EP0250136B1 - Delayed coking - Google Patents
Delayed coking Download PDFInfo
- Publication number
- EP0250136B1 EP0250136B1 EP19870305009 EP87305009A EP0250136B1 EP 0250136 B1 EP0250136 B1 EP 0250136B1 EP 19870305009 EP19870305009 EP 19870305009 EP 87305009 A EP87305009 A EP 87305009A EP 0250136 B1 EP0250136 B1 EP 0250136B1
- Authority
- EP
- European Patent Office
- Prior art keywords
- fluid
- coke
- coker
- oil
- steam
- 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.)
- Expired - Lifetime
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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 6.89 x 104 to 1.03 x 105 Nm ⁇ 2 (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.
- U.S. Patent Specification No. 3,956,101 discloses a process for producing high grade needle-shaped cokes which comprises: charging a raw material oil into a coking drum, reforming the charged raw material oil in the coking drum by heating the oil at a temperature of from 300° to 400°C under a pressure of from 2mmHg to 3 atmospheres for from 0.5 to 10 hours, coking the reformed raw material oil by heating the oil in the coking drum at a temperature of from 400°C to 500°C under a pressure higher than atmospheric pressure while blowing a non-oxidizing gas selected from vaporized hydrocarbon oil, hydrogen, nitrogen and steam heated at a temperature higher than that of the reformed raw material oil by at most 300°C into the bottom of the coking drum through the oil until coking of the reformed raw material oil has been substantially completed, thereby simultaneously heating and agitating the reformed raw material oil within the coking drum to secure uniform heating of the reformed raw material oil, removal of excess heat generated in the coking drum and promotion of crystal orientation of
- U.S Patent Specification No. 4,036,736 discloses a process for producing synthetic coking coal which comprises delayed coking a heavy hydrocarbon oil by: heating the oil in a furnace to a coking temperature of from about 380 to about 500°C sufficient to initiate cracking, introducing the heated oil into a coking drum, maintaining the heavy hydrocarbon oil in the coking drum for a time ranging from 30 minutes to about 36 hours at the coking temperatures to effect coking thereof; introducing a diluent gas into the body of the oil in the cooling drum at a flow rate greater than 51/hr kg of oil to maintain the partial vapor pressure of the cracking product vapor over the oil in the coking drum at about 50 to about 600 mm Hg during coking, and recovering a synthetic coking coal having a free swelling index greater than 4 and containing 20 to 40% by weight of volatile matter.
- the diluent gas typically comprises an inert gas such as nitrogen, steam, water or a hydrocarbon gas recovered from the coking process.
- 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 present 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.
- a method for reducing coke formation in a delayed coking process carried out in a coker unit comprising a coker furnace, a coke drum and a coker fractionator, which method comprises: heating heavy oil to coking temperature in the coker furnace, passing the heated oil to the coke drum where coke and overhead vapors are formed, and passing the overhead vapors to the fractionator, which method further comprises introducing into the coke drum a fluid in an amount sufficient to lower the partial pressure of the heavy oil in the coke drum, characterised in that the fluid is heated with heat recovered from the coking process.
- 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.
- 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. Consequently, lower than normal coker furnace outlet temperatures may be used by introducing superheated fluid into the coke drum.
- the superheated fluid is preferably obtained by passing the fluid through the coker furnace.
- 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.
- 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 475°C to 525°C and a pressure of 1.03 x 105 to 5.17 x 105 Nm ⁇ 2 (15 to 75 psig).
- the temperature will range from about 490°C to about 510°C and the pressure will range from 1.38 x 105 to 3.45 x 105 Nm ⁇ 2 (20 to 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 415°C to 470°C and a pressure from 6.89 x 104 to 2.41 x 105 Nm ⁇ 2 (10 psig to 35 psig).
- the temperature and pressure preferrably range from 435°C to 455 °C and 1.03 x 105 to 1.72 x 105 Nm ⁇ 2 (15 psig to 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 15°C (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 415°C to 535°C and preferably from 480°C to 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 0.57 Kg mols/m3 (0.2 lbmols/bbl) of fresh feed to 14.27 Kg mols/m3 (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)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Coke Industry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
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 EP0250136A2 (en) | 1987-12-23 |
EP0250136A3 EP0250136A3 (en) | 1989-03-15 |
EP0250136B1 true EP0250136B1 (en) | 1992-02-19 |
Family
ID=25358514
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP19870305009 Expired - Lifetime EP0250136B1 (en) | 1986-06-09 | 1987-06-05 | Delayed coking |
Country Status (5)
Country | Link |
---|---|
EP (1) | EP0250136B1 (ja) |
JP (1) | JPH06104834B2 (ja) |
CA (1) | CA1279838C (ja) |
DE (1) | DE3776729D1 (ja) |
ES (1) | ES2030063T3 (ja) |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US9139781B2 (en) | 2009-07-10 | 2015-09-22 | Exxonmobil Research And Engineering Company | Delayed coking process |
CN111989386A (zh) * | 2018-03-13 | 2020-11-24 | 鲁姆斯科技有限责任公司 | 重质沥青及具有高结垢趋势的其他原料的原位焦化 |
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 |
Families Citing this family (11)
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 |
US5645712A (en) * | 1996-03-20 | 1997-07-08 | Conoco Inc. | Method for increasing yield of liquid products in a delayed coking process |
US8709233B2 (en) | 2006-08-31 | 2014-04-29 | Exxonmobil Chemical Patents Inc. | Disposition of steam cracked tar |
WO2008027139A1 (en) * | 2006-08-31 | 2008-03-06 | Exxonmobil Chemical Patents Inc. | Method for upgrading steam cracker tar using pox /cocker |
US8083930B2 (en) | 2006-08-31 | 2011-12-27 | Exxonmobil Chemical Patents Inc. | VPS tar separation |
US7560020B2 (en) | 2006-10-30 | 2009-07-14 | Exxonmobil Chemical Patents Inc. | Deasphalting tar using stripping tower |
CN102007201A (zh) * | 2008-02-14 | 2011-04-06 | 罗杰·G·埃特 | 为改善期望产品的收率和性质而向焦化工艺引入添加剂的系统和方法 |
US8496805B2 (en) * | 2009-07-10 | 2013-07-30 | Exxonmobil Research And Engineering Company | Delayed coking process |
CN103814112B (zh) * | 2011-07-29 | 2016-08-17 | 沙特阿拉伯石油公司 | 溶剂辅助的延迟焦化方法 |
CN103814110A (zh) * | 2012-08-29 | 2014-05-21 | 普诺米泰克股份有限公司 | 残油的延迟焦化方法 |
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 |
Family Cites Families (5)
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 |
-
1987
- 1987-06-02 CA CA000538635A patent/CA1279838C/en not_active Expired - Fee Related
- 1987-06-05 EP EP19870305009 patent/EP0250136B1/en not_active Expired - Lifetime
- 1987-06-05 DE DE8787305009T patent/DE3776729D1/de not_active Expired - Fee Related
- 1987-06-05 ES ES87305009T patent/ES2030063T3/es not_active Expired - Lifetime
- 1987-06-08 JP JP62141641A patent/JPH06104834B2/ja not_active Expired - Lifetime
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US9139781B2 (en) | 2009-07-10 | 2015-09-22 | Exxonmobil Research And Engineering Company | Delayed coking process |
CN111989386A (zh) * | 2018-03-13 | 2020-11-24 | 鲁姆斯科技有限责任公司 | 重质沥青及具有高结垢趋势的其他原料的原位焦化 |
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 |
Also Published As
Publication number | Publication date |
---|---|
ES2030063T3 (es) | 1992-10-16 |
DE3776729D1 (de) | 1992-03-26 |
EP0250136A3 (en) | 1989-03-15 |
JPH06104834B2 (ja) | 1994-12-21 |
EP0250136A2 (en) | 1987-12-23 |
JPS6317988A (ja) | 1988-01-25 |
CA1279838C (en) | 1991-02-05 |
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