CN106867554A - A kind of method that utilization delay coking process produces needle-shape coke raw material - Google Patents
A kind of method that utilization delay coking process produces needle-shape coke raw material Download PDFInfo
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- CN106867554A CN106867554A CN201510920928.6A CN201510920928A CN106867554A CN 106867554 A CN106867554 A CN 106867554A CN 201510920928 A CN201510920928 A CN 201510920928A CN 106867554 A CN106867554 A CN 106867554A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B55/00—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material
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- Oil, Petroleum & Natural Gas (AREA)
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
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Abstract
The invention discloses a kind of method for producing needle-shape coke raw material using delay coking process treatment FCC recycle oils and conventional coking raw material.The method is to introduce the FCC recycle oils of low temperature in delayed coking drums middle and upper part, the conventional coking raw material introduced with bottom is in contact through the high-temperature oil gas that Pintsch process is produced, and reacted under the conditions of delayed coking, the oil gas of generation obtains needle-shape coke raw material into being separated in coking fractional distillation column.The present invention installs supersonic generator at coking fractional distillation column bottom, using the cavitation principle of ultrasonic wave, improves fractionating effect, so that improving wax oil distillates rate, obtains the needle-shape coke raw material of good quality and high output.
Description
Technical field
The invention belongs to a kind of process for producing needle-shape coke raw material.Specifically, it is to use delayed coking
Technique productions needle-shape coke raw material, while producing a kind of method of light fraction oil and coke.
Background technology
Needle coke is production high power, the primary raw material of ultra high power graphite electrode.Produce the most pass of needle coke
Key problem is the selection and pretreatment of raw material.According to the mechanism of coke form ation of needle coke, the raw material for producing needle coke is necessary
Meet that arene content is high, wherein three rings of linearly connected, Fourth Ring short-side chain arene content are in the majority, it is general to require virtue
Hydrocarbon content reaches 30%-50%；Resin and asphalt content is low, resin and asphalt inherently macromolecular
Condensed ring or again with the hydrocarbon compound of longer side chain, molecular structure is complicated, and carburizing reagent speed is fast, is consolidated quickly
, there is mosaic structure, so as to reduce the quality of needle coke, so former in needle coke in chemical conversion original state solid
The resin and asphalt content of material is more low more advantageously ensures that needle coke quality, general control heptane insolubles content
Less than 2.0%；Ash content includes that catalyst fines, free carbon metal equal size are low, and Gao Hui branches hinder interphase
Spherular growing up is melted simultaneously, and interphase is undeveloped in showing needle coke structure, typically requires primary quinoline non-soluble
Thing content is zero, and catalyst fines content is less than 100ppm, and content of beary metal is less than 100ppm；Sulfur content is low,
It is most of after sulphur carbonization to concentrate on coke, needle coke performance is influenceed, typically require that feed sulphur content is little
In 0.5%.
Catalytic cracking (FCC) recycle oil is mink cell focus catalytic cracking production, although wherein rich in substantial amounts of three ring,
Four PAHs, but also contain cracking activity light component higher and polymerization activity heavy constituent high and substantial amounts of catalysis
The impurity such as agent powder, heavy metal, these components and impurity destroy mesophase ball during needle coke is formed
The formation of body, makes needle coke Quality Down.If these composition pretreatments unfavorable to production needle coke fallen,
It is exactly good needle-shape coke raw material.At present, what is had will carry out delayed coking in FCC slurry incorporation decompression residuum,
Yield and property for improving needle-shape coke raw material, but FCC slurry addition can not be too many, otherwise can be obvious
Shorten the service cycle of delayed coking drums single column, and FCC slurry reacts at a higher temperature, and reaction
Time is long, the cut for suitably making needle-shape coke raw material is largely cracked, and reduces the yield of needle coke.
Pretreatment of raw material refers to the process of to remove in raw material to the generation unfavorable composition and impurity of needle coke.
CN1382761A discloses a kind of method of utilization preparing acicular coke by catalytic cracking of classified oil.The method is mainly
The catalyst fines in catalytic cracking clarified oil is removed using extraction, then pin is produced using delay coking process
Shape is burnt.USP4686048 is after diluting catalytic cracking clarified oil with the light oil less than 100 DEG C, through filtering, water
Wash, remove catalyst fines therein.USP5593572 is the addition hetero atom fat in catalytic cracking clarified oil
Fat adoption compound, carries out flocculating setting, removes catalyst fines.Above-mentioned patented method is mainly used for removing and urges
Agent powder, is not suitable for the pretreatment of catalytic cracked oil pulp raw material, and it is former to be required to special device treatment
Material, flow is numerous and diverse, with duration, also increases production cost.
CN1872963A discloses a kind of preprocessing method of raw materials for producing needle coke, and feedstock oil first steams through decompression
Removing wherein undesirable components are evaporated, remaining ideal composition is contacted with hydrogen, hydrogenation catalyst, hydrogenation reaction
Logistics is isolated to the raw material of production needle coke.Wherein feedstock oil can be catalytic cracked oil pulp or clarified oil.
The method can remove light, the weight undesirable components, maximum limit in feedstock oil by two kinds of combinations of technique
Degree ground retains ideal composition, and the feedstock oil after treatment meets the requirement of production needle-shape coke raw material.The method needs
Single vacuum distillation apparatus, and the cut that distillation is obtained needs further hydrotreating, hydrotreating generation oil
Further separation is also needed, hydrogenation high cost, investment in itself is big.
The content of the invention
In view of the shortcomings of the prior art, needle-like is produced using delay coking process the invention provides a kind of
The method of burnt raw material, the method can effectively remove unfavorable to production needle coke cracking activity in FCC recycle oils
The impurity such as light component and polymerization activity higher heavy constituent high and substantial amounts of catalyst fines, heavy metal, protects
The ideal composition of production needle coke is stayed, gained needle-shape coke raw material yield is high, and property is good.
The present invention installs supersonic generator at coking fractional distillation column bottom, using the cavitation principle of ultrasonic wave, improves
Fractionating effect, so that improving wax oil distillates rate, obtains the needle-shape coke raw material of good quality and high output.
The production method of needle-shape coke raw material of the present invention, be using delay coking process treatment FCC recycle oils and often
Rule coking raw material production needle-shape coke raw material, comprises the following steps：
(1) the high temperature routine coking raw material for being heated to 450 DEG C~550 DEG C prolongs from the entrance of delayed coking tower bottom
In slow coking tower；The low temperature FCC recycle oils for being heated to 360 DEG C~460 DEG C enter from delayed coking drums middle and upper part
Enter in delayed coking drums, contacted through the high-temperature oil gas that Pintsch process is produced with conventional coking raw material, in delay coke
Reacted under the conditions of change；
(2) the FCC recycle oils described in step (1) react life with conventional coking raw material in delayed coking drums
Into oil gas be discharged into being separated in coking fractional distillation column from tower top, obtain light fraction and needle-shape coke raw material
And tail oil.
(3) supersonic generator is installed at coking fractional distillation column bottom, using the cavitation principle of ultrasonic wave, improves and divide
Effect is evaporated, so that improving wax oil distillates rate, the needle-shape coke raw material of good quality and high output is obtained.
The initial boiling point of needle-shape coke raw material described in step (2) of the present invention is 340~380 DEG C, and the end point of distillation is
440~460 DEG C.Described light fraction refers to cut of its end point of distillation less than needle-shape coke raw material initial boiling point, described
Tail oil refer to its initial boiling point more than the needle-shape coke raw material end point of distillation cut, typically circulated with conventional coking raw material
Return delayed coking drums.
The operating condition of heretofore described delayed coking unit is as follows：Conventional coking raw material furnace outlet
450 DEG C~550 DEG C, best 485 DEG C~505 DEG C of temperature；Reaction pressure 0.05MPa~0.20MPa, it is best
0.15MPa~0.17MPa；Weight is circulated than 0.05~1.0, best 0.2~0.4；Coking cycle 24h~36h；
FCC recycle oil furnace outlets temperature is 360 DEG C~460 DEG C, best 400 DEG C~420 DEG C；FCC recycle oils
Furnace outlet temperature is lower than conventional coking raw material furnace outlet temperature 50 DEG C~and 100 DEG C.Described circulation weight
Amount ratio refers to the weight ratio of the tail oil with conventional coking raw material that loop back delayed coking drums.
In the inventive method, the conventional coking raw material described in step (1) is decompression residuum, the visbreaking of petroleum
One or more in cracked residue, ethylene bottom oil, thermal cracking residue and shale oil.
In the inventive method, stop entering FCC recycle oils in each coking cycle operation later stage, while improving
Conventional coking raw material furnace outlet temperature improves the temperature in coking tower, reduces the volatile matter of coke.One
As need improve 3 DEG C~5 DEG C.
In the inventive method, conventional coking raw material is using conventional delay coking process flow, i.e., first heated
Stove convection section is heated to 300~350 DEG C, subsequently into fractionation column base further with enter fractionating column high temperature
Coking oil gas exchange heat, while the coke powder carried in drip washing coking oil gas.Fractionator Bottom tail described in step (2)
Oil with routine coking raw material together go out fractionating column, into heating furnace radiant section be heated to 450 DEG C~550 DEG C after,
Reacted in from delayed coking tower bottom into tower.
In the inventive method, the heating of FCC recycle oils and conventional coking raw material can in same heating stove heat,
Can be heated in different heating furnaces respectively.After FCC recycle oils are heated to 360 DEG C~460 DEG C in heating furnace
Reacted in from delayed coking drums middle and upper part into tower, wherein the FCC recycle oils enter delayed coking drums
Distance of the position away from coking tower bottom account at the 5/10~6/10 of the whole height of coking tower.
In the present invention, FCC recycle oils are 10 with the feed weight ratio of conventional coking raw material:90~50:50, preferably
It is 20:80~40:60.
The inventive method is while delay coking process processes conventional coking raw material, to process FCC recycle oils,
FCC recycle oils be with low temperature from delayed coking drums middle and upper part into tower in carry out pyrogenetic reaction, with following excellent
Point：
(1) FCC recycle oils fall reactivity component cracking higher under the conditions of relatively mild, then
It is fractionated away in fractionating column, reaches the purpose of elimination reaction activity light component higher.
(2) FCC recycle oils are under the conditions of relatively mild, by ideals such as most of three ring, Fourth Ring, five rings
Needle-shape coke raw material component remain, the identical cut produced with conventional coking raw material is together as production pin
Burnt raw material.
(3) under conditions of delayed coking, asphalitine and part colloid are condensed coke to FCC recycle oils,
Together it is deposited in coking tower together with heavy metal, catalyst fines etc., is unfavorable for producing needle-like so as to remove
Burnt heavy constituent and impurity, divide without being removed during pyrogenetic reaction in later coking fractional distillation column
Stayed in after evaporating and further removed in bottom of towe tail oil.
(4) the method can process FCC recycle oils and obtain needle-shape coke raw material, expand needle-shape coke raw material
Source.
(5) the method flow is simple.While FCC recycle oils production needle-shape coke raw material is pre-processed, will
Some part components for being unfavorable for producing needle coke in FCC recycle oils obtain profit in delayed coking
With, generation light fraction oil and ordinary coke.
(6) FCC recycle oils are heated to 440 DEG C of highest and are put into delayed coking drums, and heating furnace is difficult coking,
Increase the service life.
(7) injection of lower temperature FCC recycle oils reduces the cracking temperature of conventional coking raw material, shortens
Pintsch process time of convenient source, secondary response generation is reduced, cause coking yield to reduce, extended
The single column stable operation cycle.
(8) supersonic generator is installed at coking fractional distillation column bottom, fractionating effect is improved, so as to improve wax oil evaporate
Extracting rate, obtains the needle-shape coke raw material of high yield and high quality.
(9) the inventive method operating flexibility is big, low cost, flexibly, be easy to grasp, can widely use.
(10) the inventive method can manufacture high-quality needle-shape coke raw material.
Brief description of the drawings
Fig. 1 is the schematic flow sheet of the inventive method.
In figure：1 raw materials furnace and heating, 2 oil transfer lines, 3,3a coking towers, 4 coking generation product
Derivation pipeline, 5 fractionating columns, 6 cracking gas exit pipelines, 7 naphtha outlet lines, 8 diesel oil
Fraction outlets pipeline, 9 needle-shape coke raw material outlet lines, 10 coking raw materials oil enters fractionation tower tube
Line, 11 coke go out device pipeline, the 12 coking raw material oil pipelines from Fractionator Bottom, 13 FCC
Recycle oil, enters the feeding line on coking tower top, 15 ultrasounds after the heating of 14 FCC recycle oils
Wave producer.
Specific embodiment
Embodiment 1：
It is further explained in detail below in conjunction with Fig. 1 and specific embodiment, but the present invention is not by embodiment
Limitation.
As shown in figure 1, a kind of method that utilization delay coking process produces needle-shape coke raw material, including following step
Suddenly：
(1), the conventional heated stove heat of coking raw material controls 485 DEG C of heater outlet temperature to 540 DEG C, from prolonging
Slow coking tower bottom enters in delayed coking drums；FCC recycle oils are by the coking raw material oil from Fractionator Bottom
Pipeline 12 enters heating furnace 1, after being heated to 420 DEG C, into the feeding line 14 on coking tower top, from prolonging
The middle and upper part of slow coking tower 3 enters in delayed coking drums 3；With conventional Jiao entered from delayed coking tower bottom
Change the high-temperature oil gas contact of raw material reaction generation, and the together reaction under the conditions of delayed coking；
(2), the FCC recycle oils described in step (1) react life with conventional coking raw material in delayed coking drums
Into oil gas the entrance of product derivation pipeline 4 is generated by coking from tower top discharge supersonic generator 15 is installed
Coking fractional distillation column 5 in separated, obtain light fraction and needle-shape coke raw material and tail oil.Obtain gas product
Product go out device by cracking gas exit pipeline 6；C5-180 DEG C of cut goes out dress by naphtha outlet line 7
Put；180 DEG C of -350 DEG C of cuts go out device by diesel oil distillate outlet line 8；350 DEG C -450 DEG C used as pin
Shape Jiao's raw material, device is gone out by needle-shape coke raw material outlet line 9.Conventional coking raw material enters from coking raw material oil
Enter the bottom that fractionating column pipeline 10 enters coking fractional distillation column 5, it is inverse with generation oil gas from delayed coking drums 3
Stream heat exchange, while the coke powder carried in drip washing oil gas, then with coking tail oil together by from Fractionator Bottom
Coking raw material oil pipeline 12 return to heating furnace 1 be heated to 450 DEG C~550 DEG C by oil transfer line 2 enter postpone
Coking tower 3 carries out pyrogenetic reaction, and the oil gas of generation generates product derivation pipeline 4 and enters fractionating column 5 by coking
Separated, coke goes out device pipeline 11 and goes out device by coke.After coking tower 3 is full of, switch coking tower 3a
Same operation is carried out, adustion 4 hours removes volatile matter.
The present invention installs supersonic generator at coking fractional distillation column bottom, fractionating effect is improved, so as to improve wax oil
Rate is distillated, the needle-shape coke raw material of high yield and high quality is obtained.
The initial boiling point of the needle-shape coke raw material is 340 DEG C, and the end point of distillation is 440 DEG C.
Described tail oil is cut of the initial boiling point more than the needle-shape coke raw material end point of distillation, is circulated with conventional coking raw material
Return delayed coking drums.
Described FCC recycle oil furnace outlet temperature is lower than conventional coking raw material furnace outlet temperature
65℃。
Described conventional coking raw material is decompression residuum, visbroken resids, ethylene bottom oil, the heat of petroleum
One or more in cracked residue and shale oil.
Stop entering FCC recycle oils in each coking cycle operation later stage, while improve conventional coking raw material adding
3 DEG C~5 DEG C of hot heater outlet temperature, improves the temperature in coking tower, reduces the volatile matter of coke.
First heated stove convection section is heated to 350 DEG C to conventional coking raw material described in step (1), subsequently into
Fractionation column base further exchanges heat with the high-temperature-coked oil gas for entering fractionating column, while being taken in drip washing coking oil gas
The coke powder of band, and together go out fractionating column with the Fractionator Bottom tail oil described in step (2), into the spoke of heating furnace
Penetrate after section is heated to 450 DEG C~550 DEG C, from delayed coking tower bottom into tower in reacted.
Described FCC recycle oils heating can be heated with conventional coking raw material in the different parts of same heating furnace,
Or the heating in different heating furnaces respectively.
Described FCC recycle oils are 20 with the feed weight ratio of conventional coking raw material:80.
Described FCC recycle oils refer to the catalytic cracking complete alternation oil more than 350 DEG C, wherein comprising recycle oil and
Slurry oil.
Embodiment 2：
The present embodiment is with the difference of embodiment 1：
(1), the conventional heated stove heat of coking raw material controls 500 DEG C of heater outlet temperature to 550 DEG C, from prolonging
Slow coking tower bottom enters in delayed coking drums；FCC recycle oils are by the coking raw material oil from Fractionator Bottom
Pipeline 12 enters heating furnace 1,400 DEG C is heated to, into the feeding line 14 on coking tower top, from delay
The middle and upper part of coking tower 3 enters in delayed coking drums 3；
The initial boiling point of the needle-shape coke raw material is 380 DEG C, and the end point of distillation is 460 DEG C.
Described FCC recycle oil furnace outlet temperature is lower than conventional coking raw material furnace outlet temperature
100℃。
Described FCC recycle oils are 25 with the feed weight ratio of conventional coking raw material:75.
Embodiment 3：
The present embodiment is with the difference of embodiment 1：
(1), the conventional heated stove heat of coking raw material controls 495 DEG C of heater outlet temperature to 545 DEG C, from prolonging
Slow coking tower bottom enters in delayed coking drums；FCC recycle oils are by the coking raw material oil from Fractionator Bottom
Pipeline 12 enters heating furnace 1, after being heated to 410 DEG C, by the feeding line 14 on coking tower top from delay
The middle and upper part of coking tower 3 enters in delayed coking drums 3；
The initial boiling point of the needle-shape coke raw material is 360 DEG C, and the end point of distillation is 450 DEG C.
Described FCC recycle oils are 50 with the feed weight ratio of conventional coking raw material:50.
Embodiment 4：
The present embodiment is with the difference of embodiment 1：
(1), the conventional heated stove heat of coking raw material controls 490 DEG C of heater outlet temperature to 535 DEG C, from prolonging
Slow coking tower bottom enters in delayed coking drums；FCC recycle oils are by the coking raw material oil from Fractionator Bottom
Pipeline 12 enters heating furnace 1,415 DEG C is heated to, into the feeding line 14 on coking tower top, from delay
The middle and upper part of coking tower 3 enters in delayed coking drums 3；
The initial boiling point of the needle-shape coke raw material is 360 DEG C, and the end point of distillation is 440 DEG C.
Described FCC recycle oil furnace outlet temperature is lower than conventional coking raw material furnace outlet temperature
75℃。
Described FCC recycle oils are 10 with the feed weight ratio of conventional coking raw material:90.
Embodiment 5：
The present embodiment is with the difference of embodiment 1：
(1), the conventional heated stove heat of coking raw material controls 505 DEG C of heater outlet temperature to 550 DEG C, from prolonging
Slow coking tower bottom enters in delayed coking drums；FCC recycle oils are by the coking raw material oil from Fractionator Bottom
Pipeline 12 enters heating furnace 1,405 DEG C is heated to, into the feeding line 14 on coking tower top, from delay
The middle and upper part of coking tower 3 enters in delayed coking drums 3；
The initial boiling point of the needle-shape coke raw material is 370 DEG C, and the end point of distillation is 460 DEG C.
Described FCC recycle oil furnace outlet temperature is lower than conventional coking raw material furnace outlet temperature
100℃。
Described FCC recycle oils are 40 with the feed weight ratio of conventional coking raw material:60.
The raw material oil nature that the embodiment 1-5 of table 1 is used
The technological condition of table 2 and product slates and major product property
The property of the embodiment 1-5 of table 3 gained needle-shape coke raw materials
Claims (10)
1. a kind of method that utilization delay coking process produces needle-shape coke raw material, comprises the following steps：
（1）450 DEG C~550 DEG C of high temperature routine coking raw material is heated to enter in delayed coking drums from delayed coking tower bottom；It is heated to 360 DEG C~460 DEG C of low temperature FCC recycle oils to enter in delayed coking drums from delayed coking drums middle and upper part, is contacted through the high-temperature oil gas that Pintsch process is produced with conventional coking raw material, is reacted under the conditions of delayed coking；
（2）Step（1）The oil gas that described FCC recycle oils react generation with conventional coking raw material in delayed coking drums is discharged into being separated in the coking fractional distillation column for be provided with supersonic generator from tower top, obtains light fraction and needle-shape coke raw material and tail oil.
2. the method that a kind of utilization delay coking process according to claim 1 produces needle-shape coke raw material, it is characterised in that the initial boiling point of the needle-shape coke raw material is 340 ~ 380 DEG C, the end point of distillation is 440 ~ 460 DEG C.
3. the method that a kind of utilization delay coking process according to claim 1 produces needle-shape coke raw material, it is characterized in that described tail oil is cut of the initial boiling point more than the needle-shape coke raw material end point of distillation, delayed coking drums are looped back with conventional coking raw material, circulation weight is than 0.05~1.0.
4. the method that a kind of utilization delay coking process according to claim any one of 1-3 produces needle-shape coke raw material, it is characterised in that the operating condition of described delayed coking is as follows：450 DEG C~550 DEG C of conventional coking raw material furnace outlet temperature；Reaction pressure 0.05
MPa~0.20MPa；Coking cycle 24h~36h；FCC recycle oil furnace outlets temperature is 360 DEG C~460 DEG C；FCC recycle oil furnace outlet temperature is lower than conventional coking raw material furnace outlet temperature 50~100 DEG C.
5. the method that a kind of utilization delay coking process according to claim 4 produces needle-shape coke raw material, it is characterised in that the operating condition of described delayed coking is as follows：485 DEG C~505 DEG C of conventional coking raw material furnace outlet temperature；Reaction pressure 0.15
MPa~0.17MPa；Circulation weight is than 0.2~0.4；Coking cycle 24h~36h；FCC recycle oil furnace outlets temperature is 400 DEG C~420 DEG C.
6. the method that a kind of utilization delay coking process according to claim 1 produces needle-shape coke raw material, it is characterised in that step（1）Described conventional coking raw material is one or more in decompression residuum, visbroken resids, ethylene bottom oil, thermal cracking residue and the shale oil of petroleum.
7. the method that a kind of utilization delay coking process according to claim 1 produces needle-shape coke raw material, it is characterised in that step（1）First heated stove convection section is heated to 300~350 DEG C to described conventional coking raw material, is further exchanged heat with the high-temperature-coked oil gas for entering fractionating column subsequently into fractionation column base, while the coke powder carried in drip washing coking oil gas, and and step（2）Described Fractionator Bottom tail oil together goes out fractionating column, into heating furnace radiant section be heated to 450 DEG C~550 DEG C after, from delayed coking tower bottom into tower in reacted.
8. the method that a kind of utilization delay coking process according to claim 1 produces needle-shape coke raw material, it is characterized in that described FCC recycle oils heating can be heated with conventional coking raw material in the different parts of same heating furnace, or the heating in different heating furnaces respectively.
9. the method that a kind of utilization delay coking process according to claim 1 produces needle-shape coke raw material, it is characterised in that step（1）Distance of the FCC recycle oils into the position of delayed coking drums away from coking tower bottom is accounted at the 5/10 ~ 6/10 of the whole height of coking tower.
10. the method that a kind of utilization delay coking process according to claim 1 produces needle-shape coke raw material, it is characterised in that described FCC recycle oils are 10 with the feed weight ratio of conventional coking raw material:90~50:50.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109233886A (en) * | 2018-10-26 | 2019-01-18 | 重庆润科新材料技术有限公司 | Coalite tar prepares the production method of coal-based needle coke in a kind of utilization |
| CN109777458A (en) * | 2017-11-14 | 2019-05-21 | 中国石油化工股份有限公司 | A kind of preparation method of high-quality needle coke |
| CN112048330A (en) * | 2020-09-01 | 2020-12-08 | 北京奥博斯工程技术有限公司 | Process and device for reducing coke powder of delayed coking fractionating tower |
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