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EP0250136A2 - Procédé de cokéfaction retardée - Google Patents

Procédé de cokéfaction retardée Download PDF

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Publication number
EP0250136A2
EP0250136A2 EP87305009A EP87305009A EP0250136A2 EP 0250136 A2 EP0250136 A2 EP 0250136A2 EP 87305009 A EP87305009 A EP 87305009A EP 87305009 A EP87305009 A EP 87305009A EP 0250136 A2 EP0250136 A2 EP 0250136A2
Authority
EP
European Patent Office
Prior art keywords
fluid
coke
coker
steam
fractionator
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP87305009A
Other languages
German (de)
English (en)
Other versions
EP0250136B1 (fr
EP0250136A3 (en
Inventor
Michael John Mcgrath
Rino Lodivico Godino
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Foster Wheeler Inc
Amec Foster Wheeler USA Corp
Original Assignee
Foster Wheeler USA Corp
Foster Wheeler Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Foster Wheeler USA Corp, Foster Wheeler Inc filed Critical Foster Wheeler USA Corp
Publication of EP0250136A2 publication Critical patent/EP0250136A2/fr
Publication of EP0250136A3 publication Critical patent/EP0250136A3/en
Application granted granted Critical
Publication of EP0250136B1 publication Critical patent/EP0250136B1/fr
Expired legal-status Critical Current

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Classifications

    • 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
    • C10B57/04—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition
    • C10B57/06—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition containing additives
    • 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
    • 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
    • C10B57/04—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition
    • C10B57/045—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition containing mineral oils, bitumen, tar or the like or mixtures thereof
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/005—Coking (in order to produce liquid products mainly)

Definitions

  • the present invention relates to delayed coking.
  • this invention relates to a process for minimizing the quantity of coke produced in a delayed coking process.
  • Delayed coking is a process in which heavy oil is rap­idly heated in a coker furnace and then passed to a reac­tion zone comprising one or more coke drums. There, the heavy oil undergoes cracking and condensation reactions, resulting in coke and a full boiling range of oils and gases which are then subjected to fractionation in a coker fractionator.
  • the goal in a delayed coking process is to minimize the quantity of low value coke while maximizing the quanti­ty of liquid product output.
  • the pressure in the coke drum is set at minimum levels. In today's delayed cokers, the minimum practical pressure level is about 10 to 15 psig. To achieve lower pressures requires large and expensive equipment with high compression requirements.
  • the same result can be achieved by operating the process at a low­ered effective pressure, which is achieved by lowering the partial pressure of the heavy oil in the coke drum.
  • the quantity of steam or water injected into the coker furnace has conventionally been limited to only that amount of steam or water required to maintain the velocity of the heavy oil and reduce coking in the furnace tubes.
  • certain instruments and valves are purged with steam, but again the rate is set at the minimum required to meet the purging requirements.
  • the delayed coking process is such that large amounts of waste heat can be recovered in the fractionation portion of the process. Some of this heat is available at high and useful levels. Some of it is at such a temperature as to be useful only for producing low pressure steam. Fre­quently, this steam is in excess and is of little or no value.
  • the instant invention provides for using this low value heat, or low value heat from another process, to pro­vide an inexpensive source of steam or other heated fluid that can be used to reduce the partial pressure of the heavy oil in the coke drums and thereby the amount of coke formed therein.
  • the instant invention then is a method for reducing coke formation in a delayed coking process carried out in a coker unit comprised of a coker furnace, a coke drum and a coker fractionator, wherein heavy oil is heated to coking temperature in the coker furnace and then passed to the coke drum where coke and overhead vapors are formed and wherein the overhead vapors are passed to the coker frac­tionator, this method comprising introducing into the coke drum a fluid in an amount sufficient to lower the partial pressure of the heavy oil in the coke drum.
  • the heated fluid is sour water, recovered from the coker fractionator.
  • the heated fluid is steam, which can be superheated by passing the fluid through the coker furnace.
  • One of the advantages of this invention is that fluids already present in the delayed coking process, such as sour water recovered from the coker fractionator, or other flu­ids, can be used to reduce the partial pressure of the oil in the coke drum and thereby achieve decreased coke yields.
  • Another advantage is that heat available within the delayed coking process, which is of low value otherwise, is used to preheat the fluids to be used in the coke drum.
  • Another consequential advantage of this invention is that a lower than normal coker furnace outlet temperatures can be used by introducing superheated fluid into the coke drum, the superheated fluid obtained by passing the fluid through the coker furnace.
  • fresh coker feedstock which can be preheated from a means not shown, is introduced into the bottom of the coker fractionator through line 1.
  • the invention is particularly useful when oils having an API gravity of about 15 degrees or heavier are coked.
  • Typical feedstocks to which the invention is especially useful include vacuum residues, asphalts and coal tar pitches.
  • Feed which has been stored in the coker fractionator is withdrawn via line 3 and fed into the coker furnace where the oil is heated to coking temperature.
  • the coker furnace will operate at a temper­ature ranging from about 475°C to about 525°C and a pres­sure of about 15 to about 75 psig.
  • the tempera­ture will range from about 490°C to about 510°C and the pressure will range from about 20 to about 50 psig.
  • the oil is then transferred via transfer line 5 to one of several coke drums 6 and 7, where the oil is coked.
  • the coke drums are maintained at a coking temperature generally ranging from about 415°C to about 470°C and a pressure from about 10 psig to about 35 psig.
  • the tempera­ture and pressure preferrably range from about 435°C to about 455 and about 15 psig to about 25 psig, respectively.
  • More than one coke drum is used so that when one of the coke drums is full of solid coke, the feed can be switched to another drum. The full drum is then cooled and emptied by conventional methods.
  • Vapors leaving the coke drums via line 8 are returned to the fractionator. These vapors are fractionated to pro­duce desired products including heavy coker gas oil, light coker gas oil, overhead naphtha and overhead gases. Over­head gases are recovered through line 10, heat exchanger 12, knock-out drum 14 and line 15. Coker naphtha is recov­ered through lines 16 and 17. Light coker gas oil is re­covered through line 18. Heavy coker gas oil is recovered through line 20 and sour water is recovered through line 11.
  • low pressure steam or heated fluid is introduced via line 9, into transfer line 5 and/or directly into coke drums 6 and 7 through lines 21 and 22.
  • the heated fluid introduced into the coke drums to lower the effective pressure of the oil can be generally be any fluid, including water, sour water, steam, gases, naph­tha, or other material which can be vaporized by low level heat.
  • the fluid is a gas at 60°F and atmo­spheric pressure.
  • the fluid is water, sour water, naphtha or steam.
  • the fluid is preferably heated according to the inven­tion using low level heat from the coker fractionator. This can be accomplished through conventional heat exchange processes known in the art.
  • the fluid is generally heated so that it will not adversely lower the temperature of the coke drums. Gener­ally, this temperature ranges from about 415°C to about 535°C and preferably from about 480°C to about 510°C. Alternatively, heated fluid product of the fractionator can be used directly. The fluid can also be superheated by being passed through the coker furnace.
  • the amount of the fluid introduced into the coke drums depends upon the type of fluid and the pro­cessing conditions.
  • the amount of fluid intro­duced into the drum ranges from about 0.2 lbmols/bbl of fresh feed to about 5.0 lbmols/bbl of fresh feed.
  • sour water recovered from the fractionator, through lines 10, 11 and 23, is heated using reflux from line 13 and then introduced through line 9 into transfer line 5 and/or directly into coke drums 6 and 7 through lines 21 and 22.
  • sour water from line 23 is converted to steam using column 24 with heat from reflux line 13, which exchanges with recycle in line 26.
  • the steam from column 24 can be superheated by passing it through line 25 and the coker furnace.
  • the superheated steam allows for the use of a lower outlet temperature from the coker furnace for the oil transfered via line 5.
  • Figure 5 demonstrates the use of other fluids, such as naphtha, which is withdrawn from the fractionator through lines 10, 16, 17, 23, and 9.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Coke Industry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
EP19870305009 1986-06-09 1987-06-05 Procédé de cokéfaction retardée Expired EP0250136B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US87194686A 1986-06-09 1986-06-09
US871946 1986-06-09

Publications (3)

Publication Number Publication Date
EP0250136A2 true EP0250136A2 (fr) 1987-12-23
EP0250136A3 EP0250136A3 (en) 1989-03-15
EP0250136B1 EP0250136B1 (fr) 1992-02-19

Family

ID=25358514

Family Applications (1)

Application Number Title Priority Date Filing Date
EP19870305009 Expired EP0250136B1 (fr) 1986-06-09 1987-06-05 Procédé de cokéfaction retardée

Country Status (5)

Country Link
EP (1) EP0250136B1 (fr)
JP (1) JPH06104834B2 (fr)
CA (1) CA1279838C (fr)
DE (1) DE3776729D1 (fr)
ES (1) ES2030063T3 (fr)

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0956324A4 (fr) * 1996-03-20 2000-01-12 Conoco Inc Procede destine a accroitre le rendement en produits liquides dans un processus de cokefaction differee
WO2008027139A1 (fr) * 2006-08-31 2008-03-06 Exxonmobil Chemical Patents Inc. Procédé de valorisation d'un goudron de vapocraqueur en utilisant une unité pox/cokeur
WO2011005918A3 (fr) * 2009-07-10 2011-03-03 Exxonmobil Research And Engineering Company Procédé de cokéfaction retardée
US8057640B2 (en) 2006-10-30 2011-11-15 Exxonmobil Chemical Patents Inc. Deasphalting tar using stripping tower
US8083930B2 (en) 2006-08-31 2011-12-27 Exxonmobil Chemical Patents Inc. VPS tar separation
US20130026069A1 (en) * 2011-07-29 2013-01-31 Omer Refa Koseoglu Solvent-assisted delayed coking process
US8709233B2 (en) 2006-08-31 2014-04-29 Exxonmobil Chemical Patents Inc. Disposition of steam cracked tar
US20190284482A1 (en) * 2018-03-13 2019-09-19 Lummus Technology Llc In situ coking of heavy pitch and other feedstocks with high fouling tendency
CN114369474A (zh) * 2020-10-15 2022-04-19 山东方宇润滑油有限公司 一种油基针状焦生产装置及生产工艺
RU2775970C2 (ru) * 2018-03-13 2022-07-12 ЛАММУС ТЕКНОЛОДЖИ ЭлЭлСи Коксование на месте тяжелого пека и другого сырья с высокой тенденцией к загрязнению

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4983272A (en) * 1988-11-21 1991-01-08 Lummus Crest, Inc. Process for delayed coking of coking feedstocks
JP5743552B2 (ja) * 2008-02-14 2015-07-01 ロジャー・ジー・エッター 所望の生成物の収率および特性を改善するために添加剤をコーキング法に導入するシステムおよび方法
US9139781B2 (en) 2009-07-10 2015-09-22 Exxonmobil Research And Engineering Company Delayed coking process
WO2014035279A1 (fr) * 2012-08-29 2014-03-06 Общество С Ограниченной Ответственностью "Проминтех" Procédé de cokéfaction ralentie de résidus pétroliers
US11920099B2 (en) 2021-11-23 2024-03-05 Saudi Arabian Oil Company Extruder systems and processes for production of petroleum coke
US11959022B2 (en) 2021-11-23 2024-04-16 Saudi Arabian Oil Company Extruder systems and processes for production of petroleum coke and mesophase pitch

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3956101A (en) * 1970-10-09 1976-05-11 Kureha Kagaku Kogyo Kabushiki Kaisha Production of cokes
US4036736A (en) * 1972-12-22 1977-07-19 Nippon Mining Co., Ltd. Process for producing synthetic coking coal and treating cracked oil
JPS595165B2 (ja) * 1976-09-29 1984-02-03 ダイキン工業株式会社 液圧制御装置
US4519898A (en) * 1983-05-20 1985-05-28 Exxon Research & Engineering Co. Low severity delayed coking
US4518487A (en) * 1983-08-01 1985-05-21 Conoco Inc. Process for improving product yields from delayed coking

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0956324A4 (fr) * 1996-03-20 2000-01-12 Conoco Inc Procede destine a accroitre le rendement en produits liquides dans un processus de cokefaction differee
US8083930B2 (en) 2006-08-31 2011-12-27 Exxonmobil Chemical Patents Inc. VPS tar separation
WO2008027139A1 (fr) * 2006-08-31 2008-03-06 Exxonmobil Chemical Patents Inc. Procédé de valorisation d'un goudron de vapocraqueur en utilisant une unité pox/cokeur
US8709233B2 (en) 2006-08-31 2014-04-29 Exxonmobil Chemical Patents Inc. Disposition of steam cracked tar
US8083931B2 (en) 2006-08-31 2011-12-27 Exxonmobil Chemical Patents Inc. Upgrading of tar using POX/coker
US8057640B2 (en) 2006-10-30 2011-11-15 Exxonmobil Chemical Patents Inc. Deasphalting tar using stripping tower
US8496805B2 (en) 2009-07-10 2013-07-30 Exxonmobil Research And Engineering Company Delayed coking process
WO2011005918A3 (fr) * 2009-07-10 2011-03-03 Exxonmobil Research And Engineering Company Procédé de cokéfaction retardée
US20130026069A1 (en) * 2011-07-29 2013-01-31 Omer Refa Koseoglu Solvent-assisted delayed coking process
WO2013019321A1 (fr) * 2011-07-29 2013-02-07 Saudi Arabian Oil Company Procédé de cokéfaction retardée assisté par solvant
US8894841B2 (en) 2011-07-29 2014-11-25 Saudi Arabian Oil Company Solvent-assisted delayed coking process
US20190284482A1 (en) * 2018-03-13 2019-09-19 Lummus Technology Llc In situ coking of heavy pitch and other feedstocks with high fouling tendency
KR20200123476A (ko) * 2018-03-13 2020-10-29 루머스 테크놀로지 엘엘씨 파울링 경향이 높은 중질 피치 및 다른 공급 원료의 현장 코킹
RU2775970C2 (ru) * 2018-03-13 2022-07-12 ЛАММУС ТЕКНОЛОДЖИ ЭлЭлСи Коксование на месте тяжелого пека и другого сырья с высокой тенденцией к загрязнению
CN114369474A (zh) * 2020-10-15 2022-04-19 山东方宇润滑油有限公司 一种油基针状焦生产装置及生产工艺

Also Published As

Publication number Publication date
JPS6317988A (ja) 1988-01-25
EP0250136B1 (fr) 1992-02-19
ES2030063T3 (es) 1992-10-16
CA1279838C (fr) 1991-02-05
JPH06104834B2 (ja) 1994-12-21
DE3776729D1 (de) 1992-03-26
EP0250136A3 (en) 1989-03-15

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