EP0204410A2 - Méthode pour fournir de la chaleur à des courants processionnels à haute température - Google Patents

Méthode pour fournir de la chaleur à des courants processionnels à haute température Download PDF

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Publication number
EP0204410A2
EP0204410A2 EP86302917A EP86302917A EP0204410A2 EP 0204410 A2 EP0204410 A2 EP 0204410A2 EP 86302917 A EP86302917 A EP 86302917A EP 86302917 A EP86302917 A EP 86302917A EP 0204410 A2 EP0204410 A2 EP 0204410A2
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EP
European Patent Office
Prior art keywords
oxygen
further characterized
containing gas
petroleum
coking
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.)
Withdrawn
Application number
EP86302917A
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German (de)
English (en)
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EP0204410A3 (fr
Inventor
Frederick John Krambeck
Samuel Allen Tabak
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.)
ExxonMobil Oil Corp
Original Assignee
Mobil Oil Corp
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Filing date
Publication date
Application filed by Mobil Oil Corp filed Critical Mobil Oil Corp
Publication of EP0204410A2 publication Critical patent/EP0204410A2/fr
Publication of EP0204410A3 publication Critical patent/EP0204410A3/fr
Withdrawn legal-status Critical Current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
    • 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
    • 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
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/20—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert heated gases or vapours
    • C10G11/22—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert heated gases or vapours produced by partial combustion of the material to be cracked
    • 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
    • C10G9/007—Visbreaking
    • 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
    • C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
    • C10G9/36—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
    • C10G9/38—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours produced by partial combustion of the material to be cracked or by combustion of another hydrocarbon

Definitions

  • This invention relates to a method for supplying heat to high temperature process streams and more particularly, to a method for supplying heat to petroleum feedstocks which are to be processed in thermal conversion processes such as visbreaking, thermal cracking and coking.
  • One method for inhibiting the degree of coking is to include an inert gas, generally steam, in the feedstock as it is passed through the tubes so as to increase the velocity of the oil in the tube and reduce its residence time, thereby reducing the extent of cracking which occurs in the tubes of the fumace.
  • the steam helps to strip volatile material from the coke in the coking drum.
  • the furnace tubes may be subjected to an undesirable degree of coking because of the long residence times which are encountered in these units.
  • the seat of the problem has generally been in the furnace where the objective has been to supply the required heat to the process stream without, however, employing conditions which are conducive to the production of quantities of coke and other thermal decomposition products.
  • both moving bed and fluidized bed units have been proposed for reduced crude coking. Because units of this kind generally operate at lower pressures and higher temperatures than delayed cokers, more of the feedstock is vaporized and the higher temperatures also resutt'in higher octane gasoline and more olefin gasoline than those from delayed cokers. However, despite the development of these higher temperature coking processes, most commercial coking operations currently employ the delayed coking process.
  • U.S. Patent No. 4,302,324 discloses a method for increasing the temperature of the coker feedstock by adding hot coke to the feed which is charged to the coking drum. In this way, the furnace is permitted to operate at a relatively lower temperature, with reduced fouling in the furnace tubes.
  • U.S. Patent No. 2,775,549 discloses a coking operation in which additional heat may be supplied by introducing a superheated steam or relatively light hydrocarbon or steam directly into the coke still.
  • 3,956,101 describes a method for producing coke by a two-step operation in which the feedstock is first subjected to reforming and then to coking in a coking drum with a superheated nonoxidizing gas being injected into the bottom of the drum in order to bring the oil to the desired coking temperature.
  • Suitable nonoxidizing gases include the vapors of light hydrocarbon oils or gases such as hydrogen, nitrogen and steam, all of which are required to be nonoxidizing at the temperatures used in the process.
  • process streams particularly refinery process streams which are to be brought to high temperatures
  • process streams may be effectively heated by a process of direct, internal combustion, which reduces the need for supplying heat in preheating furnaces and may, in favorable cases, totally eliminate the requirement for such furnaces.
  • the present invention provides a method for processing petroleum at an elevated temperature in which the petroleum is heated, characterized by heating the petroleum by injecting an oxygen-containing gas into it to cause a partial combustion of the petroleum.
  • the heat content of a combustible process stream is increased by injecting an oxygen-containing gas into the stream so that combustion of a part of the process stream occurs directly in the stream.
  • the heat from the exothermic combustion reaction is transferred directly to the process stream so that a rise in temperature of the stream takes place and this enables the requirement for externally supplied heat to be reduced.
  • the amount of heat which needs to be supplied in the preheater furnace is reduced and, in favorable cases, it may be possible to eliminate the preheating furnace entirely. Because the amount of heat which is to be supplied by the furnace is decreased, the furnace may be operated under lower severity conditions, i.e. at lower temperatures, or with a reduced furnace residence time, so that the extent of thermal decomposition which takes place in the furnace is reduced and internal fouling of the furnace tubes is reduced or eliminated.
  • the process stream will generally be selected from petroleum feedstock such as gas oil, vacuum reduced crudes, atmospheric residua, heavy cycle oils, slurry oils, FCC tower bottoms, thermal cracking residua and products from synthetic liquid fuel production, for example, heavy fractions from Fi- scher-Tropsch syntheses.
  • the process may be applied to the heating of any combustible process stream whose temperature is to be raised for a subsequent processing step but obviously, it will not be used under circumstances where there might be a hazard of uncontrolled combustion or explosion.
  • the process is particularly applicable for heating petroleum refinery streams which are to be heated to temperatures above 400°C (750°F) and more particularly, for such streams which are to be heated to temperatures above 450°C (840°F), e.g. to temperatures of 500°C (930°F), 525°C (980°F) or even higher.
  • thermal conversion processes such as coking, especially delayed coking, thermal cracking and visbreaking.
  • thermal conversion is meant a process in which a hydrocarbon feedstock is converted at least in part to products of lower boiling range solely by the influence of elevated temperature, i.e. is noncatalytic in nature.
  • the method may also be used to heat process streams which are going to nonhydrogena- tive catalytic processes such as fluid catalytic cracking (FCC).
  • FCC fluid catalytic cracking
  • the process stream may be brought to a higher temperature than the furnace temperature by the injection of the oxygen-containing gas.
  • FIG. 1 An illustrative process scheme for heating a heavy oil coker feedstock is shown in Figure 1 of the accompanying drawings.
  • the heavy oil feed, together with any recycle (optional) enters through conduit 10 together with any steam which is desired for stripping purposes.
  • the feed is heated in preheater furnace 11 and then passes to coking drum 12 in which coking takes place.
  • Oxygen is injected at the bottom of drum 12 through injection nozzle 13 at a rate which is proportioned in accordance with the charge rate of the feedstock to the coker drum.
  • combustion occurs to the extent permitted by the quantity of oxygen injected and the heat of the combustion is released to the feed as it passes up the coker drum, with a resulting increase in temperature.
  • coking may be carried out at the requisite coking temperature, typically at 450°C (840°F) or higher, although temperatures within the range of 450 to 475°C (840 to 900°F) will normally be used.
  • the discharge temperature of the preheater furnace may be maintained at a lower value, typically 400 to 425°C (750 to 800°F). The use of lower temperatures in the furnace reduces the degree of furnace fouling and it is therefore possible to operate over longer periods of time without the necessity of cleaning the inside of the furnace tubes.
  • FIG. 2 A similar arrangement is shown in Figure 2 in which a heavy hydrocarbon feedstock is preheated in a furnace together with any recycle and added steam for stripping. In this case, oxygen is injected into the feed in a combustion vessel 15 between furnace 11 and coking drum 12. Partial combustion of the feedstock takes place as in the previous arrangement, with a similar resulting rise in temperature. It will also permit the coker to be operated at higher temperatures so as to increase liquid yield. As shown in Tables 1 and 2 below, increasing the temperature at which coking or visbreaking is carried out, increases the liquid yields.
  • the visbreaker feed usually a vacuum residuum or possibly a full range heavy crude, topped heavy crude or atmospheric residuum, enters through conduit 20 and oxygen is injected through a suitable nozzle at 21.
  • a requisite residence time is provided by the length of conduit 22 before a gas oil quench is introduced at 23, after which the visbreaking products pass to flash drum 24.
  • the gaseous products pass to fractionator 25 to give the lighter products such as gas, gasoline and light gas oil; the liquid fraction from flashdrum 24 passes to vacuum tower 26 to separate the heavy gas oil fraction (HGO) from the visbroken residuum.
  • HGO heavy gas oil fraction
  • the hydrocarbons should be brought to a temperature which is at least as high as the flashpoint of at least one of the hydrocarbons in the stream.
  • the hydrocarbons should be brought to a temperature which is at least as high as the flashpoint of at least one of the hydrocarbons in the stream.
  • a promoter may be added to the oil or a chamber holding a combustion catalyst may be inserted after the preheat furnace or the preheat exchanger.
  • the use of promotors and combustion catalysts is especially desirable in cases where the presence of the oxygen-containing gas might be deleterious to the subsequent processing step.
  • Oxygen is the preferred oxygen-containing gas for use in this method since it readily initiates spontaneous ignition. Air is somewhat less preferred since the nitrogen which is present in it adds to the amount of gas which requires to be accommodated in the downstream process unit but it is, of course, considerably cheaper. As a compromise, oxygen-enriched air may be used and in such cases, an oxygen concentration of at least 75% by volume is normally preferred.
  • the amount of the oxygen-containing gas which is to be injected will depend upon a number of factors including the temperature rise which is to be achieved, the heat of combustion of the particular process stream, the composition of the oxygen-containing gas and the amount of any steam or other inert material which is present. The actual amount necessary may be determined by calculation from the known values of the appropriate factors or by experiment. Generally, the amount of oxygen necessary for thermal processing of petroleum residua will be from 4 to 70 Kg oxygen per 1000 Kg of oil; if steam is present as a stripper, an additional 2 to 40 Kg of oxygen should be used for every 1000 Kg of steam.
  • the oxidant gas and the combustion products act as a stripper, maintaining oil velocities in the conduits and in the rest of the processing equipment. Because of this, the amount of injected steam may be reduced or, in favorable cases, eliminated. For this reason, it may be preferred to operate with injection of the oxygen upstream of the preheat furnace or the preheat exchanger so that a limited degree of combustion occurs as the oil passes through the heater; the gaseous combustion products reduce the space velocity of the oil in the heater with a consequent reduction in the likelihood of fouling.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Materials Engineering (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Coke Industry (AREA)
EP86302917A 1985-05-28 1986-04-18 Méthode pour fournir de la chaleur à des courants processionnels à haute température Withdrawn EP0204410A3 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US73832485A 1985-05-28 1985-05-28
US738324 1985-05-28

Publications (2)

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EP0204410A2 true EP0204410A2 (fr) 1986-12-10
EP0204410A3 EP0204410A3 (fr) 1988-07-20

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EP86302917A Withdrawn EP0204410A3 (fr) 1985-05-28 1986-04-18 Méthode pour fournir de la chaleur à des courants processionnels à haute température

Country Status (4)

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EP (1) EP0204410A3 (fr)
JP (1) JPS61276893A (fr)
AU (1) AU5599186A (fr)
ZA (1) ZA862711B (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5041207A (en) * 1986-12-04 1991-08-20 Amoco Corporation Oxygen addition to a coking zone and sludge addition with oxygen addition
FR2741889A1 (fr) * 1995-12-04 1997-06-06 Total Raffinage Distribution Perfectionnements apportes aux procedes et aux dispositifs de viscoreduction de charges lourdes d'hydrocarbures

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP4865461B2 (ja) * 2006-09-11 2012-02-01 Ｊｘ日鉱日石エネルギー株式会社 ディレイドコーカーの加熱炉の運転方法

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB361714A (en) * 1930-02-06 1931-11-26 Georg Zotos Process of and apparatus for the treatment of fuel by destructive hydrogenation and for like purposes
US2630378A (en) * 1949-07-23 1953-03-03 Texaco Development Corp Generation of synthesis gas
FR1026393A (fr) * 1950-07-21 1953-04-27 Procédé pour le cracking de charges liquides
US2775549A (en) * 1954-01-25 1956-12-25 Great Lakes Carbon Corp Production of coke from petroleum hydrocarbons
US2813824A (en) * 1955-03-09 1957-11-19 Consolidation Coal Co Process for coking hydrocarbonaceous liquids
GB912445A (en) * 1960-03-14 1962-12-05 Shell Int Research A process for the production of acetylene-containing gas mixtures
US4166830A (en) * 1978-06-21 1979-09-04 Arand John K Diacritic cracking of hydrocarbon feeds for selective production of ethylene and synthesis gas
US4240898A (en) * 1978-12-12 1980-12-23 Union Carbide Corporation Process for producing high quality pitch

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB361714A (en) * 1930-02-06 1931-11-26 Georg Zotos Process of and apparatus for the treatment of fuel by destructive hydrogenation and for like purposes
US2630378A (en) * 1949-07-23 1953-03-03 Texaco Development Corp Generation of synthesis gas
FR1026393A (fr) * 1950-07-21 1953-04-27 Procédé pour le cracking de charges liquides
US2775549A (en) * 1954-01-25 1956-12-25 Great Lakes Carbon Corp Production of coke from petroleum hydrocarbons
US2813824A (en) * 1955-03-09 1957-11-19 Consolidation Coal Co Process for coking hydrocarbonaceous liquids
GB912445A (en) * 1960-03-14 1962-12-05 Shell Int Research A process for the production of acetylene-containing gas mixtures
US4166830A (en) * 1978-06-21 1979-09-04 Arand John K Diacritic cracking of hydrocarbon feeds for selective production of ethylene and synthesis gas
US4240898A (en) * 1978-12-12 1980-12-23 Union Carbide Corporation Process for producing high quality pitch

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5041207A (en) * 1986-12-04 1991-08-20 Amoco Corporation Oxygen addition to a coking zone and sludge addition with oxygen addition
FR2741889A1 (fr) * 1995-12-04 1997-06-06 Total Raffinage Distribution Perfectionnements apportes aux procedes et aux dispositifs de viscoreduction de charges lourdes d'hydrocarbures
EP0778331A1 (fr) * 1995-12-04 1997-06-11 Total Raffinage Distribution S.A. Procédés et dispositifs de viscoréduction de charges lourdes d'hydrocarbures
US5925236A (en) * 1995-12-04 1999-07-20 Total Rafinage Distribution S.A. Processes for visbreaking heavy hydrocarbon feedstocks

Also Published As

Publication number Publication date
AU5599186A (en) 1986-12-04
ZA862711B (en) 1987-11-25
EP0204410A3 (fr) 1988-07-20
JPS61276893A (ja) 1986-12-06

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