CN1876767B - Coal tar hydrocracking method - Google Patents
Coal tar hydrocracking method Download PDFInfo
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- CN1876767B CN1876767B CN2006100282639A CN200610028263A CN1876767B CN 1876767 B CN1876767 B CN 1876767B CN 2006100282639 A CN2006100282639 A CN 2006100282639A CN 200610028263 A CN200610028263 A CN 200610028263A CN 1876767 B CN1876767 B CN 1876767B
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- coal tar
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- 238000004517 catalytic hydrocracking Methods 0.000 title claims abstract description 51
- 238000000034 method Methods 0.000 title claims abstract description 36
- 239000011280 coal tar Substances 0.000 title claims description 54
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 32
- 239000003921 oil Substances 0.000 claims abstract description 31
- 238000006243 chemical reaction Methods 0.000 claims abstract description 29
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 24
- 239000007789 gas Substances 0.000 claims abstract description 11
- 239000007788 liquid Substances 0.000 claims abstract description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000003502 gasoline Substances 0.000 claims abstract description 7
- 239000001257 hydrogen Substances 0.000 claims description 30
- 229910052739 hydrogen Inorganic materials 0.000 claims description 30
- 239000003054 catalyst Substances 0.000 claims description 24
- 239000002283 diesel fuel Substances 0.000 claims description 11
- 238000000926 separation method Methods 0.000 claims description 11
- 238000002203 pretreatment Methods 0.000 claims description 9
- 239000000463 material Substances 0.000 claims description 6
- 229910052759 nickel Inorganic materials 0.000 claims description 6
- 230000001681 protective effect Effects 0.000 claims description 6
- 238000006356 dehydrogenation reaction Methods 0.000 claims description 5
- 238000007324 demetalation reaction Methods 0.000 claims description 5
- 239000004411 aluminium Substances 0.000 claims description 4
- 229910052782 aluminium Inorganic materials 0.000 claims description 4
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 4
- 229910021417 amorphous silicon Inorganic materials 0.000 claims description 4
- 238000005194 fractionation Methods 0.000 claims description 4
- 239000002808 molecular sieve Substances 0.000 claims description 4
- 229910052750 molybdenum Inorganic materials 0.000 claims description 4
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims description 4
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 4
- 229910052721 tungsten Inorganic materials 0.000 claims description 4
- 230000000694 effects Effects 0.000 claims description 3
- 238000005336 cracking Methods 0.000 claims description 2
- 238000011068 loading method Methods 0.000 claims description 2
- 239000002253 acid Substances 0.000 claims 1
- LKTZODAHLMBGLG-UHFFFAOYSA-N alumanylidynesilicon;$l^{2}-alumanylidenesilylidenealuminum Chemical compound [Si]#[Al].[Si]#[Al].[Al]=[Si]=[Al] LKTZODAHLMBGLG-UHFFFAOYSA-N 0.000 claims 1
- 239000000047 product Substances 0.000 abstract description 16
- 239000007795 chemical reaction product Substances 0.000 abstract description 4
- 239000010742 number 1 fuel oil Substances 0.000 abstract 3
- 239000000446 fuel Substances 0.000 description 12
- 238000004519 manufacturing process Methods 0.000 description 7
- PXHVJJICTQNCMI-UHFFFAOYSA-N nickel Substances [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 6
- 238000009835 boiling Methods 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 239000005864 Sulphur Substances 0.000 description 4
- 239000013543 active substance Substances 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 238000007670 refining Methods 0.000 description 4
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 3
- 238000011049 filling Methods 0.000 description 3
- 239000000295 fuel oil Substances 0.000 description 3
- 239000003208 petroleum Substances 0.000 description 3
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 241000219793 Trifolium Species 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 239000000084 colloidal system Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 150000002989 phenols Chemical class 0.000 description 2
- 239000003223 protective agent Substances 0.000 description 2
- 230000003245 working effect Effects 0.000 description 2
- YZCKVEUIGOORGS-OUBTZVSYSA-N Deuterium Chemical compound [2H] YZCKVEUIGOORGS-OUBTZVSYSA-N 0.000 description 1
- 206010033307 Overweight Diseases 0.000 description 1
- LOTCVJJDZFMQGB-UHFFFAOYSA-N [N].[O].[S] Chemical compound [N].[O].[S] LOTCVJJDZFMQGB-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004508 fractional distillation Methods 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000001465 metallisation Methods 0.000 description 1
- 235000020825 overweight Nutrition 0.000 description 1
- 239000011269 tar Substances 0.000 description 1
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Abstract
The invention discloses the coal oil hydrocracking method. The method comprises the following steps: mixing the coal oil and hydrogen gas, adding them into hydrogenation reaction chamber, getting the generating oil, putting the generating oil into heat-high pressure separator, getting light-end products and water from upper logistics, putting lower logistics and hydrogen gas into hydrocracker reaction chamber, getting hydrocracking product, putting the product into high pressure separator, getting hydrogen gas to be used again, and putting the liquid into fractionating tower to get gas, petrol, diesel, light-end products and tail oil. The invention uses low grade coal oil to produce premium grade gasoline and diesel.
Description
Technical field
The present invention relates to high-quality automotive fuel production field, be specifically related to a kind of coal tar hydrocracking method, promptly be stock oil with coal tar, come production lightweight automotive fuel oil product by methods such as widely used hydrogenation pre-treatment in refining of petroleum field and hydrocracking, thereby not only clean utilization coal tar, the source of also widening automotive fuel oil.
Background technology
The world is increasing to the demand of automotive fuel, and is more and more higher to the specification of quality of automotive fuel.Because the restriction of politics cause and petroleum resources produced quantity and total amount, the price of crude oil continues high, add the environmental regulation increasingly stringent, the automotive fuel of necessary production compliance with environmental protection requirements, cause the production cost of refinery to increase, the result who brings like this is more and more higher by the automotive fuel price of oil production, chance is provided therefore for the development of the oil replacement energy.
Coal tar is the byproduct of coking technology, and no matter from boiling range still from forming, coal tar more near the composition of automotive fuel, comes production high-quality cleaning automotive fuel method easier by coal tar than other substitute energys like this, also has more economy.Because the coal tar oil composition is based on aromatic hydrocarbon, and foreign matter content height such as sulphur nitrogen oxygen, can not directly satisfy the specification requirement of cleaning automotive fuel, therefore can not directly use as automotive fuel, need further process.Hydrocracking technology is one of topmost means of light materialization of heavy oil, and be direct best-of-breed technology by heavy ends direct production high-quality automotive fuel, especially strong to stock oil adaptability, good product quality, obtained using widely in the refining of petroleum field, and technology is quite ripe, and the nearly all large-scale refinery in countries in the world has all been built hydroeracking unit.And method is limited for the coal tar secondary processing, and it is few especially that the use method for hydrogen cracking carries out method for processing.The method of present coal tar hydrogenating, wherein:
Chinese invention patent CN1464031A discloses a kind of coal tar hydrogenation process and catalyzer on December 31st, 2003.This patent requires the special special-purpose catalyst of exploitation, flow process is common processing process, and only raw material has been carried out upgrading, contain molecular sieve in its catalyst for hydro-upgrading in addition, very responsive to the water that coal tar hydrogenating generates, because the existence of water vapor or water will make that catalyzer is destroyed, reduced the work-ing life of catalyzer like this, serious destruction catalyzer and cause bed pressure drop to rise, cause device to stop work.
Chinese invention patent CN1351130A discloses the method that a kind of coal tar hydrogenating is produced diesel oil on 05 09th, 2002.What this method was described mainly is that coal tar at first passes through fractionation, the last running that obtains is not as the raw material of hydrotreatment, just the light ends in the coal tar carries out hydrotreatment, owing to do not use hydrocracking catalyst, the course of processing obtains diesel oil distillate can only be as the blend component of diesel product, and coal tar is not utilized fully, cause the whole yield of light-end products to reduce greatly.
Summary of the invention
At the above-mentioned deficiency of prior art, technical problem to be solved by this invention is to provide a kind of coal tar hydrocracking method.This method not only can be utilized tar resource fully, and coal tar all is converted into automotive fuel, has characteristics such as good product quality, device length running period simultaneously.
The present invention solves the problems of the technologies described above the technical scheme that adopts to be: a kind of coal tar hydrocracking method comprises the steps:
A, coal tar and hydrogen are that 4.0MPa-21.0MPa, hydrogen to oil volume ratio are 400 at the reaction stagnation pressure: 1-3000: 1, average reaction temperature is that 200 ℃-450 ℃, volume space velocity are 0.1h
-1-5.0h
-1Under the condition, carry out the hydrogenation pre-treatment by the reactor that contains protective material, catalyst for demetalation and dehydrogenation catalyst, obtain the hydrogenation pre-treatment and generate oil, obtain hydrogen-rich gas, light ends, heavy ends and water through the high pressure hot separator separation, hydrogen-rich gas recycles, and light ends and water are discharged reactive system;
B, be that 4.0MPa-21.0MPa, hydrogen to oil volume ratio are 400 with the heavy ends of step a and hydrogen at the reaction stagnation pressure: 1-4000: 1, average reaction temperature is that 280 ℃-480 ℃, volume space velocity are 0.1h
-1-5.0h
-1Condition under, be carrier by containing with aluminum oxide, amorphous silicon aluminium and molecular sieve, be that the reactor of the hydrocracking catalyst of hydrogenation component carries out hydrocracking with Co, Mo, W, Ni, obtain hydrocracking and generate oil; Hydrocracking generates oil gas-liquid separation in high pressure hot separator, obtain hydrogen-rich gas and liquid, hydrogen-rich gas recycles, and liquid fractionation in separation column, obtain gasoline and diesel oil, obtaining tail oil can partly or entirely circulate as the charging in hydrocracking reaction district.
The described hydrogen-rich gas circulation of above-mentioned steps a of the present invention and b can adopt the two cover recycle systems to circulate respectively, also can adopt a cover recycle system.Light, heavy ends among step a and the b are as the criterion with diesel oil, and diesel oil and the component lighter than diesel oil are counted light ends, and the cut that overweights diesel oil is counted heavy ends.
Among the above-mentioned steps a of the present invention, the full cut of coal tar that coal tar raw material obtains for the coal tar metallization processes, general requirement is done and is not more than 600 ℃, preferably is not more than 580 ℃.
Among the above-mentioned steps a of the present invention, the hydrogenation pretreatment reaction can carry out in the reactor of 1-10 arranged in series setting, preferably carries out in the reactor of 1-8 arranged in series setting, and each reactor is provided with 1-8 beds, preferred 1-6 beds; Except that first reactor, other each reactor tops all are provided with cold hydrogen inlet, and cold hydrogen inlet all is set between each bed; The active substance of pretreatment reaction device filling mainly contains protective material, catalyst for demetalation, dehydrogenation catalyst etc., adopt grading loading, promptly according to liquid flow direction order filling protective material, catalyst for demetalation and dehydrogenation catalyst, and keep granularity to reduce gradually, activity increases gradually, wherein these active substances be the oil refining industry hydrogenation unit widely used be carrier with the aluminum oxide, with Co, Mo, W, Ni is the hydrogenation protecting agent of hydrogenation component, Hydrodemetalation catalyst and hydrogenating desulfurization, hydrodenitrogenation catalyst, shape can be Raschig ring, spherical, sheet, the trifolium shape, four pages of careless shapes and cylinder strip etc.; The hydrogenation pretreatment reaction preferably carries out under the following conditions: reaction stagnation pressure 5.0MPa-19.0MPa, and hydrogen to oil volume ratio 600: 1-2500: 1,220 ℃-400 ℃ of average reaction temperature, volume space velocity 0.1h
-1-3.0h
-1
Among the above-mentioned steps a of the present invention, the light ends that the high pressure hot separator separation obtains is done and is no more than 350 ℃, preferably is no more than 280 ℃, preferably is no more than 205 ℃.
Among the above-mentioned steps b of the present invention, hydrocracking reaction carries out in the reactor of 1-6 arranged in series setting, preferably carries out in the reactor of 1-4 arranged in series setting, and each reactor is provided with 1-8 beds, preferred 1-6 beds; Except that first reactor, other each reactor tops all are provided with cold hydrogen inlet, and cold hydrogen inlet all is set between each bed; The active substance of hydrocracking reactor filling mainly contains protective material, hydrocracking pretreatment catalyst and hydrocracking catalyst, these active substances are that the oil refining industry hydrogenation unit is widely used with aluminum oxide, amorphous silicon aluminium, molecular sieves etc. are carrier, with Co, Mo, W, Ni is the hydrogenation protecting agent of hydrogenation component, hydrocracking pretreatment catalyst and hydrocracking catalyst, wherein hydrocracking catalyst preferably is the hydrocracking catalyst of carrier with the amorphous silicon aluminium, and shape can be Raschig ring, spherical, sheet, the trifolium shape, Herba Galii Bungei shape and cylinder strip etc.; Hydrocracking reaction preferably carries out under the following conditions: reaction stagnation pressure 5.0MPa-19.0MPa, and hydrogen to oil volume ratio 600: 1-3500: 1,300 ℃-450 ℃ of average reaction temperature, volume space velocity 0.1h
-1-3.0h
-1
Because phenols content height in the coal tar, cause oxygen element content higher, therefore in hydrocracking process, produce more water, and these phenols mainly concentrate in the lighter cut of coal tar, and hydrogenation reaction very easily takes place, promptly oxygen removal can be considered the coal tar fractional distillation branch is carried out the hydrogenation pre-treatment earlier like this in lower temperature of reaction, and the water that generates removed from system rapidly, and then the coal tar after the deoxidation is separated through after the hydrocracking.Select this working method, can prolong the work-ing life of hydrocracking reaction district catalyzer after the water that generates in the reaction process removed, thereby improve the running period of device, and method that can be by hydrocracking is with the heavy ends lighting, improve the character of light-end products greatly, to satisfy at present and the specification requirement of automotive fuel in the future.
Description of drawings
Fig. 1 is the process flow diagram of coal tar hydrocracking method of the present invention.
Wherein: 1 is coal tar raw material oil; 2 are hydrogenation pre-treatment inlet hydrogen; 3 is hydrogenation pretreatment reaction device; 4 is high-pressure separator; 5 is hydrocracking reactor; 6 is high-pressure separator; 7 is separation column; 8 is circulating hydrogen compressor; 9 is new hydrogen.
Embodiment
Below in conjunction with drawings and Examples the present invention program and effect are set forth in more detail.
As shown in Figure 1, in the coal tar hydrocracking method that following preferred embodiment 1 of the present invention and preferred embodiment 2 provide, coal tar raw material 1 through purifying treatment at first is mixed into hydrogenation pretreatment reaction device 3 with hydrogen 2, obtaining effluent enters high-pressure separator 4 and carries out gas-liquid separation, the gas circulation that obtains is used, the lighting end and the water that obtain go out system, and the last running continuation and the hydrogen that obtain are mixed into hydrocracking reactor 5; The hydrocracking effluent that obtains enters high-pressure separator 6, separating the gas circulation that obtains mixes after circulating hydrogen compressor 8 recycles with new hydrogen 9, the liquid that separation obtains enters separation column 9 fractionation and obtains gas products, gasoline products, diesel product and tail oil, tail oil can get rid of in addition, also can be used as the charging of hydrocracking reactor 5.
The coal tar character that embodiment 1 uses is listed in table 1.
Table 1 coal tar character
| Coal tar | Coal tar 1 |
| The cut scope, ℃ | ＜540 |
| Density (20 ℃), g/cm 3 | 1.021 |
| Carbon residue, m% | 3.5 |
| Elementary composition, m% | |
| Sulphur | 0.36 |
| Nitrogen | 0.72 |
| Coal tar | Coal tar 1 |
| Oxygen | 6.99 |
| Metal content, μ g/g | |
| Iron | 48 |
| Nickel | 1.2 |
| Calcium | 24 |
| Aromatic hydrocarbons+colloid, m% | 89.1 |
Processing condition are listed in table 2, and product property is listed in table 3.
Table 2 processing condition
Table 3 product main character
| Product yield | Gasoline | Diesel oil | Turning oil |
| Yield, wt% | 45.5 | 50.1 | 0.5 |
| Density (20 ℃), g/cm 3 | 0.69 | 0.85 | 0.91 |
| Boiling range, ℃ | ASTM D86 | ASTM D86 | ASTM D1160 |
| Initial boiling point/10% | 45/56 | 192/222 | 345/378 |
| Product yield | Gasoline | Diesel oil | Turning oil |
| 50％/90％ | 113/168 | 269/305 | 446/512 |
| Do | 185 | 336 | 535 |
| Sulphur content, μ g/g | 10 | 55 | 100 |
| Condensation point, ℃ | -15 | 15 | |
| Cetane value | 46 |
The coal tar character that embodiment 2 uses is listed in table 4.
Table 4 coal tar character
| Coal tar | Coal tar 2 |
| The cut scope, ℃ | ＜550 |
| Density (20 ℃), g/cm 3 | 1.155 |
| Carbon residue, m% | 6.4 |
| Elementary composition, m% | |
| Sulphur | 0.45 |
| Nitrogen | 0.99 |
| Oxygen | 4.25 |
| Metal content, μ g/g | |
| Iron | 77 |
| Nickel | 5.30 |
| Calcium | 36 |
| Aromatic hydrocarbons+colloid, m% | 95.5 |
Processing condition are listed in table 5, and product property is listed in table 6.
Table 5 processing condition
Table 6 product main character
| Product yield | Gasoline | Diesel oil | Turning oil |
| Yield, wt% | 52.2 | 43.0 | 1.0 |
| Density (20 ℃), g/cm 3 | 0.71 | 0.87 | 0.93 |
| Boiling range, ℃ | ASTM D86 | ASTM D86 | ASTM D1160 |
| Initial boiling point/10% | 42/55 | 209/235 | 345/378 |
| 50％/90％ | 110/169 | 271/314 | 446/512 |
| Do | 195 | 339 | 535 |
| Sulphur content, μ g/g | 15 | 70 | 150 |
| Condensation point, ℃ | -10 | 40 | |
| Cetane value | 42 |
Claims (10)
1. a coal tar hydrocracking method is characterized in that, comprises the steps:
A, coal tar and hydrogen are that 4.0MPa-21.0MPa, hydrogen to oil volume ratio are 400 at the reaction stagnation pressure: 1-3000: 1, average reaction temperature is that 200 ℃-450 ℃, volume space velocity are 0.1h
-1-5.0h
-1Under the condition, carry out the hydrogenation pre-treatment, obtain the hydrogenation pre-treatment and generate oil, separate obtaining hydrogen-rich gas, light ends, heavy ends and water through high pressure hot separator by the reactor that contains protective material, catalyst for demetalation and dehydrogenation catalyst;
B, be that 4.0MPa-21.0MPa, hydrogen to oil volume ratio are 400 with the heavy ends of step a and hydrogen at the reaction stagnation pressure: 1-4000: 1, average reaction temperature is that 280 ℃-480 ℃, volume space velocity are 0.1h
-1-5.0h
-1Condition under, be carrier by containing with aluminum oxide, amorphous silicon aluminium and molecular sieve, be that the reactor of the hydrocracking catalyst of hydrogenation component carries out hydrocracking with Co, Mo, W, Ni, obtain hydrocracking and generate oil; Hydrocracking generates oil gas-liquid separation in high pressure hot separator, obtains hydrogen-rich gas and liquid; The fractionation in separation column of this liquid obtains gasoline and diesel oil.
2. coal tar hydrocracking method as claimed in claim 1 is characterized in that, doing of the described coal tar of step a is not more than 600 ℃.
3. coal tar hydrocracking method as claimed in claim 1; it is characterized in that; the described hydrogenation pre-treatment of step a is to finish in the reactor of 1-10 arranged in series setting; the protective material that loads in the reactor, catalyst for demetalation and dehydrogenation catalyst adopt grading loading; promptly keep granularity to reduce gradually according to liquid flow direction, activity increases gradually.
4. coal tar hydrocracking method as claimed in claim 1, it is characterized in that the described hydrogenation pre-treatment of step a is carried out under the following conditions: reaction stagnation pressure 5.0MPa-19.0MPa, hydrogen to oil volume ratio 600: 1-2500: 1,220 ℃-400 ℃ of average reaction temperature, volume space velocity 0.1h
-1-3.0h
-1
5. coal tar hydrocracking method as claimed in claim 1 is characterized in that, the light ends that the described high pressure hot separator separation of step a obtains is done and is no more than 350 ℃.
6. coal tar hydrocracking method as claimed in claim 5 is characterized in that, light ends is done and is no more than 280 ℃.
7. coal tar hydrocracking method as claimed in claim 5 is characterized in that, light ends is done and is no more than 205 ℃.
8. coal tar hydrocracking method as claimed in claim 1 is characterized in that, the described hydrocracking reaction of step b carries out in the reactor of 1-6 arranged in series setting.
9. coal tar hydrocracking method as claimed in claim 1 is characterized in that, the described hydrocracking catalyst of step b is acid cracking component with amorphous aluminum silicide.
10. coal tar hydrocracking method as claimed in claim 1, it is characterized in that the described hydrocracking of step b is carried out under the following conditions: reaction stagnation pressure 5.0MPa-19.0MPa, hydrogen to oil volume ratio 600: 1-3500: 1,300 ℃-450 ℃ of average reaction temperature, volume space velocity 0.1h
-1-3.0h
-1
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Cited By (1)
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| CN103059944A (en) * | 2011-10-21 | 2013-04-24 | 中国石油化工股份有限公司 | Hydrocracking technological method for processing inferior raw material |
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| CN101240193B (en) * | 2007-02-09 | 2011-06-22 | 中国石油化工股份有限公司 | Coal tar multistage hydrogenation treatment technique |
| CN101294107B (en) * | 2007-04-24 | 2011-11-30 | 中国石油化工股份有限公司 | Method for preparing fuel oil with coal oil hydrogenation |
| JP2011517470A (en) * | 2008-04-06 | 2011-06-09 | ユーオーピー エルエルシー | Fuel and fuel blend components from biomass-derived pyrolysis oil |
| CN101885982B (en) * | 2010-06-23 | 2013-04-10 | 煤炭科学研究总院 | Hydrogenation method for coal tar suspension bed of heterogeneous catalyst |
| CN102311782B (en) * | 2010-06-29 | 2013-11-27 | 中国石油化工股份有限公司 | Method for producing diesel oil by purifying coal tar through hydrogenating |
| CN101979469B (en) * | 2010-11-17 | 2013-05-15 | 湖南长岭石化科技开发有限公司 | Method for removing free oxygen from inferior hydrogenation raw oil |
| CN101979470B (en) * | 2010-11-17 | 2013-05-15 | 湖南长岭石化科技开发有限公司 | Method for removing free oxygen from inferior hydrogenated feedstock oil |
| CN102604675A (en) * | 2012-03-30 | 2012-07-25 | 宁波金远东工业科技有限公司 | Coal tar hydrogenation and fractionation device |
| CN102851066B (en) * | 2012-08-27 | 2014-08-13 | 王小英 | Two-stage combined hydrogenation process of coal tar |
| CN102851073B (en) * | 2012-08-27 | 2014-08-13 | 王小英 | Medium and low temperature combination processing method of coal tar |
| CN104449817B (en) * | 2014-12-29 | 2016-05-04 | 七台河宝泰隆煤化工股份有限公司 | The method of diesel oil is produced in a kind of hydrocracking |
| CN106701178B (en) * | 2015-11-13 | 2018-03-23 | 中石化洛阳工程有限公司 | A kind of coal tar suspension bed method for hydrogen cracking |
| CN106635155A (en) * | 2016-11-03 | 2017-05-10 | 兰州兰石集团有限公司 | Efficient-residual-heat-utilization system for light-fraction conversion of coal tar and method |
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2006
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| GB2148937A (en) * | 1983-11-03 | 1985-06-05 | Chevron Res | Two-stage petroleum residuum hydroconversion using a countercurrent gas-liquid first stage |
| CN1676583A (en) * | 2004-07-14 | 2005-10-05 | 王守峰 | Medium-high-temperature coal tar hydro cracking process |
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| GB 2148937 A,全文. |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103059944A (en) * | 2011-10-21 | 2013-04-24 | 中国石油化工股份有限公司 | Hydrocracking technological method for processing inferior raw material |
| CN103059944B (en) * | 2011-10-21 | 2015-04-01 | 中国石油化工股份有限公司 | Hydrocracking technological method for processing inferior raw material |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1876767A (en) | 2006-12-13 |
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