CN103666556A - Preparation method of petroleum coke - Google Patents
Preparation method of petroleum coke Download PDFInfo
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- CN103666556A CN103666556A CN201210322538.5A CN201210322538A CN103666556A CN 103666556 A CN103666556 A CN 103666556A CN 201210322538 A CN201210322538 A CN 201210322538A CN 103666556 A CN103666556 A CN 103666556A
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Abstract
The invention relates to a preparation method of petroleum coke. The preparation method comprises the steps: (1) carrying out reduced pressure distillation on catalytic cracking oil slurry, wherein the catalytic cracking oil slurry contains 0.5-2.5wt% of sulfur, 0.01-1wt% of ash and 1-20wt% of asphaltene; (2) mixing distillate oil with hydrogen gas, and then, enabling the mixture to be in sequential contact with a hydrogenation protecting agent and a hydrogenation refining agent, wherein the distillate oil is obtained in the step (1); (3) inputting a liquid hydrogenation product to a delayed coking unit to carry out thermal cracking reaction to obtain the petroleum coke, wherein the liquid hydrogenation product is obtained in the step (2). By using the method provided by the invention, high-quality needle coke can be produced by using poor-quality catalytic cracking oil slurry, not only is the source of production raw materials of the needle coke widened, but also the additional value of the poor-quality catalytic cracking oil slurry is increased.
Description
Technical field
The present invention relates to a kind of preparation method of refinery coke.
Background technology
Needle coke is the main raw material of manufacturing senior Graphite Electrodes, because its outward appearance has obvious needle-like or fibrous texture structure, therefore be called needle coke (Needle Coke).Needle coke has the series of advantages such as low thermal coefficient of expansion, low porosity, low-sulfur, low ash content, low-metal content, high conductivity and easy greying.The graphite product of being made by needle coke has high-density, high strength, high purity, high-crystallinity, electric-conductivity heat-conductivity high, low thermal coefficient of expansion, the low feature such as ablative, in national defence and metallurgical industry, be widely used, wherein the consumption in metallurgical industry is maximum.In metallurgical industry, the ultra high power made from needle coke (UHP) Graphite Electrodes can obviously improve efficiency, reduces power consumption and raw materials consumption, reduces environmental pollution.In recent years, along with the progress with Graphite Electrodes production technology that develops rapidly of domestic Electric furnace steel making industry, the demand of needle coke increases considerably.The annual production of current domestic needle coke is only 100,000 tons of left and right, and market has openings is every year up to more than 200,000 tons.
According to needle coke mechanism of coke formation, it is high that the ingredient requirement of production needle coke has aromaticity content, colloid, bituminous matter, ash content and low-sulfur content feature, and require raw material in thermal conversion processes, to have higher Mesophase Transformation temperature and wider Mesophase Transformation temperature range, the ingredient requirement of production high-quality needle coke is: density >1.0g/cm
3, the heavy % of aromaticity content >50, the heavy % of asphalt content <1.0, ash oontent <100 μ g/g, the heavy % of sulphur content <0.5.
Aspect raw material, produce the raw material that needle coke should be selected low-sulfur, low resin and asphalt, low ash content, generally adopt thermal cracking residue, Pintsch process ethylene bottom oil processed, furfural extract oil or fluid catalytic cracking decant oil etc.Raising along with raw material in poor quality and operating severity, catalytically cracked oil character also worse and worse, shows as ash content, resin and asphalt content and sulphur content more and more higher, and in refinery, catalytically cracked oil sulphur content is up to 1.6 heavy %, metal content reaches 0.7 heavy %, and bituminous matter reaches 14.6 heavy %.Such catalytically cracked oil obviously can not meet as the character requirement of producing needle-shape coke raw material, cannot produce qualified needle coke.
US20050284793 has introduced the technology of utilizing long residuum to prepare needle coke, to sulphur content in long residuum, will be controlled in 0.7 heavy %.
CN1098336C " combined technical method of residue hydrogenating and delaying coking " has proposed that residual oil, coker gas oil are entered to hydrogenation unit together with hydrogen and has carried out hydrogenation, then enter the combination process of delayed coker produces needle coke, needle coke CTE < 2.6 * 10
-6/ ℃, sulphur content is less than 0.7 heavy %.
CN1191321C " a kind of method of producing acicular petroleum coke from sulfur containing atmospheric " is the long residuum for sulfur-bearing, and by preparing needle coke after hydrofining, hydrodemetallation (HDM) and hydrogenating desulfurization, its raw material is sulfur containing atmospheric.
US4740293 has introduced thermo-cracking residual oil and has adopted delay coking process to produce the technique of needle coke with together with fluid catalytic cracking decant oil after hydrotreatment, and the blending ratio of thermo-cracking residual oil is 50%～75 heavy %.
US5167796 has introduced the hydrogenating desulfurization of sulfur-bearing fluid catalytic cracking decant oil process, can make the sulphur content of needle coke be less than 0.8 heavy %.
Above-mentioned prior art all cannot utilize catalytically cracked oil inferior to produce needle coke.
Summary of the invention
The technical problem that the present invention proposes and will solve is how rationally to utilize catalytically cracked oil inferior, improves its utility value.The invention provides a kind of preparation method of refinery coke, the method can utilize catalytically cracked oil inferior to produce high-quality petroleum coke, and the method can expand the raw material sources of high-quality petroleum coke, improves the added value of catalytically cracked oil inferior simultaneously.
A preparation method for refinery coke, comprising:
(1) catalytically cracked oil is carried out to underpressure distillation, cut out 315 ± 35 ℃～500 ℃ ± 20 ℃ cuts, the sulphur content of described catalytically cracked oil is the 0.5 heavy % in heavy %～2.5, and ash oontent is the 0.01 heavy % in heavy %～1, and asphalt content is the 1 heavy % in heavy %～20;
(2) distillate step (1) being obtained mixes laggard process furnace with hydrogen through raw oil pump supercharging, enter fixed bed hydrogenation reactor after heating, contacts successively with hydrogenation protecting agent with hydrofining agent; Hydrogenated oil carries out gas-liquid separation through high-pressure separator, liquid product goes out device, and gas mixes with stock oil after mixing with new hydrogen after compressor compression, and hydrogenation conditions is: temperature of reaction is 250 ℃～450 ℃, hydrogen dividing potential drop is 1MPa～15MPa, and volume space velocity is 0.1h
-1～2h
-1, hydrogen to oil volume ratio 100Nm
3/ m
3～1000Nm
3/ m
3;
(3) hydrogenation liquid product input delay coker step (2) being obtained, carries out heat cracking reaction, obtains coking dry gas, coker gasoline and coker gas oil, coker gas oil and refinery coke; Operational condition is: 420 ℃～530 ℃ of furnace outlet temperature, coke drum pressure 0.2MPa～1MPa, recycle ratio 0.5～1.
The present invention first utilizes underpressure distillation to remove most bituminous matters and the most of metal in catalytically cracked oil inferior; And then the cut cutting out is selected to hydrogenation, in the time of desulfurization, carry out modifying oil product; Finally by delayed coking, prepare high-quality needle coke.The present invention adopts the combination of three kinds of techniques, can utilize catalytically cracked oil inferior to carry out production high-quality needle coke, has both expanded the raw material sources of needle coke, improves again the added value of catalytically cracked oil inferior.
Embodiment
A preparation method for refinery coke, comprising:
(1) catalytically cracked oil is carried out to underpressure distillation, cut out 315 ± 35 ℃～500 ℃ ± 20 ℃ cuts, the sulphur content of described catalytically cracked oil is the 0.5 heavy % in heavy %～2.5, and ash oontent is the 0.01 heavy % in heavy %～1, and asphalt content is the 1 heavy % in heavy %～20;
(2) distillate step (1) being obtained mixes laggard process furnace with hydrogen through raw oil pump supercharging, enter fixed bed hydrogenation reactor after heating, contacts successively with hydrogenation protecting agent with hydrofining agent; Hydrogenated oil carries out gas-liquid separation through high-pressure separator, liquid product goes out device, and gas mixes with stock oil after mixing with new hydrogen after compressor compression, and hydrogenation conditions is: temperature of reaction is 250 ℃～450 ℃, hydrogen dividing potential drop is 1MPa～15MPa, and volume space velocity is 0.1h
-1～2h
-1, hydrogen to oil volume ratio 100Nm
3/ m
3～1000Nm
3/ m
3;
(3) hydrogenation liquid product input delay coker step (2) being obtained, carries out heat cracking reaction, obtains coking dry gas, coker gasoline and coker gas oil, coker gas oil and refinery coke; Operational condition is: 420 ℃～530 ℃ of furnace outlet temperature, coke drum pressure 0.2MPa～1MPa, recycle ratio 0.5～1.
In step (2), preferred hydrogenation conditions is: temperature of reaction is 300～420 ℃, and hydrogen dividing potential drop is 2～12MPa, and volume space velocity is 0.2～1.5h
-1, hydrogen to oil volume ratio 200Nm
3/ m
3～900Nm
3/ m
3.
In preferred situation, the total fill able volume of catalyzer in fixed-bed reactor of take is benchmark, and the percent by volume of hydrogenation protecting agent and hydrofining agent filling is respectively 2%～30% and 70%～98%.
In preferred situation, described hydrogenation protecting agent is Raschig ring shape, contain a kind of alumina supporter and load on molybdenum and/or the tungsten on this alumina supporter, and nickel and/or cobalt, the gross weight of hydrogenation protecting agent of take is benchmark, and in oxide compound, the content of molybdenum and/or tungsten is 1 % by weight～10 % by weight, the content of nickel and/or cobalt is 0.5 % by weight～3 % by weight; Described aluminum oxide is gama-alumina, and the pore volume of described hydrogenation protecting agent is not less than 0.50ml/g, is preferably not less than 0.60ml/g.Use this hydrogenation protecting agent can protect Primary Catalysts, extend the working time of hydrotreater.
In preferred situation, described Hydrobon catalyst contains a kind of carrier and loads on molybdenum and/or the tungsten on this carrier, and nickel and/or cobalt, the gross weight of catalyzer of take is benchmark, and in oxide compound, the content of molybdenum and/or tungsten is the 8 heavy % in heavy %～20, and the content of nickel and/or cobalt is the 0.3 heavy % in heavy %～8, and carrier is aluminum oxide and optional silicon oxide; The pore distribution of described carrier is that diameter is that the pore volume of 60 dust～100 dusts accounts for 75%～98% of total pore volume, and the pore volume of described Hydrobon catalyst is not less than 0.40ml/g.While adopting above-mentioned catalyzer to carry out hydrotreatment to the distillate that step (1) is obtained, not only the most of sulphur in raw material is removed, and three rings and the also increase to some extent of Fourth Ring aromatic hydrocarbons, hydrogenated oil can be used as the needle-shape coke raw material of high-quality.
One embodiment of the present invention are that hydrogenation liquid product that step (2) is obtained is separately as the raw material of step (3).
Another embodiment of the invention is that hydrogenation liquid product that step (2) is obtained mixes with other raw materials of producing high-quality petroleum cokes, jointly as the raw material of step (3).The raw material of described production high-quality petroleum coke is one or more in long residuum, vacuum residuum, thermal cracking residue, Pintsch process ethylene bottom oil processed, furfural extract oil and fluid catalytic cracking decant oil.
As the general knowledge of the art, delayed coking unit at least comprises a process furnace, two coke drums and a separation column.
Adopt method of the present invention, the yield of refinery coke (green coke) is greater than 43 heavy %(and accounts for coking raw material), the CTE of needle coke (ripe Jiao) is lower than 2.6 * 10
-6/ ℃, the sulphur content of needle coke is less than 0.5 heavy %.
Further illustrate by the following examples the present invention, but not thereby limiting the invention.
Embodiment 1
Raw material is catalytically cracked oil, and its character is listed in table 1.Underpressure distillation operational condition is 15mmHg, 410 ℃ of heating kettle temperature, and underpressure distillation material distributes as shown in table 2.Hydrogenation protecting agent adopts the RG-30B catalyzer of Shi Ke institute exploitation, and hydrofining agent adopts the exploitation RMS-30 of Shi Ke institute catalyzer, by Sinopec catalyzer branch office Chang Ling catalyst plant, produces.Hydrogenation reaction temperature is 375 ℃, hydrogen dividing potential drop 5.5MPa, hydrogen to oil volume ratio 500Nm
3/ m
3, volume space velocity is 1.2h
-1.The operational condition of delayed coking is: 440 ℃ of furnace outlet temperature, coke drum pressure 0.8MPa, recycle ratio 1.After raw materials pretreatment, the results are shown in Table 1, from the data of table 1 can be found out and process by underpressure distillation and selective hydrogenation, can make catalytically cracked oil inferior meet the feedstock property requirement of needle coke.Coke chemicals distribute in Table 3, and the character of refinery coke is as shown in table 4, show that the catalytically cracked oil inferior of high-sulfur, high ash content and high asphalt content can be prepared the needle coke product of high-quality after the processing of underpressure distillation-hydrofining-delayed coking combination process.
Catalytically cracked oil character before and after table 1 raw materials pretreatment
| Oil product title | Catalytic slurry | Catalytic slurry after underpressure distillation | Needle-shape coke raw material |
| Density (20 ℃)/(g/cm 3） | 1.0831 | 1.0591 | 1.0298 |
| Kinematic viscosity/(mm 2/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 content)/% | 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-components)/% | |||
| Stable hydrocarbon | 14.6 | 18.6 | 23.2 |
| Aromatic hydrocarbons | 65.6 | 70.4 | 67.1 |
| Colloid | 15.7 | 11.0 | 9.7 |
| Bituminous matter | 4.1 | <0.1 | <0.1 |
| W(aromatic hydrocarbons)/% | |||
| Thrcylic aromatic hydrocarbon | 9.4 | 10.2 | 18.4 |
| Fourth Ring aromatic hydrocarbons | 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/℃ | |||
| 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 |
Table 2 catalytically cracked oil underpressure distillation material distributes
| Underpressure distillation | Yield, w/% |
| Distilled oil (ideal composition) | 85.7 |
| Tower top is extracted oil (lightweight undesirable components) out | 2.2 |
| The low extraction oil of tower (heavy undesirable components) | 12.1 |
| Amount to | 100.0 |
Table 3 delayed coking product distributes
| Coke chemicals | Yield, w/% |
| Coking dry gas | 19.26 |
| Coker gasoline | 9.21 |
| Coker gas oil | 20.56 |
| Coker gas oil | 5.80 |
| Refinery coke | 45.17 |
| Add up to | 100.0 |
Table 4 refinery coke character
| Project | Yield, w/% |
| Coke (green coke) character | |
| w（S）/% | 0.41 |
| W(ash content)/% | 0.08 |
| W(volatile matter)/% | 8.9 |
| Coke (ripe Jiao) character | |
| w（S）/% | 0.26 |
| W(ash content)/% | 0.10 |
| W(volatile matter)/% | 0.8 |
| True density (20 ℃)/(g/cm 3） | 2.12 |
| CTE/(10 -6/℃) | 2.54 |
Embodiment 2
Raw material is the oil sample that catalytically cracked oil after pretreatment and vacuum residuum mix by a certain percentage, and its blending ratio and character are listed in table 5.Hydrogenation protecting agent adopts the RG-30B catalyzer of Shi Ke institute exploitation, and hydrofining agent adopts the exploitation RMS-30 of Shi Ke institute catalyzer, by Sinopec catalyzer branch office Chang Ling catalyst plant, produces.Hydrogenation reaction temperature is 345 ℃, hydrogen dividing potential drop 4.0MPa, hydrogen to oil volume ratio 300Nm
3/ m
3, volume space velocity is 1.0h
-1.The operational condition of delayed coking is: 430 ℃ of furnace outlet temperature, coke drum pressure 0.8MPa, recycle ratio 0.9.The results are shown in Table 5 before and after catalytic slurry pre-treatment, from the data of table 5, can find out that pretreated catalytically cracked oil inferior can meet the feedstock property requirement of needle coke.Coke chemicals distribute in Table 6, the character of refinery coke is as shown in table 7, show that the catalytically cracked oil inferior of the high ash content of high-sulfur and high asphalt content is after the processing of underpressure distillation-hydrofining-delayed coking combination process, can be with other raw materials as after vacuum residuum mix, the needle coke product of production high-quality.
The pretreated catalytically cracked oil of table 5 and Vacuum Residue Properties
| Oil product title | Catalytic slurry | Pretreated catalytic slurry | Vacuum residuum |
| W(coking raw material forms)/% | - | 85 | 15 |
| Density (20 ℃)/(g/cm 3） | 1.0743 | 1.0158 | 0.9908 |
| Kinematic viscosity/(mm 2/s） | |||
| 50℃ | ＞3000 | 404.5 | ＞3000 |
| 80℃ | 605.4 | 42.23 | ＞3000 |
| W(carbon residue)/% | 24.1 | 1.45 | 16.7 |
| W(ash content)/% | 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-components)/% | |||
| Stable hydrocarbon | 15.6 | 33.1 | 15.3 |
| Aromatic hydrocarbons | 54.0 | 58.6 | 32.8 |
| Colloid | 17.6 | 8.3 | 50.9 |
| Bituminous matter | 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/℃ | |||
| 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 distributes
| Coke chemicals | Yield, w/% |
| Coking dry gas | 13.80 |
| Coker gasoline | 11.94 |
| Coker gas oil | 25.01 |
| Coker gas oil | 6.03 |
| Refinery coke | 43.22 |
| Add up to | 100.0 |
Table 7 refinery coke character
| Project | Yield, w/% |
| Coke (green coke) character | |
| w（S）/% | 0.59 |
| W(ash content)/% | 0.07 |
| W(volatile matter)/% | 7.8 |
| Coke (ripe Jiao) character | |
| w（S）/% | 0.35 |
| W(ash content)/% | 0.09 |
| W(volatile matter)/% | 0.7 |
| True density (20 ℃)/(g/cm 3） | 2.12 |
| CTE/(10 -6/℃) | 2.48 |
Claims (6)
1. a preparation method for refinery coke, comprising:
(1) catalytically cracked oil is carried out to underpressure distillation, cut out 315 ± 35 ℃～500 ℃ ± 20 ℃ cuts, the sulphur content of described catalytically cracked oil is the 0.5 heavy % in heavy %～2.5, and ash oontent is the 0.01 heavy % in heavy %～1, and asphalt content is the 1 heavy % in heavy %～20;
(2) distillate step (1) being obtained mixes laggard process furnace with hydrogen through raw oil pump supercharging, enter fixed bed hydrogenation reactor after heating, contacts successively with hydrogenation protecting agent with hydrofining agent; Hydrogenated oil carries out gas-liquid separation through high-pressure separator, liquid product goes out device, and gas mixes with stock oil after mixing with new hydrogen after compressor compression, and hydrogenation conditions is: temperature of reaction is 250 ℃～450 ℃, hydrogen dividing potential drop is 1MPa～15MPa, and volume space velocity is 0.1h
-1～2h
-1, hydrogen to oil volume ratio 100Nm
3/ m
3～1000Nm
3/ m
3;
(3) hydrogenation liquid product input delay coker step (2) being obtained, carries out heat cracking reaction, obtains coking dry gas, coker gasoline and coker gas oil, coker gas oil and refinery coke; Operational condition is: 420 ℃～530 ℃ of furnace outlet temperature, coke drum pressure 0.2MPa～1MPa, recycle ratio 0.5～1.
2. in accordance with the method for claim 1, it is characterized in that, in step (2), hydrogenation conditions is: temperature of reaction is 300～420 ℃, and hydrogen dividing potential drop is 2～12MPa, and volume space velocity is 0.2～1.5h
-1, hydrogen to oil volume ratio 200Nm
3/ m
3～900Nm
3/ m
3.
3. in accordance with the method for claim 1, it is characterized in that, the total fill able volume of catalyzer in fixed-bed reactor of take is benchmark, and the percent by volume of hydrogenation protecting agent and hydrofining agent filling is respectively 2%～30% and 70%～98%.
4. in accordance with the method for claim 1, it is characterized in that, described hydrogenation protecting agent is Raschig ring shape, contain a kind of alumina supporter and load on molybdenum and/or the tungsten on this alumina supporter, and nickel and/or cobalt, the gross weight of hydrogenation protecting agent of take is benchmark, and in oxide compound, the content of molybdenum and/or tungsten is 1 % by weight～10 % by weight, and the content of nickel and/or cobalt is 0.5 % by weight～3 % by weight; Described aluminum oxide is gama-alumina, and the pore volume of described hydrogenation protecting agent is not less than 0.50ml/g.
5. in accordance with the method for claim 1, it is characterized in that, described Hydrobon catalyst contains a kind of carrier and loads on molybdenum and/or the tungsten on this carrier, and nickel and/or cobalt, the gross weight of catalyzer of take is benchmark, and in oxide compound, the content of molybdenum and/or tungsten is the 8 heavy % in heavy %～20, the content of nickel and/or cobalt is the 0.3 heavy % in heavy %～8, and carrier is aluminum oxide and optional silicon oxide; The pore distribution of described carrier is that diameter is that the pore volume of 60 dust～100 dusts accounts for 75%～98% of total pore volume, and the pore volume of described Hydrobon catalyst is not less than 0.40ml/g.
6. in accordance with the method for claim 1, it is characterized in that, the hydrogenation liquid product that step (2) is obtained mixes with other raw materials of producing high-quality petroleum cokes, jointly as the raw material of step (3); The raw material of described production high-quality petroleum coke is one or more in long residuum, vacuum residuum, thermal cracking residue, Pintsch process ethylene bottom oil processed, furfural extract oil and fluid catalytic cracking decant oil.
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|---|---|---|---|---|
| CN104962314A (en) * | 2015-06-18 | 2015-10-07 | 山东菏泽德泰化工有限公司 | System and method for producing raw material of needle coke by oil slurry |
| CN112342059A (en) * | 2019-08-06 | 2021-02-09 | 中国石油化工股份有限公司 | Method for blending catalytic cracking slurry oil in delayed coking unit |
| CN113122333A (en) * | 2019-12-31 | 2021-07-16 | 中国石油化工股份有限公司 | Production method and system of low-sulfur petroleum coke |
| CN113122329A (en) * | 2019-12-31 | 2021-07-16 | 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 |
| CN114456841A (en) * | 2020-10-22 | 2022-05-10 | 中国石油化工股份有限公司 | Petroleum coke and preparation method thereof, and carbon negative electrode material and preparation method thereof |
| CN114763496A (en) * | 2021-01-13 | 2022-07-19 | 中国石油化工股份有限公司 | Petroleum coke and preparation method thereof, carbon negative electrode material and preparation method thereof |
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|---|---|---|---|---|
| CN104962314A (en) * | 2015-06-18 | 2015-10-07 | 山东菏泽德泰化工有限公司 | System and method for producing raw material of needle coke by oil slurry |
| CN112342059A (en) * | 2019-08-06 | 2021-02-09 | 中国石油化工股份有限公司 | Method for blending catalytic cracking slurry oil in delayed coking unit |
| 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 |
| CN113122333A (en) * | 2019-12-31 | 2021-07-16 | 中国石油化工股份有限公司 | Production method and system of low-sulfur petroleum coke |
| CN113122329A (en) * | 2019-12-31 | 2021-07-16 | 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 |
| 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 |
| CN114456841A (en) * | 2020-10-22 | 2022-05-10 | 中国石油化工股份有限公司 | Petroleum coke and preparation method thereof, and carbon negative electrode material and preparation method thereof |
| 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 |
| CN114763496A (en) * | 2021-01-13 | 2022-07-19 | 中国石油化工股份有限公司 | Petroleum coke and preparation method thereof, carbon negative electrode 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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