CN103666556B - A kind of preparation method of petroleum coke - Google Patents
A kind of preparation method of petroleum coke Download PDFInfo
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Abstract
The present invention relates to the preparation method of a kind of petroleum coke, including: (1) carries out decompression distillation to catalytic cracked oil pulp, and the sulfur content of described catalytic cracked oil pulp is 0.5 weight %～2.5 weight %, and content of ashes is 0.01 weight %～1 weight %, and asphalt content is 1 weight %～20 weight %；(2), after the distillate that step (1) obtains being mixed with hydrogen, contact with hydrogenation protecting agent and hydrofinishing agent successively；(3) hydrogenated liquid product input delay coking plant step (2) obtained, carries out heat cracking reaction, obtains petroleum coke.Use method of the invention, it is possible to utilize catalytic cracked oil pulp inferior to produce high-quality needle coke, both expanded the raw material sources of needle coke, and improved again the added value of catalytic cracked oil pulp inferior.
Description
Technical field
The present invention relates to the preparation method of a kind of petroleum coke.
Background technology
Needle coke is the primary raw material manufacturing senior graphite electrode, because its outward appearance has obvious needle-like or fibre
Dimension shape texture structure, therefore referred to as needle coke (Needle Coke).Needle coke have low thermal coefficient of expansion,
The series of advantages such as low-porosity, low-sulfur, low ash, low-metal content, high conductivity and easy graphitization.
The graphite product being made up of needle coke has high density, high intensity, high-purity, high-crystallinity, high connductivity
Heat conductivity, low thermal coefficient of expansion, the low feature such as ablative, obtain widely in national defence and metallurgical industry
Application, wherein the consumption in metallurgical industry is maximum.In metallurgical industry, the superelevation merit made with needle coke
Rate (UHP) graphite electrode can significantly improve efficiency, reduces power consumption and raw materials consumption, reduces
Environmental pollution.In recent years, developing rapidly and graphite electrode production technology along with the industry of domestic electric furnace steel making
Progress, the demand of needle coke increases considerably.The annual production of current domestic needle coke is only 100,000
About Dun, market has openings up to more than 200,000 tons every year.
According to needle coke mechanism of coke form ation, it is high that the ingredient requirement of production needle coke has arene content, colloid,
Asphalitine, ash and low-sulfur content feature, and it is higher to require that raw material has in thermal conversion processes
Mesophase Transformation temperature and wider Mesophase Transformation temperature range, produce the ingredient requirement of high-quality needle coke
For: density > 1.0g/cm3, arene content>and 50 weight %, asphalt content<1.0 weight %, content of ashes<100
μ g/g, sulfur content < 0.5 weight %.
In terms of raw material, produce needle coke and should select low-sulfur, low resin and asphalt, low ash content
Raw material, typically uses thermal cracking residue, Pintsch process ethylene bottom oil, furfural extract oil or catalytic cracking
Clarified oil etc..Along with raw material in poor quality and the raising of operating severity, catalytic cracked oil pulp character is the most more come
The poorest, show as ash, resin and asphalt content and sulfur content more and more higher, catalytic cracking in refinery
Slurry oil sulfur content is up to 1.6 weight %, and tenor reaches 0.7 weight %, and asphalitine reaches 14.6 weight %.This
The catalytic cracked oil pulp of sample obviously can not meet as the Property requirements producing needle-shape coke raw material, it is impossible to produces
Qualified needle coke.
US20050284793 describes the technology utilizing reduced crude to prepare needle coke, in reduced crude
Sulfur content to control within 0.7 weight %.
CN1098336C " combined technical method of residue hydrogenating and delaying coking " propose by residual oil,
Coker gas oil enters hydrogenation plant together with hydrogen and is hydrogenated with, and produces subsequently into delayed coking unit
The group technology of needle coke, needle coke CTE ＜ 2.6 × 10-6/ DEG C, sulfur content is less than 0.7 weight %.
CN1191321C " a kind of method producing acicular petroleum coke from sulfur containing atmospheric " is for sulfur-bearing
Reduced crude, by preparing needle coke after hydrofinishing, HDM and hydrodesulfurization, its raw material
It it is sulfur containing atmospheric.
US4740293 describes thermal cracking residual oil and uses together with the catalytic cracking clarified oil after hydrotreating
Delay coking process produces the technique of needle coke, and the mixed proportion of thermal cracking residual oil is 50%～75 heavily %.
US5167796 describes sulfur-bearing catalytic cracking clarified oil through hydrodesulfurization, can make needle coke
Sulfur content is less than 0.8 weight %.
Above-mentioned prior art all cannot utilize catalytic cracked oil pulp inferior to produce needle coke.
Summary of the invention
The present invention proposes and to solve the technical problem that to be how Appropriate application poor quality catalytic cracked oil pulp, carries
Its value high.The invention provides the preparation method of a kind of petroleum coke, the method can utilize poor quality
Catalytic cracked oil pulp produces high-quality petroleum coke, and the method can expand the raw materials for production of high-quality petroleum coke and come
Source, improves the added value of catalytic cracked oil pulp inferior simultaneously.
A kind of preparation method of petroleum coke, including:
(1) catalytic cracked oil pulp is carried out decompression distillation, cuts out 315 ± 35 DEG C～500 DEG C ± 20 DEG C
Fraction, the sulfur content of described catalytic cracked oil pulp is 0.5 weight %～2.5 weight %, and content of ashes is 0.01
Weight %～1 weight %, asphalt content is 1 weight %～20 weight %；
(2) distillate step (1) obtained mixes laggard heating furnace through raw oil pump supercharging with hydrogen,
Enter fixed bed hydrogenation reactor after heating, contact with hydrogenation protecting agent and hydrofinishing agent successively;Hydrogenation
Generating oil and carry out gas-liquid separation through high-pressure separator, fluid product goes out device, and gas is after compressor compresses
Mixing with raw oil after mixing with new hydrogen, hydrogenation conditions is: reaction temperature is 250 DEG C～450 DEG C,
Hydrogen dividing potential drop is 1MPa～15MPa, and volume space velocity is 0.1h-1～2h-1, hydrogen to oil volume ratio 100Nm3/m3~
1000Nm3/m3；
(3) hydrogenated liquid product input delay coking plant step (2) obtained, carries out thermal cracking
Reaction, obtains coking dry gas, coker gasoline and coker gas oil, coker gas oil and petroleum coke；Operation bar
Part is: furnace outlet temperature 420 DEG C～530 DEG C, coke drum pressure 0.2MPa～1MPa, recycle ratio
0.5～1.
The present invention first with the most asphalitines in decompression distillation removing catalytic cracked oil pulp inferior and
Major part metal；Carry out the fraction cut out the most again selecting hydrogenation, carry out oil product while desulfurization and change
Matter；High-quality needle coke is prepared finally by delayed coking.The present invention uses the combination of three kinds of techniques, energy
Enough utilizations catalytic cracked oil pulp inferior produces high-quality needle coke, and the raw materials for production both having expanded needle coke come
Source, improves again the added value of catalytic cracked oil pulp inferior.
Detailed description of the invention
A kind of preparation method of petroleum coke, including:
(1) catalytic cracked oil pulp is carried out decompression distillation, cuts out 315 ± 35 DEG C～500 DEG C ± 20 DEG C
Fraction, the sulfur content of described catalytic cracked oil pulp is 0.5 weight %～2.5 weight %, and content of ashes is 0.01
Weight %～1 weight %, asphalt content is 1 weight %～20 weight %；
(2) distillate step (1) obtained mixes laggard heating furnace through raw oil pump supercharging with hydrogen,
Enter fixed bed hydrogenation reactor after heating, contact with hydrogenation protecting agent and hydrofinishing agent successively;Hydrogenation
Generating oil and carry out gas-liquid separation through high-pressure separator, fluid product goes out device, and gas is after compressor compresses
Mixing with raw oil after mixing with new hydrogen, hydrogenation conditions is: reaction temperature is 250 DEG C～450 DEG C,
Hydrogen dividing potential drop is 1MPa～15MPa, and volume space velocity is 0.1h-1～2h-1, hydrogen to oil volume ratio 100Nm3/m3~
1000Nm3/m3；
(3) hydrogenated liquid product input delay coking plant step (2) obtained, carries out thermal cracking
Reaction, obtains coking dry gas, coker gasoline and coker gas oil, coker gas oil and petroleum coke；Operation bar
Part is: furnace outlet temperature 420 DEG C～530 DEG C, coke drum pressure 0.2MPa～1MPa, recycle ratio
0.5～1.
In step (2), preferred hydrogenation conditions is: reaction temperature is 300～420 DEG C, and hydrogen divides
Pressure is 2～12MPa, and volume space velocity is 0.2～1.5h-1, hydrogen to oil volume ratio 200Nm3/m3～900Nm3/m3。
In the case of You Xuan, in fixed bed reactors on the basis of the total fill able volume of catalyst, hydrogenation is protected
The percentage by volume protecting agent and hydrofinishing agent filling is respectively 2%～30% and 70%～98%.
In the case of You Xuan, described hydrogenation protecting agent is Raschig ring shape, containing a kind of alumina support with negative
It is loaded in the molybdenum on this alumina support and/or tungsten, and nickel and/or cobalt, with the gross weight of hydrogenation protecting agent
On the basis of, and in terms of oxide, the content of molybdenum and/or tungsten is 1 weight %～10 weight %, nickel and/or cobalt
Content be 0.5 weight %～3 weight %；Described aluminium oxide is gama-alumina, described hydrogenation protecting
The pore volume of agent is not less than 0.50ml/g, preferably not less than 0.60ml/g.Use this hydrogenation protecting agent can
Protection major catalyst, extends the operation time of hydrotreater.
In the case of You Xuan, described Hydrobon catalyst contains a kind of carrier and loads on this carrier
Molybdenum and/or tungsten, and nickel and/or cobalt, on the basis of the gross weight of catalyst, and in terms of oxide,
The content of molybdenum and/or tungsten is 8 weight %～20 weight %, and the content of nickel and/or cobalt is 0.3 weight %～8 weight %, carries
Body is aluminium oxide and optional silicon oxide；The pore size distribution of described carrier is a diameter of 60 angstroms～hole of 100 angstroms
Holding and account for the 75%～98% of total pore volume, the pore volume of described Hydrobon catalyst is not less than 0.40ml/g.Adopt
With above-mentioned catalyst to when the distillate that step (1) obtains is carried out hydrotreating, not only by raw material
In the removing of most of sulfur, and three rings and four PAHs also have and are increased, and hydrogenated oil can conduct
The needle-shape coke raw material of high-quality.
One embodiment of the present invention is that hydrogenated liquid product step (2) obtained is separately as step
Suddenly the raw material of (3).
Another embodiment of the invention is that hydrogenated liquid product step (2) obtained is raw with other
Produce the raw material mixing of high-quality petroleum coke, collectively as the raw material of step (3).Described production high-quality stone
The raw material of oil coke is reduced crude, decompression residuum, thermal cracking residue, Pintsch process ethylene bottom oil, bran
One or more in aldehyde tapped oil and catalytic cracking clarified oil.
As the general knowledge of the art, delayed coking unit at least includes a heating furnace, two coke
Tower and a fractionating column.
The method using the present invention, the yield of petroleum coke (green coke) accounts for coking raw material more than 43 weight %(),
The CTE of needle coke (ripe Jiao) is less than 2.6 × 10-6/ DEG C, the sulfur content of needle coke is less than 0.5 weight %.
Further illustrate the present invention by the following examples, but not thereby limiting the invention.
Embodiment 1
Raw material is catalytic cracked oil pulp, and its character is listed in table 1.Decompression distillation procedure condition is 15mmHg,
Heating kettle temperature 410 DEG C, decompression distilling material distribution is as shown in table 2.Hydrogenation protecting agent uses Shi Keyuan
Exploitation RG-30B catalyst, hydrofinishing agent use Shi Ke institute exploitation RMS-30 catalyst, by
Effect of Catalysis In Petrochemistry agent branch company of state Chang Ling catalyst plant produces.Hydrogenation reaction temperature is 375 DEG C, hydrogen dividing potential drop
5.5MPa, hydrogen to oil volume ratio 500Nm3/m3, volume space velocity is 1.2h-1.The operating condition of delayed coking is:
Furnace outlet temperature 440 DEG C, coke drum pressure 0.8MPa, recycle ratio 1.Knot after pretreatment of raw material
Fruit is shown in Table 1, can be seen that after being processed by decompression distillation and selective hydrogenation from the data of table 1, it is possible to
Catalytic cracked oil pulp inferior is made to meet the feedstock property requirement of needle coke.Coke chemicals distribution is shown in Table 3, stone
The character of oil coke is as shown in table 4, shows the catalytic cracking inferior of high-sulfur, high ash and high asphalt content
Slurry oil can prepare the pin of high-quality after decompression distillation-hydrofinishing-delayed coking group technology processing
Shape Jiao's product.
Catalytic cracked oil pulp character before and after table 1 pretreatment of raw material
| Oil product title | Catalytic slurry | Catalytic slurry after decompression distillation | Needle-shape coke raw material |
| Density (20 DEG C)/(g/cm3) | 1.0831 | 1.0591 | 1.0298 |
| Kinematic viscosity/(mm2/ s) | |||
| 50℃ | 188.9 | 18.32 | 14.44 |
| 80℃ | 44.69 | 9.147 | 7.468 |
| W(carbon residue)/% | 9.68 | 2.36 | 0.50 |
| W(ash)/% | 0.24 | 0.009 | <0.002 |
| W(element)/% | |||
| C | 90.96 | 90.71 | 90.60 |
| H | 7.64 | 8.33 | 9.15 |
| S | 1.0 | 0.87 | 0.24 |
| N | 0.22 | 0.19 | 0.17 |
| W(tetra-component)/% | |||
| Saturated hydrocarbons | 14.6 | 18.6 | 23.2 |
| Aromatic hydrocarbons | 65.6 | 70.4 | 67.1 |
| Colloid | 15.7 | 11.0 | 9.7 |
| Asphalitine | 4.1 | <0.1 | <0.1 |
| W(aromatic hydrocarbons)/% | |||
| Thrcylic aromatic hydrocarbon | 9.4 | 10.2 | 18.4 |
| Four PAHs | 28.9 | 31.7 | 26.7 |
| W(metal)/(μ g/g) | |||
| Al | 350 | 8.2 | 5.2 |
| Ca | 17.6 | 1.3 | 1.1 |
| Cu | 0.1 | <0.1 | <0.1 |
| Fe | 14.9 | 5.8 | 1.2 |
| Na | 3.6 | 0.9 | |
| Ni | 15.5 | 1.1 | 0.5 |
| V | 2.0 | <0.1 | 0.2 |
| Boiling range/DEG C | |||
| Initial boiling point | 231 | 275 | 249 |
| 5% | 322 | 302 | 284 |
| 10% | 396 | 345 | 336 |
| 30% | 439 | 422 | 410 |
| 50% | 463 | 440 | 427 |
| 70% | 497 | 451 | 443 |
| 90% | 625(88%) | 495 | 481 |
The decompression distilling material distribution of table 2 catalytic cracked oil pulp
| Decompression distillation | Yield, w/% |
| Distillate oil (ideal composition) | 85.7 |
| Tower top tapped oil (lightweight undesirable components) | 2.2 |
| The low tapped oil of tower (heavy undesirable components) | 12.1 |
| Amount to | 100.0 |
Table 3 delayed coking product slates
| Coke chemicals | Yield, w/% |
| Coking dry gas | 19.26 |
| Coker gasoline | 9.21 |
| Coker gas oil | 20.56 |
| Coker gas oil | 5.80 |
| Petroleum coke | 45.17 |
| Add up to | 100.0 |
Table 4 petroleum coke character
| Project | Yield, w/% |
| Coke (green coke) character | |
| W(S)/% | 0.41 |
| W(ash)/% | 0.08 |
| W(volatile matter)/% | 8.9 |
| Coke (ripe Jiao) character | |
| W(S)/% | 0.26 |
| W(ash)/% | 0.10 |
| W(volatile matter)/% | 0.8 |
| True density (20 DEG C)/(g/cm3) | 2.12 |
| CTE/(10-6/℃) | 2.54 |
Embodiment 2
The oil sample that raw material is catalytic cracked oil pulp after pretreatment and decompression residuum mixes by a certain percentage,
Its mixed proportion and character are listed in table 5.Hydrogenation protecting agent uses the RG-30B catalyst of Shi Ke institute exploitation,
Hydrofinishing agent uses Shi Ke institute exploitation RMS-30 catalyst, by Sinopec catalyst branch company Chang Ling
Catalyst plant produces.Hydrogenation reaction temperature is 345 DEG C, hydrogen dividing potential drop 4.0MPa, hydrogen to oil volume ratio
300Nm3/m3, volume space velocity is 1.0h-1.The operating condition of delayed coking is: furnace outlet temperature 430
DEG C, coke drum pressure 0.8MPa, recycle ratio 0.9.The results are shown in Table 5 before and after catalytic slurry pretreatment,
Can be seen that pretreated catalytic cracked oil pulp inferior can meet the feed stock of needle coke from the data of table 5
Matter requirement.Coke chemicals distribution is shown in Table 6, and the character of petroleum coke is as shown in table 7, shows high-sulfur height ash
Decompression distillation-hydrofinishing-delayed coking group is passed through with the catalytic cracked oil pulp inferior of high asphalt content
After closing processes, after can mixing such as decompression residuum with other raw materials, produce the needle coke product of high-quality.
The pretreated catalytic cracked oil pulp of table 5 and Vacuum Residue Properties
| Oil product title | Catalytic slurry | Pretreated catalytic slurry | Decompression residuum |
| W(coking raw material forms)/% | - | 85 | 15 |
| Density (20 DEG C)/(g/cm3) | 1.0743 | 1.0158 | 0.9908 |
| Kinematic viscosity/(mm2/ s) | |||
| 50℃ | ＞ 3000 | 404.5 | ＞ 3000 |
| 80℃ | 605.4 | 42.23 | ＞ 3000 |
| W(carbon residue)/% | 24.1 | 1.45 | 16.7 |
| W(ash)/% | 0.61 | ＜ 0.001 | 0.053 |
| W(element)/% | |||
| C | 89.18 | 89.89 | 86.01 |
| H | 8.74 | 9.19 | 11.09 |
| S | 1.30 | 0.26 | 1.29 |
| N | 0.34 | 0.14 | 0.81 |
| W(tetra-component)/% | |||
| Saturated hydrocarbons | 15.6 | 33.1 | 15.3 |
| Aromatic hydrocarbons | 54.0 | 58.6 | 32.8 |
| Colloid | 17.6 | 8.3 | 50.9 |
| Asphalitine | 12.8 | <0.1 | 1.0 |
| W(metal)/(μ g/g) | |||
| Al | 642 | 0.2 | 2.8 |
| Ca | 11.8 | 0.3 | 79.4 |
| Cu | <0.1 | 0.3 | 0.1 |
| Fe | 21.9 | 0.3 | 42.7 |
| Na | 10.2 | 0.5 | 2.7 |
| Ni | 13.0 | 0.3 | 53.0 |
| V | 22.6 | <0.1 | 8.4 |
| Boiling range/DEG C | |||
| Initial boiling point | 367 | 294 | 265 |
| 5% | 422 | 373 | 498 |
| 10% | 452 | 406 | 530 |
| 30% | 511 | 444 | 597 |
| 50% | 547 | 478 | 623(42%) |
| 70% | 584 | 505 | - |
| 90% | 626 | 529 | - |
Table 6 delayed coking product slates
| Coke chemicals | Yield, w/% |
| Coking dry gas | 13.80 |
| Coker gasoline | 11.94 |
| Coker gas oil | 25.01 |
| Coker gas oil | 6.03 |
| Petroleum coke | 43.22 |
| Add up to | 100.0 |
Table 7 petroleum coke character
| Project | Yield, w/% |
| Coke (green coke) character | |
| W(S)/% | 0.59 |
| W(ash)/% | 0.07 |
| W(volatile matter)/% | 7.8 |
| Coke (ripe Jiao) character | |
| W(S)/% | 0.35 |
| W(ash)/% | 0.09 |
| W(volatile matter)/% | 0.7 |
| True density (20 DEG C)/(g/cm3) | 2.12 |
| CTE/(10-6/℃) | 2.48 |
Claims (4)
1. a preparation method for petroleum coke, including:
(1) catalytic cracked oil pulp is carried out decompression distillation, cuts out 315 ± 35 DEG C～500 DEG C ± 20 DEG C
Fraction, the sulfur content of described catalytic cracked oil pulp is 0.5 weight %～2.5 weight %, and content of ashes is 0.01
Weight %～1 weight %, asphalt content is 1 weight %～20 weight %；
(2) distillate step (1) obtained mixes laggard heating furnace through raw oil pump supercharging with hydrogen,
Enter fixed bed hydrogenation reactor after heating, contact with hydrogenation protecting agent and hydrofinishing agent successively；Hydrogenation
Generating oil and carry out gas-liquid separation through high-pressure separator, fluid product goes out device, and gas is after compressor compresses
Mixing with raw oil after mixing with new hydrogen, hydrogenation conditions is: reaction temperature is 250 DEG C～450 DEG C,
Hydrogen dividing potential drop is 1MPa～15MPa, and volume space velocity is 0.1h-1～2h-1, hydrogen to oil volume ratio 100Nm3/m3~
1000Nm3/m3；
Described hydrogenation protecting agent is Raschig ring shape, contains a kind of alumina support and is supported on this carrying alumina
Molybdenum on body and/or tungsten, and nickel and/or cobalt, on the basis of the gross weight of hydrogenation protecting agent, and with oxygen
The content of compound meter, molybdenum and/or tungsten be the content of 1 weight %～10 weight %, nickel and/or cobalt be 0.5
Weight %～3 weight %；Described aluminium oxide is gama-alumina, and the pore volume of described hydrogenation protecting agent is the least
In 0.50ml/g；
Described Hydrobon catalyst contains a kind of carrier and loads molybdenum on this carrier and/or tungsten,
And nickel and/or cobalt, on the basis of the gross weight of catalyst, and in terms of oxide, containing of molybdenum and/or tungsten
Amount be 8 weight %～20 weight %, the content of nickel and/or cobalt be 0.3 weight %～8 weight %, carrier be aluminium oxide and
Optional silicon oxide；The pore size distribution of described carrier is that the pore volume of a diameter of 60 angstroms～100 angstroms accounts for total pore volume
75%～98%, the pore volume of described Hydrobon catalyst is not less than 0.40ml/g；
(3) hydrogenated liquid product input delay coking plant step (2) obtained, carries out thermal cracking
Reaction, obtains coking dry gas, coker gasoline and coker gas oil, coker gas oil and petroleum coke；Operation bar
Part is: furnace outlet temperature 420 DEG C～530 DEG C, coke drum pressure 0.2MPa～1MPa, recycle ratio
0.5～1.
The most in accordance with the method for claim 1, it is characterised in that in step (2), hydrogenation reaction
Condition is: reaction temperature is 300～420 DEG C, and hydrogen dividing potential drop is 2～12MPa, volume space velocity be 0.2～
1.5h-1, hydrogen to oil volume ratio 200Nm3/m3～900Nm3/m3。
The most in accordance with the method for claim 1, it is characterised in that with catalyst in fixed bed reactors
Total fill able volume on the basis of, hydrogenation protecting agent and hydrofinishing agent filling percentage by volume be respectively
2%～30% and 70%～98%.
The most in accordance with the method for claim 1, it is characterised in that the hydrogenation that step (2) is obtained
The raw material that fluid product produces high-quality petroleum coke with other mixes, collectively as the raw material of step (3)；
The described raw material producing high-quality petroleum coke is reduced crude, decompression residuum, thermal cracking residue, high anneal crack
Solve one or more in ethylene bottom oil processed, furfural extract oil and catalytic cracking clarified oil.
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| CN104962314B (en) * | 2015-06-18 | 2017-10-03 | 山东菏泽德泰化工有限公司 | Slurry oil produces the system and method for needle-shape coke raw material |
| CN112342059B (en) * | 2019-08-06 | 2022-04-12 | 中国石油化工股份有限公司 | Method for blending catalytic cracking slurry oil in delayed coking unit |
| CN113122329B (en) * | 2019-12-31 | 2022-06-07 | 中国石油化工股份有限公司 | Method and system for co-producing needle coke and low-sulfur petroleum coke |
| CN113122333B (en) * | 2019-12-31 | 2022-06-07 | 中国石油化工股份有限公司 | Production method and system of low-sulfur petroleum coke |
| CN114456841B (en) * | 2020-10-22 | 2024-01-09 | 中国石油化工股份有限公司 | Petroleum coke and preparation method thereof, carbon anode material and preparation method thereof |
| CN114763496B (en) * | 2021-01-13 | 2023-09-05 | 中国石油化工股份有限公司 | Petroleum coke and preparation method thereof, carbon anode material and preparation method thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1872963A (en) * | 2005-05-31 | 2006-12-06 | 中国石油化工股份有限公司 | Method of treating raw material for producing acerate coke |
| CN101928601A (en) * | 2009-06-25 | 2010-12-29 | 中国石油化工股份有限公司 | Processing method for catalytic cracking heavy oil |
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| US4235703A (en) * | 1979-03-27 | 1980-11-25 | Conoco, Inc. | Method for producing premium coke from residual oil |
| CN1180055C (en) * | 2001-04-28 | 2004-12-15 | 中国石油化工股份有限公司 | Process for preparing acicular coke to remove solid particles from raw oil |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1872963A (en) * | 2005-05-31 | 2006-12-06 | 中国石油化工股份有限公司 | Method of treating raw material for producing acerate coke |
| CN101928601A (en) * | 2009-06-25 | 2010-12-29 | 中国石油化工股份有限公司 | Processing method for catalytic cracking heavy oil |
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