CN103666556B - A kind of preparation method of petroleum coke - Google Patents

A kind of preparation method of petroleum coke Download PDF

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CN103666556B
CN103666556B CN201210322538.5A CN201210322538A CN103666556B CN 103666556 B CN103666556 B CN 103666556B CN 201210322538 A CN201210322538 A CN 201210322538A CN 103666556 B CN103666556 B CN 103666556B
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hydrogenation
coke
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范启明
申海平
刘自宾
阎龙
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Sinopec Research Institute of Petroleum Processing
China Petroleum and Chemical Corp
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Sinopec Research Institute of Petroleum Processing
China Petroleum and Chemical Corp
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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

A kind of preparation method of petroleum coke
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
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
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
CN116376596A (en) * 2022-12-27 2023-07-04 湖南长炼新材料科技股份公司 Production method of needle coke raw material

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