US3617515A - Production of needle coke from coal for pitch - Google Patents

Production of needle coke from coal for pitch Download PDF

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US3617515A
US3617515A US827603A US3617515DA US3617515A US 3617515 A US3617515 A US 3617515A US 827603 A US827603 A US 827603A US 3617515D A US3617515D A US 3617515DA US 3617515 A US3617515 A US 3617515A
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fraction
temperature
coke
coking
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Ward J Bloomer
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Lummus Technology LLC
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Lummus Co
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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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  • This invention relates to the production of graphitizable needle coke and more particularly to a process for the simultaneous production of such needle coke and carbon electrode grade coke.
  • Needle coke after calcination and graphitization, is characterized by a low longitudinal coefl'icient of thermal expansion which is matched by a low electric resistivity and it is primarily used in producing high-quality synthetic graphite electrodes for electrosteel furnaces and for other electrothermal and chlor-alkali industries. Needle coke is a premium grade coke which is generally priced at $50$ 100 per ton.
  • Carbon electrode grade coke is generally priced at $-$40 per ton and consequently the production of needle coke from such a feed is more desirable.
  • an object of this invention is to provide a new and improved process for producing graphitizable needle coke.
  • Another object of this invention is to provide a process for the simultaneous production of such needle coke and carbon electrode grade coke.
  • a further object of this invention is to provide a process for producing such needle coke by a delayed coking technique.
  • Still another object of this invention is to provide a process for producing such needle coke from a feed having a high content of condensed ring aromatic compounds.
  • FIG. 1 is a simplified schematic flow diagram of an embodiment of the invention.
  • FIG. 2 is a simplified schematic flow diagram of another embodiment of the invention.
  • the objects of this invention are broadly accomplished by subjecting to coking conditions of temperature and pressure a fraction derived from a nonpetroleum source having a high content of condensed ring aromatic compounds and at least 80 percent of which boils within the range from about 600 F. to about l,200 F., preferably from about 600 F to about l,000 F., to produce graphitizable needle coke.
  • the fraction boiling within the range from about 600 F. to about l,200 F. is derived from a feedstock which includes components boiling above l,200 F. and the residue, after separation of the fraction used as a source of such needle coke, is employed for the production of .a carbon electrode grade coke.
  • the feeds generally treated in accordance with the invention are derived from coal and contain a fraction having a high content; i.e., generally greater than about 70 percent, of condensed ring (polynuclear) aromatic compounds, both heterocyclic and isocyclic.
  • the feed is preferably treated to recover a fraction having upper and lower cut points falling within the range from about 600 F. to about l ,200 F. and this fraction is coked to a high-grade needle coke, with the higher boiling residue; i.e., the fraction boiling above the upper cut point of the needle coke fraction, preferably being coked to carbon electrode grade coke.
  • the fraction employed for the production of needle coke may have components boiling throughout the 600 F. to L200" F.
  • range or components boiling through only a portion of the range i.e., 700900 F. It is further to be understood that components boiling below about 600 F. are only excluded for the reason that such components are not coke precursors and therefore would not he "coked” during the operation. Consequently, if desired, components boiling below about 600 F. may be ineluded lit! a diluent, but in general such components are excluded in that they would diminish the overall capacity of the equipment.
  • a preferred feed is a coal tar pitch obtained by either the high-temperature or low-temperature carbonization of coal, as generally known in the art, the former feed particularly being generally characterized as completely comprised of condensed ring aromatic compounds (an estimated 5,000 of such compounds), with two-thirds of the aromatic compounds being isocyclic and the remaining third heterocyclic.
  • the feed to be converted to needle coke may also contain components which boil above about l,200 F., but higher boiling components should not comprise more than about 20 percent of the feed to be coked to needle coke, preferably no greater than about 15 percent of the feed.
  • the coking of a feed containing components boiling above about l,200 F. produces a grade of needle coke which is lower than the grade of needle coke produced from a feed free of such components, but this lower grade of needle coke has a coefficient of thermal expansion sufficiently low to meet various commercial specifications for a needle coke.
  • a feed such as soft coal tar pitch derived from the higher temperature carbonization of coal
  • in line 10 is passed through a heater 11 to effect heating thereof to the operating temperature of a vacuum flash tower, as hereinafter described.
  • the heated feed from heater ll in line 12 is introduced into a vacuum flash tower 13, operating at a temperature and pressure designed to recover from the feed an overhead fraction containing components having boiling points up to about l,000 F.; the tower 13 generally being operated at a temperature from about 700 F. to about 850 F. and a pressure from about 0.25 p.s.i.a. to about 2.0 p.s.i.a.
  • An overhead is withdrawn from flash tower 13 through line 14, compressed to atmospheric pressure in a suitable compression device 15, preferably a multistage vacuum ejector and passed through cooler 16 wherein the vapor is cooled to a temperature at which the vapor is condensed, generally a temperature from about 300 F. to about 500 F.
  • the cooled liquid from cooler 16 in lines 17A and B is introduced above and below, respectively, the vapor-liquid contact decks of a combination fractionator l8 operated under temperature and pressure conditions to produce a heavy oil bottoms having a lower cut point of about 600 F. and an upper cut point between about 900 F.; and about 1,000 F.; a light oil, generally having cut points between about 400 F.
  • the fractionator 18 is also provided with coke drum overhead vapors through lines 19 and 20 and heavy oil recycle through lines 53 and 54, as hereinafter described.
  • the fractionator 18 is generally operated at an overhead temperature between about 300 F. and about 400 F., a bottoms temperature of between about 650 F. and about 850 F. a pressure between about 25 p.s.i.g. and about p.s.i.g. and a volumetric recycle ratio of from about 0.3:1 to about 20:], preferably from about 0.5:l to about 2.0:l, based upon equivalent feed to fractionator 18, with higher recycle ratios generally decreasing the overall capacity of the equipment.
  • a portion of the liquid from cooler 16 may be passed through branch line 17C to storage and/or further treatment; e.g., to produce carbon black.
  • a heavy oil bottoms having the hereinabove noted cut points is withdrawn from fractionator 18 through line 21 and a portion thereof is passed through line 22 to a coking heater 23 operated at an outlet temperature of between about 900 F.- and about l,000 F. and in a manner to prevent premature coking therein; i.e., the feed is maintained in turbulent motion or at a high velocity by providing temperature and pressure profiles in the heater that will produce partial vaporization of the feed, thereby preventing the coking problems caused by slow moving feed in the liquid state.
  • controlled amounts of steam may by introduced into the coking heater 23 at appropriate places to obtain the required turbulence or high velocity.
  • the heated heavy oil is withdrawn from the coking heater 23 through line 24 and introduced into coke drums 25, of a type known in the art, wherein the heavy oil is converted to needle coke and lighter components.
  • the coking drums are operated at a pressure of between about p.s.i.g. and about 90 p.s.i.g., preferably between about 25 and about 90 p.s.i.g. and an overhead temperature of between about 840 F. and about 900 F., preferably between about 860 F. and about 900 F.
  • the needle coke is withdrawn from the drums 25 through line 26.
  • An overhead is withdrawn from the coke drums 25 through line 19 and introduced into the fractionator 18 at a point below the introduction of the flashed overhead in line 17A.
  • the cooled flashed overhead in line 17A aids in condensing heavy oil from the coke drum overhead vapor.
  • the light oil and/or heavy oil is mixed with thebottoms in an amount to provide a volumetric ratio of between about 0.2 and about 0.5 of light and/or heavy oil to bottoms.
  • the remainder of the light oil is passed through line 33A to storage and/or further treatment.
  • the mixture is introduced into a coking heater 35, of a type known in the art.
  • the coking heater is operated so as to produce an outlet temperature of between about 900 F. and about 960 F.
  • the coking heater 35 is operated as generally known in the art to prevent premature coking therein, i.e., the feed is maintained in turbulent motion or at a high velocity by providing temperature and pressure profiles in the heater that will produce partial vaporization of the feed, thereby preventing the coking problems caused by slow moving feed in the liquid state.
  • controlled amounts of steam may be introduced into the coking heater 35 at appropriate places to obtain the required turbulence or high velocity.
  • the heated mixture is withdrawn from the coking heater 35 through line 36 and introduced into coke drums 37, of a type known in the art, wherein the mixture is converted to carbon electrode grade coke and lighter components.
  • the coking drums are operated at a pressure of between about 15 p.s.i.g. and about 90 p.s.i.g., preferably between about 25 and about 90 p.s.i.g. and an overhead temperature of between about 840 F. and about 900 F. preferably between about 860 F. and about 900 F.
  • the coke is withdrawn from the drums 37 through line 38.
  • An overhead is withdrawn from the coke drums 37 through line and introduced into the fractionator 18 at a point below the introduction of the flashed overhead in line 17A.
  • the cooled flashed overhead in line 17A aids in condensing heavy oil from the coke drum overhead vapor.
  • a portion of the heavy oil withdrawn from fractionator 18 through-line 21 is passed through line 50, cooled in heat exchanger 51 by indirect heat transfer with a suitable coolant; e.g., the feed to the flash tower 13 in line 10, and further cooled by indirect heat transfer with a suitable coolant; e.g., boiler feed water, in heat exchanger 52 to a temperature suitable for inducing additional recycle in fractionator 18 to meet the hereinabove noted volumetric recycle requirements, generally a temperature from about 400 F.
  • a portion of the cooled heavy oil from heat exchanger 52 is introduced into the fractionator 18 through line 53 to aid in providing the recycle requirements.
  • the total recycle is comprised of: the heavy oil fraction returned through line 53 and the condensed portion of the coke drum overhead vapors introduced through lines 19 and 20, with the condensation of materials from the coke drum overhead vapors being induced by direct contact in fractionator 18 between the coke drum overhead vapors and both the cooled liquid introduced through line 17A and the cooled heavy oil recycle introduced through line 53.
  • the remaining heavy oil from heat exchanger 52 is introduced into the fractionator 18 through line 54 to maintain desired operating conditions and passed through line 55 to storage and/or further treatment; e.g., the production of carbon black.
  • FIG. 2 A further embodiment of the invention is illustrated in FIG. 2.
  • a liquid feed such as, soft coal tar pitch derived from the highor low-temperature carbonization of coal
  • a coker combination fractionator 101 operated under temperature and pressure conditions to produce a heavy oil having a lower cut point of about 600 F and an upper cut point between about 700 F. and about 1,000 F.; light oil, generally having cut points between about 400 F. and about 600 F.; and an overhead vapor comprised ofgas and distillate, generally boiling up to about 400 F.
  • the fractionator 101 is generally operated at an overhead temperature of between about 300 F. and about 400 F., a pressure between about 25 p.s.i.g.
  • the liquid feed introduced into the fractionator 10! through line 100 is contacted with hot coke drum overhead vapors introduced through lines 102 and 103, obtained as hereinafter described, resulting in flashing of materials having boiling points up to about 900 F. to about l,000 F. from the liquid feed.
  • the unflashed portion of the liquid feed is withdrawn from the fractionator 101 through line 104 and if the heat input to the fractionator 101 is not sufficient to flash essentially all of the material boiling up to about 900 F. to about l,000 F.
  • the portion of the liquid in line 104 is introduced into a flash tower 105 through line 106, operating at a temperature and pressure to provide an overhead containing components boiling up to about l,000 F.; generally an operating temperature of between about 600 F. and about 800 F. and an operating pressure between about 0.25 p.s.i.a. and about 2.0 p.s.i.a.
  • An overhead is withdrawn from flash tower 105 through line 107 compressed to atmospheric pressure in a suitable compression device 108, preferably a multistage vacuum ejector, and passed through cooler 109 wherein vapor is cooled to a temperature at which the vapor is condensed, generally a temperature from about 200 F. to about 400 F.
  • the cooled liquid from cooler 109 in line 110 is mixed with heavy oil in line 112 withdrawn from the combination-fractionator 101, as hereinafter described and the mixture introduced into a coking heater 113, of a type known in the art.
  • the coking heater 113 is operated at an outlet temperature of between about 900 F. and about l,000 F. and in a manner to prevent premature coking therein; i.e., the feed is maintained in turbulent motion or at a high velocity by providing temperature and pressure profiles in the heater that will produce partial vaporization of the feed, thereby preventing the coking problems caused by slow moving feed in the liquid state.
  • controlled amounts of steam may be introduced into the coking heater 113 at appropriate places to obtain the required turbulence or high velocity.
  • the heated heavy oil is withdrawn from the coking heater 113 through line 114 and introduced into coke drums 115, of a type known in the art, wherein the heavy oil is converted to graphitizable needle coke and lighter components.
  • the coking drums are operated at a pressure of between about 15 p.s.i.g. and about 90 p.s.i.g., preferably between about 25 and about 90 p.s.i.g. and an overhead temperature of between about 840 F. and about 900 F., preferabiy between about 860 F. and about 900 F.
  • the needle coke is withdrawn from the drums 115 through line 1 16.
  • An overhead is withdrawn from the coke drums 115 through line 103 and introduced into the fractionator 101 below the point of introduction of the feed in line 100 to recover various components from the overhead; the overhead also providing a portion of the heat requirements for flashing of the feed.
  • the light oil and/or heavy oil is mixed with the bottoms in an amount to provide a volumetric ratio of between about 0.2 and about 1.0 of light and/or heavy oil to bottoms.
  • the remainder of the light oil is passed through line 123A to storage and/or further treatment.
  • the mixture in line 124 is introduced into a coking heater 125, of a type known in the art.
  • the coking heater is operated so as to produce an outlet temperature of between about 900 F. and about 960 F.
  • the coking heater 125 is operated as generally known in the art to prevent premature coking therein; i.e., the feed is maintained in turbulent motion or at a high velocity by providing temperature and pressure profiles in the heater that will produce partial vaporization of the feed, thereby preventing the coking problems caused by slow moving feed in the liquid state.
  • controlled amounts of steam may be introduced into the coking heater 125 at ap-' limbate places to obtain the required turbulence or high velocity.
  • the heated mixture is withdrawn from the coking heater 125 through line 126 and introduced into coke drums 127, of a type known in the art, wherein the mixture is converted to carbon electrode grade coke and lighter components.
  • the coking drums are operated at a pressure of between about p.s.i.g. and about 90 p.s.i.g., preferably between about 25 and about 90 p.s.i.g. and an overhead temperature of between about 840 F. and about 900 F., preferably between about 860 F. and about 900 F.
  • the coke is withdrawn from the drums 127 through line 128.
  • An overhead is withdrawn from the coke drums 128 through line 102 and introduced into the fractionator 101 below the point of introduction of the feed in line 100 to recover various components from the overhead; the overhead also providing a portion of the heat requirements for flashing of the feed.
  • a heavy oil fraction having the hereinabove noted cut points, is withdrawn from fractionator 101 through line 150, cooled in heat exchanger 151 by indirect heat transfer with a suitable coolant; e.g., the feed in line 100, and further cooled by indirect heat transfer with a suitable coolant; e.g., boiler feed water, in heat exchanger 152 to a temperature suitable for inducing required recycle in fractionator 101, generally a temperature of from about 400 F. to about 700 F.
  • a suitable coolant e.g., boiler feed water
  • a portion of the cooled heavy oil is passed through line 153 to provide the heavy oil for lines 112 and 122, as hereinabove described.
  • Another portion of the heavy oil from heat exchanger 152 is introduced into the fractionator 101 through line 156 at a rate to provide the hereinabovedescribed volumetric recycle ratio.
  • the total recycle is comprised of the heavy oil fraction returned through line 154 and the condensed portion of the coke drum overhead vapors introduced through lines 102 and 103, the condensation being induced by direct contact with the cooled heavy oil fraction.
  • the remaining portion of the heavy oil fraction from heat exchanger 152 is introduced into the fractionator 101 through line 155 to maintain desired operating conditions and passed through line 156 to storage and/or further treatment; e.g., production of high-grade carbon black as a result of its high BMCI, or recognized aromatic factor and its low sulfur content.
  • needle coke may be produced from the 600 F. to l,000 F. fraction without the simultaneous production of carbon electrode grade coke from the l,000 F. fraction.
  • a separate combination fractionator may be employed for each coking operation instead of the single fractionator as employed in the embodiments illustrated in FIGS. 1 and 2.
  • the use of a second fractionator may be advantageous in some operations in that the needle coke producing drums may then be operated at a higher pressure than the carbon electrode coke drums, without necessitating throttling of vapors.
  • a portion of'the coke drum overhead vapors may be used to assist the flashing in tower 13, such overhead vapors being passed to the fractionator through line 14 in admixture with the fraction flashed from the feed.
  • FIG. 2 may be operated in accordance with the process described in US. application Ser. No. 746,706, with the heavy oil recovered from the combination fractionator being employed for the production of graphitizable needle coke. This procedure is less preferred in that needle coke production is reduced in that the graphitizable needle coke precursors are not effectively recovered in the combination-fractionator.
  • the flash towers 113 and 105 of the embodiments of FIGS. 1 and 2, respectively may be operated as conventional multijet induced vacuum flash towers with the overhead vapors being condensed for tower total reflux return and employed in lines 17 and 110, respectively, as hereinabove-described.
  • the embodiments of FIGS. 1 and 2 may be operated in a manner whereby the feed to the needle coke producing drums contains components boiling above about l,200 F., the components boiling above about l,200 F. comprising no more than about 20 percent of the feed to the needle coke drums, generally from about 5 to about '15 percent of the feed.
  • the heavy oil bottoms in line 22 may be mixed with a portion of coal tar pitch feed stock form line 10 in line 10a to provide components boiling above about l,200 F.
  • coal tar pitch is employed in line 10a in an amount whereby the total feed introduced into heater 23, as hereinabove noted, contains no more than about 20 percent of components boiling above about 1,200 F. It is to be understood, however, that the coal tar pitch in line may be mixed with the heavy oil in line 22 in proportions greater than 20 percent in that the coal tar pitch also contains components boiling below l,200 F. and therefore such greater amounts will not provide more than 20 percent of components boiling above l,200 F. Similarly, in accordance with the embodiment of FIG. 2, coal tar pitch may be added to the feed to the heater 113 in the manner hereinabove described.
  • the distillate and residue were each coked in a single pass atmospheric operation at a temperature of 840-870 F., with the coke produced from the distillate being a graphitizable needle coke having a low longitudinal coefficient of thermal expansion of not substantially above about 6.0Xl" (C.) and the coke produced from the residue having a coefficient of thermal expansion in the range of l2-20Xl0" (C.)", being characterized as carbon electrode grade coke.
  • the dual coking operation produced parts of the needle coke and 36 parts of the carbon electrode grade coke, per 100 parts of whole coal tar pitch.
  • the coking of the pitch without the dual coking of the invention, produces about 56 parts of carbon electrode grade coke per 100 parts of pitch.
  • the heavy oil is further distilled to an initial 650 F. cut point and this distilled fraction coked in a single pass atmospheric operation at a temperature of 840-870 F. to produce the following products:
  • the overall process of the present invention is an improvement over the process of copending application Ser. No. 746,706 in that a feedstock having a high content of condensed ring aromatic compounds is upgraded to a coke commonly referred to as graphitizable needle coke, which after calcination and graphitization has a longitudinal coefficient of thermal expansion/C. not substantially above about 6.0Xl0", rather than solely to carbon electrode grade coke.
  • the process of the invention incorporates the advantages inherent in an effective coking of a feedstock having a high content of condensed ring aromatic compounds, as noted in said copending application; i.e., high coke yields and the like.
  • a delayed coking process for producing graphitizable needle coke from a feed containing coal tar pitch comprising:
  • a delayed coking process for producing graphitizable needle coke from a feed containing coal tar pitch comprising:
  • step (c) is admixed with a coal tar pitch containing fraction in an amount to provide a mixture in which no more than about 20 percent of the components thereof boil above above about l200 F.
  • fractionation zone is operated at an overhead temperature from about 300 F. to about 400 F., a bottoms temperature from about 650 F. to 850 F., a pressure from about 25 p.s.i.g. to about 90 p.s.i.g. and a volumetric recycle ratio, based on equivalent feed to the, fractionation'zone, from about 0.321 to about 2.0:].
  • a delayed coking process for producing graphitizable needle coke comprising:
  • a. introducing a feed containing coal tar pitch into a coker combination fractionation zone operating under conditions to provide a heavy oil fraction having upper and lower cut points within the range from about 600 F. to about l,000 F., said fraction having a high content of condensed ring aromatic compounds, and to flash material boiling at a temperature no greater than about l,000 F. from the feed;
  • a delayed coking process for producing graphitizable needle coke and carbon grade coke from a feed containing coal tar pitch comprising:
  • a delayed coking process for producing graphitizable needle coke and carbon grade coke from a feed containing coal tar pitch comprising:
  • a delayed coking process for producing graphitizable needle coke and carbon grade coke from a feed containing coal tar pitch comprising:
  • a. introducing a feed containing coal tar pitch into a coker combination fractionation zone operating under conditions to provide a heavy oil fraction having upper and lower cut points within the range from about 600 F. to about l,000 F., said fraction having a high content of condensed ring aromatic compounds, and to flash material boiling at a temperature no greater than about l,000 F. from the feed;

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Coke Industry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
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Cited By (22)

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JPS5162804A (en) * 1974-11-29 1976-05-31 Mitsui Cokes Kogyo Kk Shinjokookusuno seizohoho
US4066532A (en) * 1975-06-30 1978-01-03 Petroleo Brasileiro S.A. Petrobras Process for producing premium coke and aromatic residues for the manufacture of carbon black
US4096097A (en) * 1976-12-27 1978-06-20 Mobil Oil Corporation Method of producing high quality sponge coke or not to make shot coke
US4111794A (en) * 1976-04-03 1978-09-05 Sigri Elektrographit Gmbh Method of producing pitch coke
US4127472A (en) * 1976-11-26 1978-11-28 Nittetsu Chemical Industrial Co., Ltd. Process for preparing a raw material for the manufacture of needle coke
US4216074A (en) * 1978-08-30 1980-08-05 The Lummus Company Dual delayed coking of coal liquefaction product
US4219404A (en) * 1979-06-14 1980-08-26 Exxon Research & Engineering Co. Vacuum or steam stripping aromatic oils from petroleum pitch
US4621724A (en) * 1984-09-13 1986-11-11 Foster Wheeler Energy Corporation Fractionator having reduced product vapor condensation in the flash zone
US4624775A (en) * 1984-10-22 1986-11-25 Union Carbide Corporation Process for the production of premium coke from pyrolysis tar
US4737261A (en) * 1984-10-05 1988-04-12 International Coal Refining Company Process for the production of premium grade needle coke from a hydrotreated SRC material
US4983272A (en) * 1988-11-21 1991-01-08 Lummus Crest, Inc. Process for delayed coking of coking feedstocks
CN102041013A (zh) * 2009-10-16 2011-05-04 中国石油化工股份有限公司 利用延迟焦化工艺生产针状焦原料的方法
US20110186478A1 (en) * 2008-09-09 2011-08-04 Jx Nippon Oil & Energy Corporation Process for producing needle coke for graphite electrode and stock oil composition for use in the process
CN103045278A (zh) * 2011-10-17 2013-04-17 中国石油化工股份有限公司 一种釜式制备针状焦的方法
CN103113907A (zh) * 2013-01-30 2013-05-22 陕西煤业化工技术研究院有限责任公司 一种制备煤系针状焦的工艺方法
CN105514439A (zh) * 2016-01-20 2016-04-20 上海应用技术学院 一种锂离子电池炭负极材料及其制备工艺
CN105713647A (zh) * 2016-03-31 2016-06-29 陕西煤业化工集团神木天元化工有限公司 一种利用煤焦油最大化制备含酚油和柴油的方法及装置
WO2017011644A1 (en) * 2015-07-14 2017-01-19 Kellogg Brown & Root Llc Co-production of anode and fuel grade petroleum coke in a delayed coker unit
US10253264B2 (en) * 2006-06-29 2019-04-09 Graftech International Holdings Inc. Method of producing needle coke for low CTE graphite electrodes
US20210179945A1 (en) * 2019-12-11 2021-06-17 Saudi Arabian Oil Company Needle coke production from hpna recovered from hydrocracking unit
EP3950887A1 (en) 2020-08-05 2022-02-09 Indian Oil Corporation Limited Process for production of graphite coke from an admixture of coal and petroleum based hydrocarbons
CN114369473A (zh) * 2020-10-15 2022-04-19 山东方宇润滑油有限公司 一种油基针状焦焦化塔放空气回收装置及工艺

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Publication number Priority date Publication date Assignee Title
JPS5641817A (en) * 1979-09-06 1981-04-18 Mitsubishi Chem Ind Ltd Manufacture of molded carbon material
US4894144A (en) * 1988-11-23 1990-01-16 Conoco Inc. Preparation of lower sulfur and higher sulfur cokes
DE10057678A1 (de) 2000-11-21 2002-05-29 Thueringisches Inst Textil Verfahren zur Herstellung von schmelzfähigen Polyestern
CN111925816A (zh) * 2020-07-22 2020-11-13 山东益大新材料股份有限公司 一种低cte煤系针状焦的生产方法

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JPS5162804A (en) * 1974-11-29 1976-05-31 Mitsui Cokes Kogyo Kk Shinjokookusuno seizohoho
US4029749A (en) * 1974-11-29 1977-06-14 Mitsui Coke Co. Ltd. Process for manufacturing needle coke
US4066532A (en) * 1975-06-30 1978-01-03 Petroleo Brasileiro S.A. Petrobras Process for producing premium coke and aromatic residues for the manufacture of carbon black
US4111794A (en) * 1976-04-03 1978-09-05 Sigri Elektrographit Gmbh Method of producing pitch coke
US4127472A (en) * 1976-11-26 1978-11-28 Nittetsu Chemical Industrial Co., Ltd. Process for preparing a raw material for the manufacture of needle coke
US4096097A (en) * 1976-12-27 1978-06-20 Mobil Oil Corporation Method of producing high quality sponge coke or not to make shot coke
US4216074A (en) * 1978-08-30 1980-08-05 The Lummus Company Dual delayed coking of coal liquefaction product
US4219404A (en) * 1979-06-14 1980-08-26 Exxon Research & Engineering Co. Vacuum or steam stripping aromatic oils from petroleum pitch
US4621724A (en) * 1984-09-13 1986-11-11 Foster Wheeler Energy Corporation Fractionator having reduced product vapor condensation in the flash zone
US4737261A (en) * 1984-10-05 1988-04-12 International Coal Refining Company Process for the production of premium grade needle coke from a hydrotreated SRC material
US4624775A (en) * 1984-10-22 1986-11-25 Union Carbide Corporation Process for the production of premium coke from pyrolysis tar
US4983272A (en) * 1988-11-21 1991-01-08 Lummus Crest, Inc. Process for delayed coking of coking feedstocks
US10253264B2 (en) * 2006-06-29 2019-04-09 Graftech International Holdings Inc. Method of producing needle coke for low CTE graphite electrodes
US20110186478A1 (en) * 2008-09-09 2011-08-04 Jx Nippon Oil & Energy Corporation Process for producing needle coke for graphite electrode and stock oil composition for use in the process
US8715484B2 (en) 2008-09-09 2014-05-06 Jx Nippon Oil & Energy Corporation Process for producing needle coke for graphite electrode and stock oil composition for use in the process
CN102041013A (zh) * 2009-10-16 2011-05-04 中国石油化工股份有限公司 利用延迟焦化工艺生产针状焦原料的方法
CN102041013B (zh) * 2009-10-16 2013-07-24 中国石油化工股份有限公司 利用延迟焦化工艺生产针状焦原料的方法
CN103045278A (zh) * 2011-10-17 2013-04-17 中国石油化工股份有限公司 一种釜式制备针状焦的方法
CN103113907B (zh) * 2013-01-30 2014-06-18 陕西煤业化工技术研究院有限责任公司 一种制备煤系针状焦的工艺方法
CN103113907A (zh) * 2013-01-30 2013-05-22 陕西煤业化工技术研究院有限责任公司 一种制备煤系针状焦的工艺方法
WO2017011644A1 (en) * 2015-07-14 2017-01-19 Kellogg Brown & Root Llc Co-production of anode and fuel grade petroleum coke in a delayed coker unit
US10316253B2 (en) 2015-07-14 2019-06-11 Kellog Brown & Root Llc Co-production of anode and fuel grade petroleum coke in a delayed coker unit
CN105514439A (zh) * 2016-01-20 2016-04-20 上海应用技术学院 一种锂离子电池炭负极材料及其制备工艺
CN105713647A (zh) * 2016-03-31 2016-06-29 陕西煤业化工集团神木天元化工有限公司 一种利用煤焦油最大化制备含酚油和柴油的方法及装置
US20210179945A1 (en) * 2019-12-11 2021-06-17 Saudi Arabian Oil Company Needle coke production from hpna recovered from hydrocracking unit
US12077714B2 (en) * 2019-12-11 2024-09-03 Saudi Arabian Oil Company Needle coke production from HPNA recovered from hydrocracking unit
EP3950887A1 (en) 2020-08-05 2022-02-09 Indian Oil Corporation Limited Process for production of graphite coke from an admixture of coal and petroleum based hydrocarbons
US11643607B2 (en) 2020-08-05 2023-05-09 Indian Oil Corporation Limited Process for production of graphite coke from an admixture of coal and petroleum based hydrocarbons
CN114369473A (zh) * 2020-10-15 2022-04-19 山东方宇润滑油有限公司 一种油基针状焦焦化塔放空气回收装置及工艺

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DE2025071B2 (de) 1974-05-22
CA937521A (en) 1973-11-27
DE2025071C3 (de) 1979-12-06
DE2025071A1 (de) 1970-12-03
FR2048847A5 (enrdf_load_stackoverflow) 1971-03-19
GB1290234A (enrdf_load_stackoverflow) 1972-09-20
BE750899A (fr) 1970-11-03
JPS4949004B1 (enrdf_load_stackoverflow) 1974-12-25

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