US20090139899A1 - Process of Modification of a Feedstock in a Delayed Coking Unit - Google Patents

Process of Modification of a Feedstock in a Delayed Coking Unit Download PDF

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Publication number
US20090139899A1
US20090139899A1 US11/990,184 US99018407A US2009139899A1 US 20090139899 A1 US20090139899 A1 US 20090139899A1 US 99018407 A US99018407 A US 99018407A US 2009139899 A1 US2009139899 A1 US 2009139899A1
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US
United States
Prior art keywords
coke
feedstock
gas oil
delayed coking
fractionation tower
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.)
Abandoned
Application number
US11/990,184
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English (en)
Inventor
Gloria Maria Gomes Soares
Natalie Jorge Goncalves
Aline Voigt Nadolni
Francisco Carlos Da Costa Barros
Sergio Cunha De Lucena
Sergio Nunes Da Costa
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.)
Petroleo Brasileiro SA Petrobras
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Petroleo Brasileiro SA Petrobras
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 Petroleo Brasileiro SA Petrobras filed Critical Petroleo Brasileiro SA Petrobras
Assigned to PETROLEO BRASILEIRO S.A.-PETROBRAS reassignment PETROLEO BRASILEIRO S.A.-PETROBRAS ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: NADOLNI, ALINE VOIGT, DA COSTA BARROS, FRANCISCO CARLOS, DA COSTA, SERGIO NUNES, DE LUCENA, SERGIO CUNHA, GONCALVES, NATALIE JORGE, SOARES, GLORIA MARIA GOMES
Publication of US20090139899A1 publication Critical patent/US20090139899A1/en
Abandoned legal-status Critical Current

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    • 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)
    • 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

Definitions

  • the field of application of the present invention is delayed coking processes. Particularly in delayed coking processes wherein the yield of diesel oil is maximised whereas the yield of heavy gas oil from coke is minimised through modifications to the feedstock of a Delayed Coking Unit.
  • LPG liquefied petroleum gas
  • the new feedstock generally a vacuum residuum
  • the natural recycle is employed to adjust the quality of heavy gas oil from coke to be sent to any Fluid Catalytic Cracking (FCC) Unit.
  • FCC Fluid Catalytic Cracking
  • the combined feedstock is sent to a furnace wherein it must dwell for a very short time, of the order of a few minutes, such that the thermal cracking reactions can be initiated and the formation of coke in the furnace tubes be minimised.
  • the cracked feedstock is fed to the coke drum wherein the thermal cracking and coking or carbonisation reactions are completed. These reactions generate hydrocarbons lighter than those in the combined feedstock and coke.
  • the reactions which take place in a coke drum are endothermic and the temperature of the effluents from the drum lie within a band of values from 430° C. to 455° C.
  • the coke formed accumulates in the drum until it requires to be removed following stages of steam purging and cooling with water. With the objective of removing the accumulated coke in a coke drum the effluent from the coke drum is diverted to another empty coke drum wherein the accumulation phase is initiated. Removal of the coke is carried out by means of high-pressure-water cutting devices.
  • U.S. Pat. No. 4,213,846 discloses a delayed coking process for the formation of premium coke wherein the recycle is hydrotreated.
  • U.S. Pat. No. 4,177,133 describes a delayed coking process for the formation of premium coke wherein the new feedstock having passed through a preheating stage is subjected to flash distillation to remove non-crystalline substances.
  • U.S. Pat. No. 4,455,219 and U.S. Pat. No. 4,518,487 disclose a delayed coking process wherein part or all of the heavy hydrocarbon product commonly used as recycle is replaced by a lighter hydrocarbon, which same is combined with the new feedstock of the unit.
  • U.S. Pat. No. 5,711,870 discloses a process of delayed coking wherein the fresh feedstock is mixed with water and, optionally, with a hydrogen donor such as methane or gas oil derived from the recycle in order to optimise the yield of liquid products and reduce the yields of coke and gas.
  • a hydrogen donor such as methane or gas oil derived from the recycle
  • the diesel oil from a refinery comprises diverse streams, among them light gas oil from coke produced in a Delayed Coking Unit.
  • diesel oil from coke As the present invention described below refers to diesel oil produced from light gas oil from coke, hereinafter such diesel oil will be referred to as diesel oil from coke.
  • the process of modification of a feedstock in a Delayed Coking Unit considers a solution maximising the yield of diesel oil from coke and minimising the yield of heavy gas oil from coke by means of modifications to the feedstock of a Delayed Coking Unit.
  • the feedstock consists of: the bottom product from the vacuum distillation tower, known in the prior art as vacuum residuum, and the heavy gas oil from coke obtained in the fractionation tower and recycled in order to comprise the aforesaid combined feedstock.
  • the percentage by volume of heavy gas oil from coke in the new feedstock lies within a band of values from 16% to 50%. Preferentially within a band of values comprised between 20% and 40%.
  • the feedstock consists of: the bottom residuum proceeding from the atmospheric distillation tower, known in the prior art as atmospheric residuum, and the heavy gas oil from coke obtained from the fractionation tower and recycled to comprise the aforesaid feedstock of the unit.
  • FIG. 1 shows schematically a delayed coking process, according to the prior art.
  • FIG. 2 shows schematically a process of modification of a feedstock in a Delayed Coking Unit according to a first embodiment of the present invention.
  • FIG. 3 shows schematically a process of modification of a feedstock in a Delayed Coking Unit according to a second embodiment of the present invention.
  • FIG. 1 shows schematically a delayed coking process according to the prior art.
  • a fresh feedstock ( 1 ) is fed to a fractionation tower ( 2 ) whence diverse derivatives are removed such as, for example, fuel gas and LPG ( 3 ), light naphtha ( 4 ), heavy naphtha ( 5 ), light gas oil ( 6 ), medium gas oil ( 7 ) and heavy gas oil from coke ( 8 ).
  • diverse derivatives such as, for example, fuel gas and LPG ( 3 ), light naphtha ( 4 ), heavy naphtha ( 5 ), light gas oil ( 6 ), medium gas oil ( 7 ) and heavy gas oil from coke ( 8 ).
  • the bottom product ( 9 ) of the fractionation tower ( 2 ) is fed to a furnace ( 10 ) such that the thermal cracking reactions may be initiated.
  • the effluent from the furnace ( 11 ) is subsequently sent to a coke drum ( 12 ) wherein the thermal cracking and coking or carbonisation reactions are completed, generating coke and an effluent from the coke drum ( 13 ) comprising light hydrocarbons.
  • the effluent from the coke drum ( 13 ) is subsequently sent to the fractionation tower ( 2 ).
  • FIG. 2 shows schematically a process of modification of a feedstock in a Delayed Coking Unit according to the present invention.
  • a fresh feedstock ( 1 ) is fed to a fractionation tower ( 2 ) whence several derivatives are removed such as, for example, fuel gas and LPG ( 3 ), light naphtha ( 4 ), heavy naphtha ( 5 ), light gas oil ( 6 ), medium gas oil ( 7 ) and heavy gas oil from coke ( 8 ).
  • fuel gas and LPG 3
  • light naphtha 4
  • heavy naphtha 5
  • light gas oil 6
  • medium gas oil 7
  • heavy gas oil from coke 8 .
  • a fraction ( 8 ′) of heavy gas oil from coke ( 8 ) is added to the bottom product ( 9 ) from the fractionation tower ( 2 ).
  • the percentage by volume of the fraction ( 8 ′) of heavy gas oil from coke ( 8 ) in relation to the fresh feedstock ( 1 ) lies within a band of values from 16% to 50%.
  • Preferentially the percentage by volume of the fraction ( 8 ′) of heavy gas oil from coke ( 8 ) in relation to the fresh feedstock ( 1 ) lies within a band of values from 20% to 40%.
  • the aforesaid fraction ( 8 ′) of heavy gas oil from coke ( 8 ) may be added to the bottom product ( 9 ) by means of a line external to the fractionation tower ( 2 ), according to the embodiment shown in FIG. 2 .
  • the aforesaid fraction ( 8 ′) of the heavy gas oil from coke ( 8 ) may be added to the bottom product ( 9 ) within aforesaid fractionation tower ( 2 ).
  • the feedstock thus combined ( 9 ′) is subsequently sent to the furnace ( 10 ) in order that the thermal cracking reactions may be initiated.
  • the effluent from the furnace ( 11 ) is subsequently sent to a coke drum ( 12 ) wherein the thermal cracking and coking or carbonisation reactions are completed, generating coke and an effluent from the coke drum ( 13 ) comprising light hydrocarbons.
  • the effluent from the coke drum ( 13 ) is subsequently sent to the fractionation tower ( 2 ).
  • FIG. 3 shows schematically a process of modification of a feedstock in a Delayed Coking Unit according to a second embodiment of the present invention.
  • Petroleum ( 14 ) is fed to an atmospheric distillation tower ( 15 ) whence diverse derivatives are removed such as, for example, fuel gas ( 16 ), naphtha ( 17 ) and others not shown in this figure.
  • the feedstock of the Delayed Coking Unit is the bottom residuum ( 18 ) from the atmospheric distillation tower ( 15 ), known in the prior art as atmospheric residuum, and a fraction ( 8 ′) of heavy gas oil from coke ( 8 ) proceeding from the fractionation tower ( 2 ) is added to the bottom product ( 9 ) of the fractionation tower ( 2 ).
  • a vacuum residuum was processed in a pilot delayed coking unit without heavy gas oil from coke recycle.
  • the temperature of the furnace was 0.500° C. and the pressure at the top of the coke drum was 2 kgf/cm 2 g. Volume yields of 51.3% for diesel oil from coke and of 20.2% for heavy gas oil from coke were obtained. The mass yield of coke was 24.5%.
  • a vacuum residuum was processed in an industrial delayed coking unit having a furnace temperature of 500° C. and pressure at the top of the coke drum of 2 kgf/cm 2 g and a heavy gas oil from coke recycle rate of 8%. Volume yields of 54.9% for diesel oil from coke and of 14.6% for heavy gas oil from coke were obtained. The mass yield of coke was 25%.
  • a vacuum residuum was processed in a pilot delayed coking unit having a furnace temperature of 500° C., pressure at the top of the coke drum of 2 kgf/cm 2 g and total recycle of heavy gas oil from coke.
  • the volume yield was 68.2% for diesel oil from coke.
  • the mass yield of coke was 26%.
  • An atmospheric residuum was processed in a pilot delayed coking unit, without heavy gas oil from coke recycle, having a furnace temperature of 500° C. and pressure at the top of the coke drum of 2 kgf/cm 2 g. Volume yields of 53.5% for diesel oil from coke and of 27.7% for heavy gas oil from coke were obtained. The mass yield of coke was 13.5%.
  • An atmospheric residuum was processed in an industrial delayed coking unit having a furnace temperature of 500° C., pressure at the top of the coke drum of 2 kgf/cm 2 g and a heavy gas oil from coke recycle rate of 25%. Volume yields of 62.9% for diesel oil from coke and of 14.0% for heavy gas oil from coke were obtained. The mass yield of coke was 15.2%.
  • An atmospheric residuum was processed in a pilot delayed coking unit having a furnace temperature of 500° C., pressure at the top of the coke drum of 2 kgf/cm 2 g and total recycle of heavy gas oil from coke.
  • the volume yield was 72.6% for diesel oil from coke.
  • the mass yield of coke was 17%.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Materials Engineering (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Coke Industry (AREA)
US11/990,184 2006-07-28 2007-02-01 Process of Modification of a Feedstock in a Delayed Coking Unit Abandoned US20090139899A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
BRPI0603016-5 2006-07-28
BRPI0603016A BRPI0603016B1 (pt) 2006-07-28 2006-07-28 processo de modificação de uma carga em uma unidade de coqueamento retardado
PCT/GB2007/000339 WO2008012484A1 (en) 2006-07-28 2007-02-01 Process of modification of a feedstock in a delayed coking unit

Publications (1)

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US20090139899A1 true US20090139899A1 (en) 2009-06-04

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US11/990,184 Abandoned US20090139899A1 (en) 2006-07-28 2007-02-01 Process of Modification of a Feedstock in a Delayed Coking Unit

Country Status (9)

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US (1) US20090139899A1 (es)
EP (1) EP2049618B1 (es)
JP (1) JP2009544789A (es)
CN (1) CN101346453A (es)
AR (1) AR059271A1 (es)
BR (1) BRPI0603016B1 (es)
ES (1) ES2626614T3 (es)
PT (1) PT2049618T (es)
WO (1) WO2008012484A1 (es)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102732285A (zh) * 2011-04-12 2012-10-17 中国石油化工股份有限公司 一种减缓焦炭塔顶油气管线结焦的方法
US9732278B2 (en) 2013-12-24 2017-08-15 Jx Nippon Oil & Energy Corporation Petroleum coke and production method for same
CN112251254A (zh) * 2020-11-18 2021-01-22 武汉轻工大学 一种延迟焦化焦炭塔的冷焦系统

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BRPI0803545A2 (pt) * 2008-07-31 2010-06-15 Petroleo Brasileiro Sa processo de produção de bio-óleo por co-processamento de biomassa em unidade de coqueamento retardado
ES2366252A1 (es) * 2008-07-31 2011-10-18 Petróleo Brasileiro S.A. Petrobras Procedimiento para la producción de bio-aceite mediante el procesamiento conjunto de biomasa en una unidad de coquización retardada.
CN105975685A (zh) * 2016-05-03 2016-09-28 华东理工大学 一种用于渣油延迟焦化过程的建模和优化方法

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3563884A (en) * 1968-07-15 1971-02-16 Lummus Co Delayed coking of coal tar pitches
US4177133A (en) * 1974-09-25 1979-12-04 Maruzen Petrochem Co Ltd Process for producing high-crystalline petroleum coke
US4213846A (en) * 1978-07-17 1980-07-22 Conoco, Inc. Delayed coking process with hydrotreated recycle
US4455219A (en) * 1982-03-01 1984-06-19 Conoco Inc. Method of reducing coke yield
US4518487A (en) * 1983-08-01 1985-05-21 Conoco Inc. Process for improving product yields from delayed coking
US4661241A (en) * 1985-04-01 1987-04-28 Mobil Oil Corporation Delayed coking process
US5711870A (en) * 1996-05-28 1998-01-27 Texaco Inc. Delayed coking process with water and hydrogen donors

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH0539489A (ja) * 1991-07-02 1993-02-19 Conoco Inc 等方性コークスの製造方法
EP1751252A1 (en) * 2004-05-14 2007-02-14 ExxonMobil Research and Engineering Company Delayed coking process for producing free-flowing coke using low molecular weight aromatic additives
CN1954050A (zh) * 2004-05-14 2007-04-25 埃克森美孚研究工程公司 在延迟焦化中从减压渣油的深拔馏分中生产基本上自由流动的焦炭

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3563884A (en) * 1968-07-15 1971-02-16 Lummus Co Delayed coking of coal tar pitches
US4177133A (en) * 1974-09-25 1979-12-04 Maruzen Petrochem Co Ltd Process for producing high-crystalline petroleum coke
US4213846A (en) * 1978-07-17 1980-07-22 Conoco, Inc. Delayed coking process with hydrotreated recycle
US4455219A (en) * 1982-03-01 1984-06-19 Conoco Inc. Method of reducing coke yield
US4518487A (en) * 1983-08-01 1985-05-21 Conoco Inc. Process for improving product yields from delayed coking
US4661241A (en) * 1985-04-01 1987-04-28 Mobil Oil Corporation Delayed coking process
US5711870A (en) * 1996-05-28 1998-01-27 Texaco Inc. Delayed coking process with water and hydrogen donors

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102732285A (zh) * 2011-04-12 2012-10-17 中国石油化工股份有限公司 一种减缓焦炭塔顶油气管线结焦的方法
US9732278B2 (en) 2013-12-24 2017-08-15 Jx Nippon Oil & Energy Corporation Petroleum coke and production method for same
CN112251254A (zh) * 2020-11-18 2021-01-22 武汉轻工大学 一种延迟焦化焦炭塔的冷焦系统

Also Published As

Publication number Publication date
WO2008012484A1 (en) 2008-01-31
JP2009544789A (ja) 2009-12-17
BRPI0603016A (pt) 2008-03-18
EP2049618B1 (en) 2017-05-10
ES2626614T3 (es) 2017-07-25
EP2049618A1 (en) 2009-04-22
CN101346453A (zh) 2009-01-14
AR059271A1 (es) 2008-03-19
BRPI0603016B1 (pt) 2015-10-27
PT2049618T (pt) 2017-06-07

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Owner name: PETROLEO BRASILEIRO S.A.-PETROBRAS, BRAZIL

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:SOARES, GLORIA MARIA GOMES;GONCALVES, NATALIE JORGE;NADOLNI, ALINE VOIGT;AND OTHERS;REEL/FRAME:021455/0692;SIGNING DATES FROM 20080620 TO 20080720

STCB Information on status: application discontinuation

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