US3563884A - Delayed coking of coal tar pitches - Google Patents

Delayed coking of coal tar pitches Download PDF

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Publication number
US3563884A
US3563884A US746706A US3563884DA US3563884A US 3563884 A US3563884 A US 3563884A US 746706 A US746706 A US 746706A US 3563884D A US3563884D A US 3563884DA US 3563884 A US3563884 A US 3563884A
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United States
Prior art keywords
coking
feed
fractionator
temperature
coke
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Expired - Lifetime
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US746706A
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English (en)
Inventor
Ward J Bloomer
William P Brison
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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

Definitions

  • the coker combination fractionator is operated at a temperature and pressure to recover a heavy oil having an initial boiling point of 600 F.-750 F.
  • the recycle of a portion of the overhead from the coking drums introduced into the fractionator is at a volumetric rate of 0.30.6:l, based on equivalent feed introduced into the coking heater. Operation of the delayed coking unit under the above conditions prevents the runaway reactions heretofore encountered when attempting to delay coke such feeds.
  • This invention relates to the production of coke and more particularly to a new and improved process for the delayed coking of liquid feed stocks having a high content of polynuclear aromatic compounds.
  • the delayed coking of petroleum derived residual, oils is one of the more important processes in the petrochemical industry in that both coke and a series of useful gas and liquid products may be produced thereby.
  • the residual oils may be converted to C and lighter gases, liquefied petroleum gases (LPG), light gasoline, heavy gasoline for catalytic reforming, light gas oil which may be treated to produce diesel or furnace oil and heavy gas oil for feed to a catalytic cracking operation.
  • LPG liquefied petroleum gases
  • an object of this invention is to provide an effective process for the delayed coking of liquid feeds having a high content of polynuclear aromatic compounds.
  • Another object of this invention is to provide a new and improved process for the delayed coking of liquid feed stocks having a high content of polynuclear aromatic compounds that eliminates previously encountered problems.
  • a further object of this invention is to provide a process particularly adapted to producing coke and other useful products from coal tar pitches.
  • the objects of this invention are broadly accomplished by effecting the delayed coking of a high boiling liquid feed stock having a high content of polynuclear aromatic compounds in a delayed coking unit of the type conventionally employed for the delayed coking of petroleum de 3,563,884 Patented Feb. 16, 1971 rived feed stocks, except that the unit is operated at a coke drum overhead temperature of between about 840 F. and about 900 F., preferably between about 860 F. and about 900 F., and a volumetric recycle ratio of between 5 about 03:1 and about 0.6:1, preferably between about 0.5 :1 and about 0.6:1, based on equivalent fresh feed.
  • equivalent fresh feed means the total feed introduced into the coking heater after flashing therefrom material boiling below the end point of the light oil to be recovered.
  • the feed is introduced into the bottom of the coker fractionator and material below the end point of the light oil to be recovered in the fractionator is flashed therefrom.
  • the equivalent fresh feed is the 15 total feed introduced into the fractionator minus the material flashed from the feed in the fractionator.
  • the liquid feeds treated in accordance with the invention have a high content; i.e., generally greater than about 70%, of condensed ring (polynuclear) aromatic compounds, both heterocyclic and isocyclic, and an initial boiling point no lower than about 600 F., generally an initial boiling point between about 600 F. and about 750 F., all converted to one atmosphere.
  • a preferred feed is a coal tar pitch obtained by either the high temperature or low temperature carbonization of coal, as gen-r erally known in the art, the former feed particularly being generally characterized as completely comprised of condensed ring aromatic compounds (an estimated 5000 of such compounds), with two-thirds of the aromatic compounds being isocyclic and the remaining third heterocyclic. It is to be understood that the initial feed may be a feed which does not meet the hereinabove characteristics;
  • a liquid feed such as, soft coal tar pitch derived from the high temperature carbonization of coal
  • line 10 is passed through heat exchanger 11 to effect heating thereof by indirect heat transfer with a heavy oil fraction, as hereinafter described, and introduced into the bottom of the coker combination fractionator 12, of a type known in the art, through line 13 to flash off material below the end point of the light gas oil tosbe recovered in the fractionator 12; i.e., material boiling below a temperature within the range between about 600 F. and about 750 F., preferably below about 600 F.
  • the operation of the fractionator 12 will be hereinafter more fully described.
  • the coking heater is operated so as to produce an outlet temperature of between about 900 F. and about 960 F.
  • the coking heater 15 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 15 through line 16 at appropriate places to obtain the required turbulence or high velocity.
  • the heated combined feed is withdrawn from the coking heater 15 through line 17 and introduced into coke drums 18, of a type known in the art, wherein the heavier components of the feed are converted to 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 18 through line 19.
  • An overhead is withdrawn from the coke drums 18 through line 21 and introduced into the coker combination fractionator 12 to recover the various components, as known in the art.
  • the fractionator is generally run at an overhead temperature between about 300 F. and about 400 F., a bottoms chimney temperature of about 750 F. to about 810 F. and a pressure between about 25 and about 40 p.s.i.g.
  • the overhead from the coke drum is separated in the fractionator 12 into a light oil generally having cut points between about 400 F. and 750 F., preferably between about 400 F. and about 600 F., a heavy oil having an initial boiling point within the range between about 600 F. and about 750 F preferably between about 600 F. and 700 F. and an overhead vapor stream comprised of distillate, generally boiling up to about 400 F., and gas.
  • the heavy oil having an initial boiling point which falls somewhere within the range between about 600 F. and about 750 F. is withdrawn from the fractionator 12 through line 22, cooled in heat exchanger 11 by indirect heat transfer with the feed in line 10 and further cooled in heat exchanger 23 to a temperature suitable for inducing required recycle in fractionator 12, generally a temperature between about 400 F. and about 700 F., by indirect heat transfer with a suitable coolant, for example, boiler feed water.
  • a portion of the cooled heavy oil from heat exchanger 23 is introduced into the fractionator 12 through line 25 at a rate to provide a volumetric recycle ratio of between about 0.3:1 and about 0.6:1, preferably between :1 and about 0611, based upon equivalent feed.
  • the total recycle is comprised of the heavy oil fraction recovered from the coke drum overhead in fractionator 12, returned through line 25 and a condensed portion of the coke overhead vapors introduced through line 21, the condensation being induced by direct contact with the cooled heavy oil fraction.
  • the remaining heavy oil from heat exchanger 23 is passed through line 26 to maintain desired operating conditions in the fractionator 12 and through line 27 to storage and/ or further treatment.
  • the feed may be treated to effect vaporization of material below the end point of the light gas oil to be recovered in the delayed coking process in apparatus other than the coker combination fractionator.
  • the various heat transfer steps may be effected otherwise than as hereinabove described, for example, the feed to the combination fractionator may be heated in the coking heater or another heater.
  • the heavy gas oil recycled through line 25 provides a iecycle ratio of 0.5 :1 by volume, based on equivalent eed.
  • the fractionator 12 is operated at an overhead temperature of 355 F. and pressure of 25 p.s.i.g., and a bottoms chimney temperature of 800 F. and pressure of 30 p.s.i.g., whereby the initial boiling point of the equivalent feed is about 600 F. and the following liquid products are recovered, based on total feed.
  • Coke is produced at a rate of 21,600 lbs/hr. (55.40 wt. percent, based on fresh feed) and has the following properties:
  • the coke produced in accordance with the invention has an extremely low ash content; from nil to a maximum of about 0.1, which makes the coke eminently suitable for the production of high purity metals; e.g., in the electrolytic reduction of alumina.
  • the liquid products recovered in the coker combination fractionator is similar to a commercial heavy tar distillate; i.e., the total distillate comprises aromatic fractions similar to those characterized in the coal tar industry as tar light oil, carbolic oil, naphthalene oil, and wash oil.
  • a process for the delayed coking of a coal tar pitch comprising:

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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)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Coke Industry (AREA)
  • Working-Up Tar And Pitch (AREA)
US746706A 1968-07-15 1968-07-15 Delayed coking of coal tar pitches Expired - Lifetime US3563884A (en)

Applications Claiming Priority (1)

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US74670668A 1968-07-15 1968-07-15

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US3563884A true US3563884A (en) 1971-02-16

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US746706A Expired - Lifetime US3563884A (en) 1968-07-15 1968-07-15 Delayed coking of coal tar pitches

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US (1) US3563884A (enrdf_load_stackoverflow)
BE (1) BE736121A (enrdf_load_stackoverflow)
DE (1) DE1935467C3 (enrdf_load_stackoverflow)
FR (1) FR2013014A1 (enrdf_load_stackoverflow)
GB (1) GB1238410A (enrdf_load_stackoverflow)

Cited By (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4216074A (en) * 1978-08-30 1980-08-05 The Lummus Company Dual delayed coking of coal liquefaction product
US4251346A (en) * 1977-12-21 1981-02-17 Sasol One (Proprietary) Limited Process for coal liquefaction
US4289604A (en) * 1976-04-03 1981-09-15 Bergwerksverband Gmbh Method of producing an isotropic coke
US4492625A (en) * 1983-11-17 1985-01-08 Exxon Research And Engineering Co. Delayed coking process with split fresh feed
US4518487A (en) * 1983-08-01 1985-05-21 Conoco Inc. Process for improving product yields from delayed coking
US4534854A (en) * 1983-08-17 1985-08-13 Exxon Research And Engineering Co. Delayed coking with solvent separation of recycle oil
US4549934A (en) * 1984-04-25 1985-10-29 Conoco, Inc. Flash zone draw tray for coker fractionator
US4624775A (en) * 1984-10-22 1986-11-25 Union Carbide Corporation Process for the production of premium coke from pyrolysis tar
US6048448A (en) * 1997-07-01 2000-04-11 The Coastal Corporation Delayed coking process and method of formulating delayed coking feed charge
RU2314333C1 (ru) * 2006-09-21 2008-01-10 Открытое акционерное общество "Научно-исследовательский и проектный институт нефтеперерабатывающей и нефтехимической промышленности" Способ замедленного коксования
US20090139899A1 (en) * 2006-07-28 2009-06-04 Gloria Maria Gomes Soares Process of Modification of a Feedstock in a Delayed Coking Unit
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
CN101619238B (zh) * 2008-07-04 2012-08-29 中国石油化工股份有限公司 一种延迟焦化-减压蒸馏联合加工方法
US8894841B2 (en) 2011-07-29 2014-11-25 Saudi Arabian Oil Company Solvent-assisted delayed coking process
US9023193B2 (en) 2011-05-23 2015-05-05 Saudi Arabian Oil Company Process for delayed coking of whole crude oil
US9023192B2 (en) 2011-07-29 2015-05-05 Saudi Arabian Oil Company Delayed coking process utilizing adsorbent materials
US9574143B2 (en) 2010-09-07 2017-02-21 Saudi Arabian Oil Company Desulfurization and sulfone removal using a coker
CN108251143A (zh) * 2016-12-28 2018-07-06 上海宝钢化工有限公司 一种采用塔底沥青制备沥青焦的方法
US10093870B2 (en) 2010-09-07 2018-10-09 Saudi Arabian Oil Company Desulfurization and sulfone removal using a coker
US10093871B2 (en) 2010-09-07 2018-10-09 Saudi Arabian Oil Company Desulfurization and sulfone removal using a coker
RU2686152C1 (ru) * 2018-12-24 2019-04-24 Общество с ограниченной ответственностью "ХАММЕЛЬ" Способ получения нефтяного игольчатого кокса
RU2717815C1 (ru) * 2019-09-16 2020-03-25 Акционерное общество "Газпромнефть - Омский НПЗ" (АО "Газпромнефть-ОНПЗ" Способ получения нефтяного игольчатого кокса
RU2720191C1 (ru) * 2019-09-16 2020-04-27 Акционерное общество "Газпромнефть - Омский НПЗ" (АО "Газпромнефть-ОНПЗ") Установка для получения нефтяного игольчатого кокса замедленным коксованием
US20210179945A1 (en) * 2019-12-11 2021-06-17 Saudi Arabian Oil Company Needle coke production from hpna recovered from hydrocracking unit

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
PL112436B1 (en) * 1978-01-23 1980-10-31 Instytut Technologii Nafty Preparation of stock charge for manufacturing of electrode coke
US4455219A (en) * 1982-03-01 1984-06-19 Conoco Inc. Method of reducing coke yield
US4551232A (en) * 1983-02-09 1985-11-05 Intevep, S.A. Process and facility for making coke suitable for metallurgical purposes
RU2256687C1 (ru) * 2004-02-02 2005-07-20 Государственное унитарное предприятие "Институт нефтехимпереработки Республики Башкортостан" (ГУП ИНХП РБ) Способ замедленного коксования нефтяных остатков

Cited By (27)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4289604A (en) * 1976-04-03 1981-09-15 Bergwerksverband Gmbh Method of producing an isotropic coke
US4251346A (en) * 1977-12-21 1981-02-17 Sasol One (Proprietary) Limited Process for coal liquefaction
US4216074A (en) * 1978-08-30 1980-08-05 The Lummus Company Dual delayed coking of coal liquefaction product
US4518487A (en) * 1983-08-01 1985-05-21 Conoco Inc. Process for improving product yields from delayed coking
US4534854A (en) * 1983-08-17 1985-08-13 Exxon Research And Engineering Co. Delayed coking with solvent separation of recycle oil
US4492625A (en) * 1983-11-17 1985-01-08 Exxon Research And Engineering Co. Delayed coking process with split fresh feed
US4549934A (en) * 1984-04-25 1985-10-29 Conoco, Inc. Flash zone draw tray for coker fractionator
US4624775A (en) * 1984-10-22 1986-11-25 Union Carbide Corporation Process for the production of premium coke from pyrolysis tar
US6048448A (en) * 1997-07-01 2000-04-11 The Coastal Corporation Delayed coking process and method of formulating delayed coking feed charge
US20090139899A1 (en) * 2006-07-28 2009-06-04 Gloria Maria Gomes Soares Process of Modification of a Feedstock in a Delayed Coking Unit
RU2314333C1 (ru) * 2006-09-21 2008-01-10 Открытое акционерное общество "Научно-исследовательский и проектный институт нефтеперерабатывающей и нефтехимической промышленности" Способ замедленного коксования
CN101619238B (zh) * 2008-07-04 2012-08-29 中国石油化工股份有限公司 一种延迟焦化-减压蒸馏联合加工方法
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
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
US10093871B2 (en) 2010-09-07 2018-10-09 Saudi Arabian Oil Company Desulfurization and sulfone removal using a coker
US9574143B2 (en) 2010-09-07 2017-02-21 Saudi Arabian Oil Company Desulfurization and sulfone removal using a coker
US10093870B2 (en) 2010-09-07 2018-10-09 Saudi Arabian Oil Company Desulfurization and sulfone removal using a coker
US9023193B2 (en) 2011-05-23 2015-05-05 Saudi Arabian Oil Company Process for delayed coking of whole crude oil
US8894841B2 (en) 2011-07-29 2014-11-25 Saudi Arabian Oil Company Solvent-assisted delayed coking process
US9023192B2 (en) 2011-07-29 2015-05-05 Saudi Arabian Oil Company Delayed coking process utilizing adsorbent materials
CN108251143A (zh) * 2016-12-28 2018-07-06 上海宝钢化工有限公司 一种采用塔底沥青制备沥青焦的方法
CN108251143B (zh) * 2016-12-28 2021-03-05 宝武炭材料科技有限公司 一种采用塔底沥青制备沥青焦的方法
RU2686152C1 (ru) * 2018-12-24 2019-04-24 Общество с ограниченной ответственностью "ХАММЕЛЬ" Способ получения нефтяного игольчатого кокса
RU2717815C1 (ru) * 2019-09-16 2020-03-25 Акционерное общество "Газпромнефть - Омский НПЗ" (АО "Газпромнефть-ОНПЗ" Способ получения нефтяного игольчатого кокса
RU2720191C1 (ru) * 2019-09-16 2020-04-27 Акционерное общество "Газпромнефть - Омский НПЗ" (АО "Газпромнефть-ОНПЗ") Установка для получения нефтяного игольчатого кокса замедленным коксованием
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

Also Published As

Publication number Publication date
FR2013014A1 (enrdf_load_stackoverflow) 1970-03-27
DE1935467A1 (de) 1970-01-22
BE736121A (enrdf_load_stackoverflow) 1969-12-16
DE1935467B2 (de) 1973-09-13
GB1238410A (enrdf_load_stackoverflow) 1971-07-07
DE1935467C3 (de) 1974-04-04

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