
| IBP/10％ | ??195/213 | ??203/214 | ??138/165 |
| 50％/90％ | ??230/250 | ??225/245 | ??189/241 |
| 98％ | ??262 | ??273 | ??247 |
Under the different hydroconversion conditions of table 3 to the evaluation result of catalyst A
| Stock oil | Virgin kerosene I | ||||
| Numbering | ????A-1 | ??A-2 | ??A-3 | ??A-4 | ??A-5 |
| Processing condition | |||||
| The hydrogen dividing potential drop, MPa | ????10.0 | ??7.0 | ??12.0 | ??15.0 | ??15.0 |
| Temperature of reaction, ℃ | ????280 | ??300 | ??320 | ??300 | ??340 |
| Volume space velocity, h -1 | ????0.4 | ??1.0 | ??1.5 | ??1.0 | ??2.0 |
| Hydrogen to oil volume ratio | ????300 | ??400 | ??500 | ??400 | ??700 |
| Hydrogenated products character | |||||
| Density, kg/m 3 | ????803.2 | ??802.5 | ??801.9 | ??802.3 | ??801.0 |
| Color (Saybolt colour number) | ????30 | ??30 | ??30 | ??30 | ??30 |
| Sulphur, μ g/g | ????＜1 | ??＜1 | ??＜1 | ??＜1 | ??＜1 |
| Nitrogen, μ g/g | ????＜1 | ??＜1 | ??＜1 | ??＜1 | ??＜1 |
| Aromatic hydrocarbons, % | ????0.018 | ??0.25 | ??0.14 | ??0.015 | ??0.11 |
| Smell | Free from extraneous odour | Free from extraneous odour | Free from extraneous odour | Free from extraneous odour | Free from extraneous odour |
| Boiling range, ℃ | |||||
| ????IBP/10％ | ????190/208 | ??185/205 | ??183/206 | ??184/206 | ??181/20 ??3 |
| ????50％/90％ | ????227/248 | ??226/247 | ??225/246 | ??226/247 | ??222/24 ??5 |
| ????98％ | ????261 | ??260 | ??260 | ??261 | ??258 |
Embodiment 4
With hydrocracking kerosene is raw material, on the medium-sized fixed bed hydrogenation device of 100ml above-mentioned catalyst A has been carried out the processing condition investigation.Stock oil character sees Table 2.
Adopt the hydrocracking kerosene shown in the table 2, under the effect of the catalyst A shown in hydrogenation technique condition shown in the table 4 and the table 1, hydrocracking kerosene is carried out hydrofining, the character of products obtained therefrom is as shown in table 4.
As can be seen from Table 4, adopt catalyst A, can produce fat coal oil type special solvent oil by hydrofining, its product colour water-white, nontoxic tasteless, sulphur, nitrogen content are all less than 1 μ g/g, and aromaticity content can be less than 200 μ g/g.
Under the different hydrofining technology conditions of table 4 to the evaluation result of catalyst A
| Stock oil | Hydrocracking kerosene | |||
| Numbering | ??H-1 | ??H-2 | ??H-3 | ??H-4 |
| Processing condition | ||||
| The hydrogen dividing potential drop, MPa | ??10.0 | ??7.0 | ??12.0 | ??15.0 |
| Temperature of reaction, ℃ | ??270 | ??260 | ??280 | ??290 |
| Volume space velocity, h -1 | ??0.8 | ??0.4 | ??1.0 | ??1.5 |
| Hydrogen to oil volume ratio | ??400 | ??300 | ??400 | ??600 |
| Hydrogenated products character | ||||
| Density, kg/m 3 | ??786.7 | ??786.9 | ??786.5 | ??786.0 |
| Color (Saybolt colour number) | ??30 | ??30 | ??30 | ??30 |
| Sulphur, μ g/g | ??＜1 | ??＜1 | ??＜1 | ??＜1 |
| Nitrogen, μ g/g | ??＜1 | ??＜1 | ??＜1 | ??＜1 |
| Aromatic hydrocarbons, % | ??0.011 | ??0.015 | ??0.018 | ??0.020 |
| Smell | Free from extraneous odour | Free from extraneous odour | Free from extraneous odour | Free from extraneous odour |
| Boiling range, ℃ | ||||
| ????IBP/10％ | ??136/164 | ??137/165 | ??135/165 | ??133/163 |
| ????50％/90％ | ??187/239 | ??188/239 | ??187/239 | ??186/239 |
| ????98％ | ??247 | ??247 | ??245 | ??244 |
Embodiment 5
With virgin kerosene II is raw material, on the medium-sized fixed bed hydrogenation device of 100ml above-mentioned catalyst B has been carried out the processing condition investigation.At first the kerosene with sulfur compound carries out prevulcanized to catalyzer, and the reactive metal on the catalyzer is converted into sulphided state by oxidation state.After a period of stabilisation, begin that it is carried out activity and investigate test.
Adopt the virgin kerosene II shown in the table 2, under the effect of the catalyst B shown in hydroconversion condition shown in the table 5 and the table 1, virgin kerosene II is carried out hydrofining, the character of products obtained therefrom is as shown in table 5.
As can be seen from Table 5, adopt catalyst B, can produce fat coal oil type special solvent oil by hydrofining, its product colour water-white, nontoxic tasteless, sulphur, nitrogen content are all less than 1 μ g/g, and aromaticity content can be less than 200 μ g/g.
Under the different hydrofining technology conditions of table 5 to the evaluation result of catalyst B
| Stock oil | Virgin kerosene II | ||||
| Numbering | ??B-1 | ??B-2 | ??B-3 | ??B-4 | ??B-5 |
| Processing condition | |||||
| The hydrogen dividing potential drop, MPa | ??12.0 | ??7.0 | ??10.0 | ??15.0 | ??15.0 |
| Temperature of reaction, ℃ | ??310 | ??300 | ??320 | ??320 | ??340 |
| Volume space velocity, h -1 | ??0.7 | ??0.4 | ??1.0 | ??1.0 | ??2.0 |
| Hydrogen to oil volume ratio | ??500 | ??400 | ??500 | ??600 | ??800 |
| Hydrogenated products character | |||||
| Density, kg/m 3 | ??798.6 | ??799.0 | ??797.6 | ??797.0 | ??796.0 |
| Color (Saybolt colour number) | ??30 | ??30 | ??30 | ??30 | ??30 |
| Sulphur, μ g/g | ??＜1 | ??＜1 | ??＜1 | ??＜1 | ??＜1 |
| Nitrogen, μ g/g | ??＜1 | ??＜1 | ??＜1 | ??＜1 | ??＜1 |
| Aromatic hydrocarbons, % | ??0.016 | ??0.12 | ??0.20 | ??0.019 | ??0.18 |
| Smell | Free from extraneous odour | Free from extraneous odour | Free from extraneous odour | Free from extraneous odour | Free from extraneous odour |
| Boiling range, ℃ | |||||
| ????IBP/10％ | ??194/208 | ??195/209 | ??192/206 | ??191/205 | ??188/202 |
| ????50％/90％ | ??222/240 | ??222/241 | ??220/239 | ??220/239 | ??218/238 |
| ????98％ | ??272 | ??273 | ??271 | ??271 | ??270 |
Claims (3)
1. the production method of a kerosene type solvent naphtha, stock oil is 130～300 ℃ virgin kerosene or hydrocracking kerosene(oil)fraction in the method, adopts hydrogenation method to produce kerosene type solvent naphtha, it is characterized in that: the used hydrogenation catalyst of this method is W-Ni/TiO
2-Al
2O
3Or W-Mo-Ni/TiO
2-Al
2O
3, the required hydrogen dividing potential drop of hydrogenation is 6.0～15.0MPa, and temperature of reaction is 220～360 ℃, and volume space velocity is 0.3～2.0h
-1, hydrogen to oil volume ratio is 300～800.
2. production method according to claim 1 is characterized in that, hydrogenation catalyst carries out prevulcanized before using, and vulcanizing agent is a dithiocarbonic anhydride.
3. the used catalyzer of the described production method of claim 1, it is characterized in that: it is carrier that this catalyzer adopts titanium dioxide, aluminium sesquioxide, W, Ni or W, Mo, Ni are reactive metal, wherein titanium dioxide accounts for 10～60% of total weight of carrier, aluminium sesquioxide accounts for 40%～90% of total weight of carrier, above percentage number average is in oxide dry basis, when adopting W, Ni to be reactive metal, catalyzer consist of WO
3Account for 5～35% of total catalyst weight, NiO accounts for 1～20% of total catalyst weight, and surplus is a carrier; When adopt W, Mo, when Ni is reactive metal, catalyzer consist of WO
3Account for 5～35% of total catalyst weight, NiO accounts for 1～20% of total catalyst weight, MoO
3Account for 1～25% of total catalyst weight, surplus is a carrier.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03126138 CN1190474C (en) | 2003-05-05 | 2003-05-05 | Method for producing kerosene type solvent oil and catalyst thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03126138 CN1190474C (en) | 2003-05-05 | 2003-05-05 | Method for producing kerosene type solvent oil and catalyst thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1450146A true CN1450146A (en) | 2003-10-22 |
| CN1190474C CN1190474C (en) | 2005-02-23 |
Family
ID=28684435
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 03126138 Expired - Lifetime CN1190474C (en) | 2003-05-05 | 2003-05-05 | Method for producing kerosene type solvent oil and catalyst thereof |
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| Country | Link |
|---|---|
| CN (1) | CN1190474C (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101942326A (en) * | 2009-07-09 | 2011-01-12 | 中国石油化工股份有限公司抚顺石油化工研究院 | Method for producing low-aromatics solvent oil by hydrogenation |
| CN1840618B (en) * | 2005-03-31 | 2011-08-10 | 中国石油化工股份有限公司 | Hydrogenation catalyst with silicon oxide-alumina as carrier and its preparation |
-
2003
- 2003-05-05 CN CN 03126138 patent/CN1190474C/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1840618B (en) * | 2005-03-31 | 2011-08-10 | 中国石油化工股份有限公司 | Hydrogenation catalyst with silicon oxide-alumina as carrier and its preparation |
| CN101942326A (en) * | 2009-07-09 | 2011-01-12 | 中国石油化工股份有限公司抚顺石油化工研究院 | Method for producing low-aromatics solvent oil by hydrogenation |
| CN101942326B (en) * | 2009-07-09 | 2015-01-14 | 中国石油化工股份有限公司 | Method for producing low-aromatics solvent oil by hydrogenation |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1190474C (en) | 2005-02-23 |
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