EP0127519B1 - Verfahren zur Dampfspaltung von Kohlenwasserstoffen - Google Patents

Verfahren zur Dampfspaltung von Kohlenwasserstoffen Download PDF

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Publication number
EP0127519B1
EP0127519B1 EP84400992A EP84400992A EP0127519B1 EP 0127519 B1 EP0127519 B1 EP 0127519B1 EP 84400992 A EP84400992 A EP 84400992A EP 84400992 A EP84400992 A EP 84400992A EP 0127519 B1 EP0127519 B1 EP 0127519B1
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EP
European Patent Office
Prior art keywords
combustion
zone
charge
steam
combustion gas
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
Application number
EP84400992A
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English (en)
French (fr)
Other versions
EP0127519A1 (de
Inventor
Philippe Bernard
Francois Prudhon
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.)
Rhodia Chimie SAS
Original Assignee
Rhone Poulenc Chimie SA
Rhone Poulenc Chimie de Base SA
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Application filed by Rhone Poulenc Chimie SA, Rhone Poulenc Chimie de Base SA filed Critical Rhone Poulenc Chimie SA
Priority to AT84400992T priority Critical patent/ATE25263T1/de
Publication of EP0127519A1 publication Critical patent/EP0127519A1/de
Application granted granted Critical
Publication of EP0127519B1 publication Critical patent/EP0127519B1/de
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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
    • C10G9/34—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

  • the present invention relates to a process for steam cracking of hydrocarbons, optionally in the presence of hydrogen.
  • steam cracking of hydrocarbons, or cracking in the presence of water vapor was used in the UNITED STATES between 1930 and 1940 for the production of ethylene and aromatic hydrocarbons.
  • the use of hydrogen has two advantages: the conversion of heavy products into light products is improved and the formation of deposits is reduced.
  • the reactor has the shape of a convergent-divergent nozzle.
  • the fundamental condition for any cracking process with olefin production is the appropriate setting of the residence time / temperature ratio, which is possible in a tubular reactor. As the recent trend is towards very short residence times, it will be more difficult to create this fundamental condition and the development of new technologies will prove to be essential ”.
  • GB-A-1 174870 has proposed a device for cracking hydrocarbons, leading to the manufacture of ethylene and acetylene, by treatment by means of a vortex gas flow, but the quantities of ethylene and acetylene obtained remain low.
  • the combustion gas is formed in situ and contains water vapor.
  • it serves to provide the mechanical energy necessary to produce, in situ, the transfer surface as well as the thermal energy necessary for cracking; heat transfer is therefore carried out without the inconvenience of a tubular exchange surface and the combustion gas and the charge are mixed intensively.
  • gaseous reagents are introduced, so that the resulting gaseous phase has the form of a symmetrical helical flow, said reagents reacting in this zone, so as to produce a gas containing superheated water vapor which is evacuated in the form of a well-vortex flow in an isorepartition zone 2 into which the charge of hydrocarbon to be cracked is introduced, at the level of the zone in relative depression generated by the well-vortex flow, the momentum of the combustion gas containing the superheated steam being sufficient relative to that of the liquid charge to cause said liquid charge to rupture, to be sprayed and to take charge of each drop formed by an associated gas volume element, the amount of heat provided the combustion gas being sufficient to allow the vaporization of this charge, overheating and cracking at the desired temperature.
  • the momentum of the volume elements of the gas phase from zone 1 is at least 100 times and preferably between 1000 and 10000 times that of the associated volume elements of the liquid phase.
  • the speed of introduction of the liquid which can be optionally predispersed, is generally low, less than 10 m / s and preferably less than 5 m / s.
  • the gas-well-vortex phase is obtained, in situ, by means of the gases serving to generate the combustion gas containing the steam of the steam cracking process.
  • This combustion gas will depend in particular on the nature of the charge to be cracked and on the final products which it is desired to favor, but it must in any case be sufficient to cause cracking of the charge, in any case higher than the cracking temperatures in tubular reactors which are of the order of 800 ° -900 ° C.
  • the temperature of this gaseous well-vortex phase will therefore advantageously be as high as possible, taking into account the possibilities of the apparatus, that is to say practically between 1000 and 25 ⁇ 0 ° C.
  • This combustion gas containing superheated steam can be obtained by combustion of a hydrocarbon.
  • the superheated steam produced in zone 1 can also be obtained by direct combustion of hydrogen and oxygen, at least one of these reactants being introduced in a symmetrical helical flow into said zone.
  • This hydrogen can fulfill several functions as a thermal diluent in zone 1 but also as a chemical participant in cracking in zone 2.
  • a non-pure oxygen source can also be used.
  • the method according to the invention has great flexibility with respect to the load introduced.
  • This comprises a combustion chamber (1) which has an envelope (3), closed at its downstream part by a restricted passage (4), a pipe (5) for tangential supply of hydrogen, a supply pipe (6) oxygen.
  • the envelope (3) ends downstream by a convergent (7) in which ends, along the axis of rotation symmetry of the chamber (1) an injection device (8) of the hydrocarbon charge, substantially at the restricted passage (4), a contact chamber (2) extending downstream the chamber (1) along the same axis of symmetry.
  • the chamber (1) has an ignition means (9), an annular cooling space (10) around the injection device (8) and another cooling circuit (11) around said chamber (1 ).
  • a quenching device (12) is provided at the outlet from the contact chamber (2).
  • the hydrocarbon charge consists of a liquid hydrocarbon fuel (domestic fuel oil according to French standards, type 2 according to ASTM standard).
  • the temperature / residence time couple is varied with a device of 20 cm overall size.
  • Examples 1 and 2 are produced with a chamber 2 in the form of a bicone as in the figure.
  • the bicone is replaced by a tube.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Combustion & Propulsion (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Claims (6)

1. Verfahren zum Dampf-Kracken von Kohlenwasserstoffen durch direkten Kontakt, unter in situ-Bildung von Wasserdampf enthaltendem Verbrennungsgas, dadurch gekennzeichnet, dass man die gasförmigen Reaktionspartner in eine erste Zone 1 so einführt, dass die dort entstehende Gasphase die Form einer symmetrischen schraubenförmigen Strömung aufweist, wobei die Reaktionspartner in dieser Zone so reagieren, dass ein Verbrennungsgas erzeugt wird, das überhitzten Wasserdampf enthält, der in Form einer symmetrischen, schraubenförmig sich verengenden Strömung in eine Zone 2 der gleichmässigen Verteilung austritt, in die die Kohlenwasserstoff-Charge, die gekrackt werden soll, auf der Höhe der Zone mit relativem Unterdruck, die durch die schraubenförmig sich verengende Strömung erzeugt wird, eingeführt wird, wobei die Bewegungsgrösse des Verbrennungsgases, das überhitzten Wasserdampf enthält, mit Bezug auf diejenige der flüssigen Charge ausreicht, um das Aufbrechen dieser flüssigen Charge, ihre Zerstäubung und die Übernahme jedes entstandenen Tröpfchens durch ein damit verbundenes Gasvolumen-Element hervorruft, wobei die durch das Verbrennungsgas zugeführte Wärme-Menge ausreicht, um die Verdampfung dieser Charge, deren Überhitzung und ihr Kracken bei der gewünschter Temperatur zu ermöglichen.
2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass die Bewegungsgrösse der Elemente der Gasphase mindestens das 100fache und vorzugsweise das 1000- bis 10000fache derjenigen der Volumenelemente der flüssigen Phase beträgt.
3. Verfahren nach einem der Ansprüche 1 und 2, dadurch gekennzeichnet, dass die Temperatur des Verbrennungsgases mehr als 800°C, vorzugsweise 1 000 bis 2500°C beträgt.
4. Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, dass das überhitzten Wasserdampf enthaltende Verbrennungsgas durch Verbrennung eines Kohlenwasserstoffes erhalten wird.
5. Verfahren nach einem der Ansprüche 1 bis 4, dadurch gekennzeichnet, dass der überhitzte Wasserdampf durch direkte Verbrennung von Wasserstoff und Sauerstoff erhalten wird und dass mindestens einer dieser Reaktionspartner entsprechend einer symmetrischen, schraubenförmigen Strömung eingebracht wird.
6. Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, dass man Wasserstoff im Überschuss einführt.
EP84400992A 1983-05-20 1984-05-16 Verfahren zur Dampfspaltung von Kohlenwasserstoffen Expired EP0127519B1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT84400992T ATE25263T1 (de) 1983-05-20 1984-05-16 Verfahren zur dampfspaltung von kohlenwasserstoffen.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8308395 1983-05-20
FR8308395A FR2546174B1 (fr) 1983-05-20 1983-05-20 Procede de vapocraquage d'hydrocarbures

Publications (2)

Publication Number Publication Date
EP0127519A1 EP0127519A1 (de) 1984-12-05
EP0127519B1 true EP0127519B1 (de) 1987-01-28

Family

ID=9289037

Family Applications (1)

Application Number Title Priority Date Filing Date
EP84400992A Expired EP0127519B1 (de) 1983-05-20 1984-05-16 Verfahren zur Dampfspaltung von Kohlenwasserstoffen

Country Status (6)

Country Link
US (1) US4832822A (de)
EP (1) EP0127519B1 (de)
JP (1) JPS6047097A (de)
AT (1) ATE25263T1 (de)
DE (1) DE3462267D1 (de)
FR (1) FR2546174B1 (de)

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2785289B1 (fr) * 1998-10-16 2007-01-05 Pierre Charles Jorgensen Conversion profonde jumelant la demetallisation et la conversion de bruts, residus ou huiles a l'aide de composes oxygenes purs ou impurs (h20 c02 co accompagnes de n2 h2 sh2...)
ID29093A (id) * 1998-10-16 2001-07-26 Lanisco Holdings Ltd Konversi mendalam yang menggabungkan demetalisasi dan konversi minyak mentah, residu atau minyak berat menjadi cairan ringan dengan senyawa-senyawa oksigenat murni atau tak murni
AU2004201428B2 (en) * 1998-10-16 2006-01-12 Carbon Resources Limited System for the conversion of hydrocarbons
US20050038304A1 (en) * 2003-08-15 2005-02-17 Van Egmond Cor F. Integrating a methanol to olefin reaction system with a steam cracking system
RU2405622C2 (ru) 2009-03-23 2010-12-10 Владимир Андреевич Бушуев Лопаточный реактор для пиролиза углеводородов
RU2518080C2 (ru) * 2011-07-08 2014-06-10 Общество с ограниченной ответственностью "Премиум Инжиниринг" Способ и устройство переработки тяжелого нефтяного сырья
FR3047483B1 (fr) * 2016-02-09 2020-02-14 Suez Rv Bioenergies Procede de traitement d'un lixiviat ou d'un concentrat de lixiviat charge en constituants mineraux et organiques

Family Cites Families (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2790838A (en) * 1952-01-16 1957-04-30 Eastman Kodak Co Process for pyrolysis of hydrocarbons
BE547808A (de) * 1955-05-13 1900-01-01
DE1112064B (de) * 1956-08-06 1961-08-03 Koppers Gmbh Heinrich Verfahren und Vorrichtung zur Erzeugung von ungesaettigten Kohlenwasserstoffen, insbesondere Acetylen und AEthylen, durch thermische Spaltung von Kohlenwasserstoffoelen
US3019271A (en) * 1958-09-08 1962-01-30 Belge Produits Chimiques Sa Process and apparatus for treatment of hydrocarbons
FR1236499A (fr) * 1958-09-30 1960-07-15 Basf Ag Procédé et dispositif pour la production d'hydrocarbures non saturés à partir d'hydrocarbures liquides
US3203769A (en) * 1961-12-06 1965-08-31 Res Ass Of Polymer Raw Materia Furnace for cracking hydrocarbons having a flame-adjustable burner
BE626824A (de) * 1962-01-08
US3168592A (en) * 1962-07-19 1965-02-02 Du Pont Manufacture of acetylene by two stage pyrolysis under reduced pressure with the first stage pyrolysis conducted in a rotating arc
GB1116521A (en) * 1964-08-24 1968-06-06 Kureha Chemical Ind Co Ltd A process for the thermal cracking of hydrocarbons
US3399245A (en) * 1966-01-28 1968-08-27 Monsanto Co Process and apparatus for partial combustion of hydrocarbons
US3498753A (en) * 1966-07-04 1970-03-03 Nippon Zeon Co Apparatus for thermal cracking of hydrocarbon
DE1643811A1 (de) * 1966-10-14 1971-03-11 Chepos Zd Y Chemickeho A Potra Verfahren und Anlage zur Durchfuehrung von Pyrolysereaktionen
JPS5836895B2 (ja) * 1973-05-23 1983-08-12 凸版印刷株式会社 タシヨクズリヨウゲンバン
CA1032561A (en) * 1973-07-09 1978-06-06 Gerard R. Kamm Process for cracking crude oil
FR2294225A1 (fr) * 1974-12-09 1976-07-09 Erap Procede perfectionne de conversion thermique d'hydrocarbures
US4136015A (en) * 1977-06-07 1979-01-23 Union Carbide Corporation Process for the thermal cracking of hydrocarbons
US4256565A (en) * 1979-11-13 1981-03-17 Rockwell International Corporation Method of producing olefins from hydrocarbons

Also Published As

Publication number Publication date
DE3462267D1 (en) 1987-03-05
EP0127519A1 (de) 1984-12-05
FR2546174A1 (fr) 1984-11-23
ATE25263T1 (de) 1987-02-15
US4832822A (en) 1989-05-23
FR2546174B1 (fr) 1986-09-19
JPS6047097A (ja) 1985-03-14

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