CN104479707A - Method and device of preparing needle coke - Google Patents
Method and device of preparing needle coke Download PDFInfo
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- CN104479707A CN104479707A CN201410716440.7A CN201410716440A CN104479707A CN 104479707 A CN104479707 A CN 104479707A CN 201410716440 A CN201410716440 A CN 201410716440A CN 104479707 A CN104479707 A CN 104479707A
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- raw material
- needle coke
- molecular distillation
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- coke
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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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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
- C10C3/00—Working-up pitch, asphalt, bitumen
- C10C3/002—Working-up pitch, asphalt, bitumen by thermal means
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
- C10C3/00—Working-up pitch, asphalt, bitumen
- C10C3/06—Working-up pitch, asphalt, bitumen by distillation
Abstract
The invention discloses a method and a device of preparing a needle coke, and belongs to the technical field of needle coke preparation. The method disclosed by the invention is characterized by comprising the following steps: separating an asphalt raw material by virtue of a degasification column and a molecular distillation column, preheating the asphalt raw material, pumping the asphalt raw material in the degasification column and carrying out degasification treatment at a degasification temperature of 250-330 DEG C under an in-column pressure of 100-1000Pa, then pumping the degasified materials to the molecular distillation column, controlling a distillation temperature in the molecular distillation column to 300-400 DEG C and controlling a pressure to 0.01-100Pa, separating the materials into a light-phase component and a heavy-phase component in the molecular distillation column through a short-path distillation action, carrying out delayed coking on the light-phase component to obtain green coke, and calcining the green coke to obtain the needle coke. The method disclosed by the invention is capable of stably and accurately controlling the cutting amounts of the raw material components, thus flexibly adjusting the product quality, and furthest reserving ideal components. Moreover, the method is low in treatment temperature, rapid in material separation, and free from forming secondary quinoline undissolved substances.
Description
Technical field
Prepare method and the device thereof of needle coke, belong to needle coke preparing technical field.
Background technology
Needle coke is a kind of high quality carbon kind greatly developed in nineteen seventies carbon materials, is the main raw material producing superpower ultra-high power graphite electrode.Because needle coke has good graphitization characteristic, the superpower produced with it and ultra-high power graphite electrode have excellent electroconductibility, heat-shock resistance and antioxidant property.Electric furnace use by needle coke manufacture ultra-high power graphite electrode compare with ordinary electrode, can make shorten 30% ~ 50% tap to tap time, economize on electricity more than 10% ~ 20%, throughput can increase by 1.3 times, and economic benefit is very remarkable.
The preparation process of needle coke comprises raw materials pretreatment, delayed coking and calcining three process engineerings, and wherein raw materials pretreatment is the core cell that needle coke is produced, and is the primary factor affecting needle coke quality.First the object of raw materials pretreatment is remove the quinoline insolubles in raw material, is secondly the molecular weight distribution of adjustment raw material.
The method of raw materials pretreatment mainly contains: flash distillation-thermal polycondensation process, solvent-settling process, centrifuging, filtration method etc.
The technical process of flash distillation-thermal polycondensation process is: raw material → flash distillation → thermal polycondensation → delayed coking → (the high-temperature calcination) → finished products such as viscid bitumen.A kind of method preparing coal-based needle coke is disclosed in early stage Anshan Jiao Nai institute patent CN 86100675A, with coal tar, coal viscid bitumen for raw material, pure oil plant is obtained after processing, carry out coking process again, concrete grammar is: coal tar, coal viscid bitumen are carried out heat treated under certain temperature, pressure condition, produces cracking and polycondensation; In flashing tower, carry out flash distillation again, remove some objectionable impurities hindering mesophasespherule to grow up and insoluble impurity, obtain pure oil plant; Described pure oil plant is again carried out heat treated under certain temperature, pressure condition, produces polycondensation, obtain polycondensation asphalt; Oil in polycondensation asphalt and circulation is carried out coking process, obtains needle coke.Close with above-mentioned technique also have disclosed in the production technique of the coal-based needle coke improved disclosed in the coastal chemical patent CN1172147A in Anshan and patent CN1304974A, coal tar or coal-tar pitch flash distillation are obtained flash oil and coordinate polycondensation with petroleum component, then stand oil delayed coking and calcining are obtained needle coke.Patent application subsequently roughly have followed the flow process of above-mentioned technique, but adds the various improvement to above-mentioned technique.CN1268544 as special in species abundance in Baosteel in Shanghai is for system jams in conventional art, the problem of coking, a kind of preparation method of coal-based needle coke is proposed, the coal viscid bitumen adopting preparation is raw material, raw material is after purification and modulation, coal-based needle coke is made again through charing, it is characterized in that purification of raw materials is after heating raw materials, two sections of vacuum flashings that pressure is lower so that first paragraph is higher than second segment temperature, remove the active high component of impurity and thermal response and obtain free from foreign meter, not containing the fine fodder of the active high component of thermal response, then fine fodder is carbonized, charing after product is processed into coal-based needle coke product through aftertreatment.Other use solvent method is also had to carry out pretreated patent as CN 1268544A, CN1304974A, CN101126027, CN1944578A etc.Flash distillation-thermal polycondensation technique carries out suitability for industrialized production in Hongte Coal Chemical Co., Ltd., Shanxi at present, but the subject matter existed is that product thermal expansivity is high, asphalt yield is low, flash oil coking when pressurizeing polycondensation, causes polycondensation reactor and back segment line clogging.
Solvent-settling process is that high with the needle-shape coke raw material yield obtained after this technical finesse, needle coke good product quality, but complex process, invest also high with mixed solvent process coal-tar pitch removing QI.Japan is had to achieve the solvent-settling process suitability for industrialized production of coal-based needle coke abroad at present; The domestic 40,000 tons/year of industrialized units having Anshan heat energy institute can the needle coke produced compared with high-quality of continous-stable.The technical process of solvent-settling process is: viscid bitumen → solvent extraction → settlement separate → delayed coking → (high-temperature calcination) → finished product.
As Anshan heat energy institute patent CN1793287A discloses a kind of employing solvent treatment, manufacture the method being applicable to producing tar needle-shape coke.Be specially: by the straight run viscid bitumen of softening temperature 30 or softening temperature 35 return join viscid bitumen be heated to 60 after and aliphatic hydrocarbon/aromatic hydrocarbon solvents of being pre-mixed respectively by being pumped into stirring tank; After stirring, leave standstill, precipitating 2 ~ 20h, upper strata in stirring tank and light phase straight run viscid bitumen or return the mixture of joining pitch and solvent and extracted out by pump again and send into solvent recovery tower, produce refined asphaltic bitumen through solvent recovery tower recycling design, obtain the raw material being applicable to producing tar needle-shape coke.On this basis, Anshan heat energy institute patent CN 101531909 provides a kind of continuous sedimentation operation of producing for needle coke, this technique, under input and output material is all continuous print situation, is carried out settlement separate to quinoline insolubles, obtains unqualified containing quinoline insolubles light phase component.The mixture that the solvent used is aliphatic solvents and aromatic hydrocarbon solvent, blending ratio is (0.6 ~ 1.2): 1.By mixed solvent with coal tar soft asphalt with (0.6 ~ 1.2): the ratio of 1 mixes, the mixing oil pump of formation is squeezed into carry out in settlement separate equipment settlement separate, in sepn process, light-phase liquid can slowly rise, after its quinoline insolubles reaches requirement, then light liquid is constantly discharged from top, obtains refined asphaltic bitumen.
The method of quinoline insolubles removed by centrifuging whizzer, and pitch enters whizzer at suitable temperature and viscosity, whizzer separate except quinoline insolubles centrifugate and be rich in the residue of quinoline insolubles, centrifugate is as the raw material of needle coke.This technology substantially increases the yield of needle-shape coke raw material, but needle coke quality is general, and technology investment is large.
Filtration method is pitch and coordinates solvent to be adopt filter material to cross the method filtering quinoline insolubles in certain temperature and viscosity.Although the simple energy consumption of this method technique is low, require strict to filter material, processing condition are comparatively harsh, and filter material is expensive, needs often to change.
To sum up, at present flash distillation-thermal polycondensation process, solvent-settling process, centrifuging, filtration method etc. are mainly contained to the pretreatment process of needle-shape coke raw material.Flash distillation-thermal polycondensation process, the subject matter of existence is that product thermal expansivity is high, asphalt yield is low, flash oil coking when pressurizeing polycondensation, causes polycondensation reactor and back segment line clogging.Solvent-settling process main drawback needs huge solvent recovering system, and pitch index is wayward.Centrifuging can improve the yield of needle coke, but needle coke quality is general, and technology investment is larger.Filtration method is pitch and coordinates solvent to be adopt filter material to cross the method filtering quinoline insolubles in certain temperature and viscosity, although the simple energy consumption of this method technique is low, require strict to filter material, processing condition are comparatively harsh, and filter material is expensive, needs often to change.
Summary of the invention
The technical problem to be solved in the present invention is: overcome the deficiencies in the prior art, and provide a kind of preparation method and device thereof of needle coke, process energy consumption is low, and treatment temp is low, and feed separation is rapid, can not form secondary quinoline insolubles.
The technical solution adopted for the present invention to solve the technical problems is: the preparation method of this needle coke, it is characterized in that, implementation step is: asphalt stock preheating melted and pump into stripper column and carry out degassed process removing small molecule component, degassing temperature is 250 ~ 330 DEG C, post internal pressure is 100 ~ 1000Pa, again by the material pumping of degassed removing small molecule component to molecular distillation post, in molecular distillation post, distillation temperature controls at 300 ~ 400 DEG C, pressure is 0.01 ~ 100Pa, in molecular distillation post, by short-path distillation effect, material is divided into weight two phase component, light phase component more delayed coking obtains green coke, needle coke is obtained after green coke calcining.
Described raw material preheating is that raw material is carried out preheating in raw material preheating still under the effect of stirring, and preheating temperature is 150 ~ 250 DEG C, and mixing speed is 20 ~ 100 revs/min.The object of raw material preheating be convenient to raw material smooth pumping and provide certain heat for stripper column.
The object of material degassing process be in order to avoid material in molecular distillation post because there is bumping containing more small molecules and remove in advance.
The coking temperature of described delayed coking is 430 ~ 500 DEG C, coking pressure 0.2 ~ 0.8MPa.
Described calcining is that the green coke obtained after delayed coking is obtained needle coke through 900 ~ 1300 DEG C of high-temperature calcination process.
Described asphalt stock is one or more mixtures in medium temperature coal pitch, low temperature coal-tar pitch, petroleum pitch, modified pitch, viscid bitumen, liquefied residue pitch.The present invention with the pitch of more difficult distillation for raw material, according to Conventional espresso means, because the component of heavy phase in pitch is too many, cannot normal distillation as coal tar, boiling point large in viscosity is high.And the present invention adopts molecular distillation technique, utilize specific vacuum tightness and distillation temperature two to make pitch realize quick weight be separated and intercept the applicable component doing needle coke wherein, make originally because viscosity is large and the too high easy generation side reaction of temperature and the asphalt stock that is difficult to reach disengaging become the raw material of needle coke.Even segregation rate exceedes the distillation means of traditional coal tar.Again because containing more small molecule component in asphalt stock, the words of molecular distillation technique are directly utilized to be easy to bumping under vacuum.The present invention utilizes the degassing tower of low vacuum successfully to remove small molecules, retains in asphalt stock to greatest extent again and is applicable to the component doing needle coke, ensure that productive rate.The present invention, by the different temperature and pressure separate bitumen raw material of front latter two, makes the needle coke coking raw material molecular weight distribution of intercepting more concentrated and is conducive to mesophase spherule and melts mutually and transform while guarantee productive rate.
Adopt molecular distillation technique to cut raw material, according to different feedstock properties, extract by the adjustment of temperature and pressure the asphalt component meeting needle coke and require.
The device that the preparation method of above-mentioned needle coke is used, is characterized in that: comprise raw material preheating still, stripper column, raw material receiving tank, molecular distillation post, gently to connect closed cans and heavy phase receiving tank, each assembly is equipped with inner heating device; Raw material preheating still is the kettle with whipping appts, bottom connects stripper column top with pipeline, stripper column bottom conduit connects raw material receiving tank opening for feed, and raw material receiving tank discharge port connects molecular distillation post with pipeline, and molecular distillation post two discharge port connects gently connect closed cans and heavy phase receiving tank respectively; The vacuum pump set that stripper column and molecular distillation post are all connected with condenser controls post internal pressure.
Raw material melt after pumping enter molecular distillation system, by molecular distillation system be divided into light, weigh two kinds of components; Light phase component, as the raw material of needle coke, obtains needle coke through delayed coking and calcining; Heavy phase component is high softening-point, high carbon residue pitch can use as binding agent.
Compared with prior art, the beneficial effect that the preparation method of a kind of needle coke of the present invention has is: compared with the prior art, preprocessing method of raw materials of the present invention has following major advantage: the present invention can adopt medium temperature coal pitch, low temperature coal-tar pitch, petroleum pitch, modified pitch, viscid bitumen, liquefied residue pitch etc. to be raw material, utilize molecular distillation system intercept for light, weigh two kinds of components, under suitable treatment temp and pressure, light constituent is not containing the easy polymers of macromole and quinoline insolubles, molecular weight distribution is concentrated, and is conducive to mesophase spherule and melts and transform; Light constituent is carried out delayed coking process and calcining, obtained needle coke.The method can the amount of cutting of stable and accurate control feed composition, thus flexible quality product, ideal composition can be retained to greatest extent; Device is simple, and industrial easy handling controls, and does not have huge solvent recuperation treatment system, concise in technology, and process raw material is extensive, and energy consumption is low, good operational environment.Obtained needle coke thermal expansivity is low, for preparing the desirable feedstock of ultra-high power graphite electrode.Treatment temp of the present invention is low, and velocity of separation is fast, and do not have polycondensation to occur, pitch can not form secondary quinoline insolubles and affect quality product, and productive rate is high.
Accompanying drawing explanation
Fig. 1 is the raw material pretreatment process schema of needle coke.
Wherein: 1, raw material preheating still 2, stripper column 3, raw material receiving tank 4, molecular distillation post 5, heavy phase receiving tank 6, gently to connect closed cans 7, condenser 8, vacuum pump set.
Embodiment
1 be also described further the preparation method of a kind of needle coke of the present invention with reference to the accompanying drawings, wherein embodiment 1 is most preferred embodiment of the present invention in conjunction with the embodiments.
With reference to accompanying drawing 1: the device that the preparation method of needle coke of the present invention is used, comprise raw material preheating still 1, stripper column 2, raw material receiving tank 3, molecular distillation post 4, gently to connect closed cans 6 and heavy phase receiving tank 5, raw material preheating still 1 is the kettle with heating and whipping appts, bottom connects stripper column 2 top with pipeline, stripper column 2 bottom conduit connects raw material receiving tank 3 opening for feed, raw material receiving tank 3 discharge port connects molecular distillation post 4 with pipeline, and molecular distillation post 4 liang of discharge ports connect gently connect closed cans 6 and heavy phase receiving tank 5 respectively; Stripper column 2 and molecular distillation post 4 are all connected with condenser 7 and vacuum pump set 8 controls post internal pressure.Raw material preheating still 1, stripper column 2, raw material receiving tank 3, molecular distillation post 4, gently connect closed cans 6 and heavy phase receiving tank 5 are equipped with inner heating device.In accompanying drawing 1, the direction of arrow is material direct of travel or heating medium traffic direction.
Embodiment 1
By softening temperature 75 DEG C, the medium temperature coal pitch of quinoline insolubles 4.8%, be preheated to 200 DEG C under mixing speed is 70 revs/min in raw material preheating still 1 after, pumping enters stripper column 2, degassing temperature 280 DEG C, degassed process under pressure 300Pa, be pumped to molecular distillation post 4 after the incoming stock receiving tank 3 of material after degassed cushions insulation and carry out molecular distillation process, distillation temperature 390 DEG C, pressure 0.01Pa.Material through molecular distillation is divided into 85% mutually light and 15% heavy phase, and light phase component is that refined asphaltic bitumen enters the raw material of closed cans 6 as needle coke that gently connect; Heavy phase component enters heavy phase receiving tank 5 and uses as binder pitch as high softening-point height carbon residue pitch.The refined asphaltic bitumen obtained enters delayed coking unit coking temperature 450 DEG C, and pressure 0.5MPa carries out delayed coking and obtains green coke, and green coke is calcined and obtained needle coke at 1200 DEG C, and its thermal expansivity CTE is 0.9 × 10
-6/ DEG C.
Embodiment 2
By softening temperature 75 DEG C, the medium temperature coal pitch of quinoline insolubles 4.8%, be preheated to 200 DEG C under mixing speed is 80 revs/min in raw material preheating still 1 after, pumping enters stripper column 2, degassing temperature 270 DEG C, degassed process under pressure 600Pa, be pumped to molecular distillation post 4 after the incoming stock receiving tank 3 of material after degassed cushions insulation and carry out molecular distillation process, distillation temperature 390 DEG C, pressure 1Pa.Material through molecular distillation is divided into 50% mutually light and 50% heavy phase, and light phase component is that refined asphaltic bitumen enters the raw material of closed cans 6 as needle coke that gently connect; Heavy phase component enters heavy phase receiving tank 5 and uses as binder pitch as high softening-point height carbon residue pitch.The refined asphaltic bitumen obtained enters delayed coking unit coking temperature 480 DEG C, and pressure 0.7MPa carries out delayed coking and obtains green coke, and green coke is calcined and obtained needle coke at 1200 DEG C, and its thermal expansivity CTE is 1.15 × 10
-6/ DEG C.
Embodiment 3
By softening temperature 75 DEG C, the medium temperature coal pitch of quinoline insolubles 4.8%, be preheated to 180 DEG C under mixing speed is 100 revs/min in raw material preheating still 1 after, pumping enters stripper column 2, degassing temperature 260 DEG C, degassed process under pressure 600Pa, be pumped to molecular distillation post 4 after the incoming stock receiving tank 3 of material after degassed cushions insulation and carry out molecular distillation process, distillation temperature 350 DEG C, pressure 100Pa.Material through molecular distillation is divided into 30% mutually light and 70% heavy phase, and light phase component is that refined asphaltic bitumen enters the raw material of closed cans 6 as needle coke that gently connect; Heavy phase component enters heavy phase receiving tank 5 and uses as binder pitch as high softening-point height carbon residue pitch.The refined asphaltic bitumen obtained enters delayed coking unit coking temperature 450 DEG C, and pressure 0.6MPa carries out delayed coking and obtains green coke, and green coke is calcined and obtained needle coke at 900 DEG C, and its thermal expansivity CTE is 0.95 × 10
-6/ DEG C.
Embodiment 4
By softening temperature 30 DEG C, the viscid bitumen of quinoline insolubles 1.8%, be preheated to 150 DEG C under mixing speed is 20 revs/min in raw material preheating still 1 after, pumping enters stripper column 2, degassing temperature 250 DEG C, degassed process under pressure 100Pa, be pumped to molecular distillation post 4 after the incoming stock receiving tank 3 of material after degassed cushions insulation and carry out molecular distillation process, distillation temperature 300 DEG C, pressure 5Pa.Material through molecular distillation is divided into 45% mutually light and 55% heavy phase, and light phase component is that refined asphaltic bitumen enters the raw material of closed cans 6 as needle coke that gently connect; Heavy phase component enters heavy phase receiving tank 5 and uses as binder pitch as high softening-point height carbon residue pitch.The refined asphaltic bitumen obtained enters delayed coking unit coking temperature 430 DEG C, and pressure 0.8MPa carries out delayed coking and obtains green coke, and green coke is calcined and obtained needle coke at 1000 DEG C, and its thermal expansivity CTE is 1.1 × 10
-6/ DEG C.
Embodiment 5
By softening temperature 110 DEG C, the coal tar pitch of quinoline insolubles 12%, be preheated to 250 DEG C under mixing speed is 60 revs/min in raw material preheating still 1 after, pumping enters stripper column 2, degassing temperature 330 DEG C, degassed process under pressure 1000Pa, be pumped to molecular distillation post 4 after the incoming stock receiving tank 3 of material after degassed cushions insulation and carry out molecular distillation process, distillation temperature 400 DEG C, pressure 1Pa.Material through molecular distillation is divided into 40% mutually light and 60% heavy phase, and light phase component is that refined asphaltic bitumen enters the raw material of closed cans 6 as needle coke that gently connect; Heavy phase component enters heavy phase receiving tank 5 and uses as binder pitch as high softening-point height carbon residue pitch.The refined asphaltic bitumen obtained enters delayed coking unit coking temperature 500 DEG C, and pressure 0.2MPa carries out delayed coking and obtains green coke, and green coke is calcined and obtained needle coke at 1300 DEG C, and its thermal expansivity CTE is 1.2 × 10
-6/ DEG C.
The above is only preferred embodiment of the present invention, and be not restriction the present invention being made to other form, any those skilled in the art may utilize the technology contents of above-mentioned announcement to be changed or be modified as the Equivalent embodiments of equivalent variations.But everyly do not depart from technical solution of the present invention content, any simple modification, equivalent variations and the remodeling done above embodiment according to technical spirit of the present invention, still belong to the protection domain of technical solution of the present invention.
Claims (6)
1. the preparation method of a needle coke, it is characterized in that, implementation step is: asphalt stock preheating melted and pump into stripper column and carry out degassed process removing small molecule component, degassing temperature is 250 ~ 330 DEG C, post internal pressure is 100 ~ 1000Pa, again by the material pumping of degassed removing small molecule component to molecular distillation post, in molecular distillation post, distillation temperature controls at 300 ~ 400 DEG C, pressure is 0.01 ~ 100Pa, in molecular distillation post, by short-path distillation effect, material is divided into weight two phase component, light phase component more delayed coking obtains green coke, needle coke is obtained after green coke calcining.
2. the preparation method of a kind of needle coke according to claim 1, is characterized in that: described raw material preheating is that raw material is carried out preheating in raw material preheating still under the effect of stirring, and preheating temperature is 150 ~ 250 DEG C, and mixing speed is 20 ~ 100 revs/min.
3. the preparation method of a kind of needle coke according to claim 1, is characterized in that: the coking temperature of described delayed coking is 430 ~ 500 DEG C, coking pressure 0.2 ~ 0.8MPa.
4. the preparation method of a kind of needle coke according to claim 1, is characterized in that: described calcining is that the green coke obtained after delayed coking is obtained needle coke through 900 ~ 1300 DEG C of high-temperature calcination process.
5. the preparation method of a kind of needle coke according to claim 1, is characterized in that: described asphalt stock is one or more mixtures in medium temperature coal pitch, low temperature coal-tar pitch, petroleum pitch, modified pitch, viscid bitumen, liquefied residue pitch.
6. the device that the preparation method of the needle coke described in a claim 1 ~ 5 is used, it is characterized in that: comprise raw material preheating still (1), stripper column (2), raw material receiving tank (3), molecular distillation post (4), gently to connect closed cans (6) and heavy phase receiving tank (5), each assembly is equipped with inner heating device; Raw material preheating still (1) is the kettle with whipping appts, bottom connects stripper column (2) top with pipeline, stripper column (2) bottom conduit connects raw material receiving tank (3) opening for feed, raw material receiving tank (3) discharge port connects molecular distillation post (4) with pipeline, and molecular distillation post (4) two discharge port connects gently connect closed cans (6) and heavy phase receiving tank (5) respectively; The vacuum pump set (8) that stripper column (2) and molecular distillation post (4) are all connected with condenser (7) controls post internal pressure.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105883750A (en) * | 2016-04-14 | 2016-08-24 | 神华集团有限责任公司 | Mesoporous carbon and preparation method thereof |
| CN105905883A (en) * | 2016-04-15 | 2016-08-31 | 神华集团有限责任公司 | Mesocarbon microbead and preparation method thereof |
| CN108975302A (en) * | 2018-07-05 | 2018-12-11 | 中冶焦耐(大连)工程技术有限公司 | A kind of preparation method and application of the low graphitized carbon material of asphaltic base |
| CN109022008A (en) * | 2018-08-27 | 2018-12-18 | 中国石油大学(华东) | A kind of preparation method of high yield acicular petroleum coke |
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| US4547284A (en) * | 1982-02-16 | 1985-10-15 | Lummus Crest, Inc. | Coke production |
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| US4547284A (en) * | 1982-02-16 | 1985-10-15 | Lummus Crest, Inc. | Coke production |
| US4519898A (en) * | 1983-05-20 | 1985-05-28 | Exxon Research & Engineering Co. | Low severity delayed coking |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105883750A (en) * | 2016-04-14 | 2016-08-24 | 神华集团有限责任公司 | Mesoporous carbon and preparation method thereof |
| CN105905883A (en) * | 2016-04-15 | 2016-08-31 | 神华集团有限责任公司 | Mesocarbon microbead and preparation method thereof |
| CN108975302A (en) * | 2018-07-05 | 2018-12-11 | 中冶焦耐(大连)工程技术有限公司 | A kind of preparation method and application of the low graphitized carbon material of asphaltic base |
| CN109022008A (en) * | 2018-08-27 | 2018-12-18 | 中国石油大学(华东) | A kind of preparation method of high yield acicular petroleum coke |
| CN109022008B (en) * | 2018-08-27 | 2021-03-19 | 中国石油大学(华东) | Preparation method of high-yield needle-shaped petroleum coke |
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| CN104479707B (en) | 2017-03-08 |
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