EP0207502B1 - Procédé pour le prétraitement des charges pour l'hydrogénation d'huiles lourdes - Google Patents

Procédé pour le prétraitement des charges pour l'hydrogénation d'huiles lourdes Download PDF

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Publication number
EP0207502B1
EP0207502B1 EP86108968A EP86108968A EP0207502B1 EP 0207502 B1 EP0207502 B1 EP 0207502B1 EP 86108968 A EP86108968 A EP 86108968A EP 86108968 A EP86108968 A EP 86108968A EP 0207502 B1 EP0207502 B1 EP 0207502B1
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EP
European Patent Office
Prior art keywords
gas
hydrogenation
heat exchanger
heavy oil
mixture
Prior art date
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Expired - Lifetime
Application number
EP86108968A
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German (de)
English (en)
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EP0207502A2 (fr
EP0207502A3 (en
Inventor
Heinz Frohnert
Bernd Uckermann
Wolfdieter Klein
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Veba Oel Technologie und Automatisierung GmbH
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Veba Oel Technologie und Automatisierung GmbH
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Publication of EP0207502A3 publication Critical patent/EP0207502A3/de
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Classifications

    • 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
    • C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00

Definitions

  • the invention relates to a method for pretreating the feed products for heavy oil hydrogenation with preheated hydrogen-containing hydrogenation gas of the type specified in the preamble of claim 1.
  • the object of the invention is to reduce the specific area required for heat exchange for heating the oil-additive mixture. Another task is to reduce the mechanical energy required to operate the gas compressors.
  • the current of the gaseous hot separator head product which is guided over the first heat exchanger designed as a gas heat exchanger, is conducted via a gas phase reactor with a contact fixedly arranged on a support and then via at least one heat exchanger for heating the mixture of heavy oil, additive and hydrogenation gas.
  • the other part of the hydrogenation gas heated by heat exchange with the gaseous hot separator head product and added to the preheated heavy oil mixture makes 40 to 80 vol .-% of the total amount of hydrogenation gas required.
  • An advantageous embodiment provides that part of the amount of hydrogenation gas passed through the gas heat exchanger is only added to the heavy oil mixture after the mixture has passed through the preheater.
  • a further advantageous embodiment consists in further heating the part of the hydrogenation gas which is passed through the first heat exchanger in an oven and adding it to the heavy oil mixture on the downstream side of the preheater, a further partial flow of the hydrogenation gas stream heated in the furnace again injecting the heavy oil mixture into can be added to the preheater.
  • the portion of hydrogenation gas which is initially conducted separately can also be heated up solely via the furnace.
  • a partial stream of the fresh hydrogen used or of the cycle hydrogenation gas can be introduced directly into the hydrogenation reactor as quench gas.
  • the top product of the hot separator which is initially passed through the gas heat exchanger, is fed to the heat exchangers for the heavy oil mixture and further cooled in countercurrent to the heavy oil mixture by heat exchange.
  • the hydrogenation gas In the reaction part, i.e. H. in the actual hydrogenation reactors, after adding the remaining amount of 40 to 80% by volume, the entire required amount of hydrogenation gas is available, where the hydrogenation gas also has the task of promoting the transfer of the vaporizable reaction products formed into the hot separator.
  • a part of the capacity of the preheater is taken over by the gas heat exchanger or furnace to which the hot separator head product is applied, with the fact that a gas heat exchanger or a furnace in which a gas is heated only takes up about a fifth of the total exchange area of one Heat exchanger or preheater required for preheating the heavy oil mixture representing a multi-phase system.
  • the present separate preheating of a part of the hydrogenation gas enables better heat utilization of the heat content of the hot separator head product and a simplified design of the preheater.
  • the design and operation of the preheater for heating the heavy oil mixture are critical for the operation of heavy oil hydrogenation in the sump phase.
  • the partial flow of the hydrogenation gas heated in the gas heat exchanger to 350 to 470 ° C, maximum 490 ° C, in countercurrent with the top product of the hot separator or in the additional furnace to temperatures between 350 and 550 ° C may still depend on the operational requirements and
  • the operating state of the preheater can be divided into a partial stream that is upstream of the preheater and a partial stream that is fed from the preheater to the heavy oil mixture on the downstream side.
  • the heavy oil additive mixture which has been mixed with the hydrogenation gas and pressurized, is directed towards the hot separator head product in successive heat exchangers, in counterflow and after passing through a gas heat exchanger.
  • the lowering of the temperature of the hot separator head product in a first heat exchanger which is expediently designed as a gas heat exchanger, is also necessary because, in the case of a subsequent gas phase hydrogenation, the fixed bed contact usually gives the best results from an operational point of view at somewhat lower temperatures than the temperature of the hot separator head product.
  • Additives in the present method include, for example, carbon-containing products with a high specific surface, e.g. B. petroleum coke, brown coal coke, gasification residues and. Like understood. They are added in an amount of about 2 to 5% by weight, based on the amount of heavy oil used.
  • the heavy oil mixture mixed with the partial flow of the hydrogenation gas and possibly the remaining hydrogenation gas has a temperature of approximately 380 ° C. after passing through the heat exchangers and a temperature of approximately 460 ° C. after passing through the downstream preheater.
  • the hydrogenation gas can be passed over the last downstream heat exchanger through which the hot separator head product flows before it is added to the heavy oil mixture.
  • the heavy oil mixture brought to the process pressure is charged with fresh gas (for example about 97% by weight hydrogen) as a hydrogenation gas via line 1.
  • fresh gas for example about 97% by weight hydrogen
  • the heavy oil mixture After admixing the possibly preheated amount of hydrogenation gas, one or more successive heat exchangers 2, in which it is preheated in countercurrent to the top product of the heat separator or the outflow of an intermediate gas phase reactor 9, then runs the preheater 4 before it enters the first hydrogenation reactor via line 5 .
  • the top product of the hot separator may pass through a gas heat exchanger 6, in which the remaining portion of the required amount of hydrogenation gas, which is conducted in line 7, is preheated to 350 to a maximum of 500 ° C., then the gas phase reactor 9, in which a further hydrogenation of the gas or vaporous hydrogenation products from the bottom phase at a fixed hydrogenation contact takes place in the mixed phase as well as the mash preheater 2 and possibly a fresh gas preheater, not shown.
  • an oven 8 is connected downstream.
  • the hydrogenation gas stream heated in this way is added to the mash in part before it enters the preheater 4 and in part on the downstream side from the preheater 4.
  • FIG. 2 shows the process control in which the stream of hydrogenation gas conducted via line 7 and gas heat exchanger 6 converts the heavy oil mixture. is supplied from the preheater 4 on the current side.
  • the hydrogenation gas stream heated in the gas heat exchanger 6 can, however, also be added to the heavy oil mixture on the downstream side from the preheater 4.
  • the remaining reference numerals have the meaning as explained for FIG. 1
  • furnace 8 for the purpose of heating the hydrogenation gas and to pass the hot separator head product over a first heat exchanger to heat the heavy oil mixture.
  • the hydrogenation gas can be heated to, for example, 550 ° C.
  • the separate heating of parts of the hydrogenation gas in the present method enables lower tube wall thicknesses for the guidance of the hydrogenation gas and a simplified distribution or division of the hydrogenation gas, as well as a lower required output of the heating and preheating furnaces. Finally, the pressure losses in the circulatory system are about 50% lower because only the proportion of fresh gas has to be pushed up to the operating pressure.

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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)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Claims (6)

  1. Procédé pour le prétraitement des charges pour l'hydrogénation des huiles lourdes avec du gaz hydrogénant préchauffé contenant de l'hydrogène sous haute pression et à haute température, en utilisant un additif, dans un milieu liquide, dans lequel on fait passer l'huile lourde dans un préchauffeur, pour la soumettre ensuite à une réaction d'hydrogénation dans une cascade de réacteur, d'où les produits de réaction sont introduits dans un séparateur chaud, dans lequel on mélange seulement une partie de l'ordre de 20 à 60 % en volume de la quantité totale de gaz hydrogénant nécessaire dans la phase liquide, avec le mélange d'huile lourde et d'additif porté à la pression du procédé mais non encore préchauffé, caractérisé en ce qu'on porte à une température de 350 à 470, au maximum à 490 ou aussi à 500°C, l'autre fraction de gaz hydrogénant, qui représente 40 à 80 %, en volume de la quantité totale nécessaire de gaz hydrogénant, par échange thermique avec le produit gazeux de tête du séparateur chaud dans un premier échangeur thermique constitué en échangeur thermique à gaz qu'on préchauffe à environ 460° le mélange d'huile lourde et d'additif, ainsi que le gaz hydrogénant par échange thermique dans un ou plusieurs échangeurs thermiques intercalés à la suite de l'échangeur thermique à gaz, parcourus par le produit de tête du séparateur chaud après son passage dans l'échangeur thermique à gaz, et on ajoute la quantité de gaz hydrogénant chauffée dans l'échangeur thermique à gaz au mélange préchauffé d'huile lourde, d'additif et de gaz hydrogénant.
  2. Procédé selon la revendication 1, caractérisé en ce qu'on fait passer le courant du produit de tête gazeux du séparateur chaud ayant traversé le premier échangeur de chaleur constitué en échangeur à gaz, dans un réacteur en phase gazeuse avec une masse de contact disposée fixement sur un support et ensuite dans au moins un échangeur thermique pour réchauffer le mélange d'huile lourde, d'additif et de gaz hydrogénant.
  3. Procédé selon la revendication 1 ou 2, caractérisé en ce qu'on ajoute une partie de la quantité de gaz hydrogénant ayant traversé l'échangeur thermique à gaz, seulement après que le mélange d'huiles lourdes ait traversé le préchauffeur.
  4. Procédé selon l'une des revendications 1 à 3, caractérisé en ce qu'on utilise un four en plus de l'échangeur thermique à gaz, pour chauffer le courant partiel de gaz hydrogénant.
  5. Procédé selon la revendication 1, caractérisé en ce qu'on prévoit à la place de l'échangeur thermique à gaz un four pour chauffer le courant partiel de gaz hydrogénant à 550°C et qu'on utilise déjà le produit de tête du séparateur chaud dans le premier échangeur thermique pour préchauffer le mélange d'huiles lourdes.
  6. Procédé selon l'une des revendications 1 à 5, caractérisé en ce qu'on partage le courant de gaz hydrogénant contenant de l'hydrogène, de façon à ce que l'addition au mélange d'huiles lourdes se fasse sous forme d'hydrogène frais et qu'on mélange la quantité restante d'hydrogène frais complémentaire au gaz hydrogénant du circuit.
EP86108968A 1985-07-03 1986-07-02 Procédé pour le prétraitement des charges pour l'hydrogénation d'huiles lourdes Expired - Lifetime EP0207502B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19853523709 DE3523709A1 (de) 1985-07-03 1985-07-03 Verfahren zur vorbehandlung der einsatzprodukte fuer die schweroelhydrierung
DE3523709 1985-07-03

Publications (3)

Publication Number Publication Date
EP0207502A2 EP0207502A2 (fr) 1987-01-07
EP0207502A3 EP0207502A3 (en) 1988-07-20
EP0207502B1 true EP0207502B1 (fr) 1991-03-06

Family

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EP86108968A Expired - Lifetime EP0207502B1 (fr) 1985-07-03 1986-07-02 Procédé pour le prétraitement des charges pour l'hydrogénation d'huiles lourdes

Country Status (3)

Country Link
EP (1) EP0207502B1 (fr)
JP (1) JPH086095B2 (fr)
DE (2) DE3523709A1 (fr)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3741105A1 (de) * 1987-12-04 1989-06-15 Veba Oel Entwicklungs Gmbh Verfahren zur hydrierung fluessiger kohlenstoffhaltiger einsatzstoffe
US6908543B1 (en) 2000-10-23 2005-06-21 Chevron U.S.A. Inc. Method for retarding fouling of feed heaters in refinery processing

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4075081A (en) * 1975-08-15 1978-02-21 Cities Service Company Fluidized bed hydroretorting of oil shale
DE2651253C2 (de) * 1976-11-10 1984-03-08 Saarbergwerke AG, 6600 Saarbrücken Verfahren zum Hydrieren von Kohle
DE3002209C2 (de) * 1980-01-22 1985-01-24 Uop Inc., Des Plaines, Ill. Verfahren zur Umwandlung von Kohlenwasserstoffen
US4424108A (en) * 1982-01-08 1984-01-03 The Pittsburg & Midway Coal Mining Co. Process for heating coal-oil slurries
US4387015A (en) * 1982-09-30 1983-06-07 International Coal Refining Company Coal liquefaction quenching process
DE3505553A1 (de) * 1985-02-18 1986-08-21 Veba Oel Entwicklungs-Gesellschaft mbH, 4650 Gelsenkirchen Verfahren zur vorbehandlung der einsatzprodukte fuer die kohlehydrierung

Also Published As

Publication number Publication date
JPH086095B2 (ja) 1996-01-24
EP0207502A2 (fr) 1987-01-07
JPS6270485A (ja) 1987-03-31
DE3523709A1 (de) 1987-01-08
DE3677834D1 (de) 1991-04-11
EP0207502A3 (en) 1988-07-20

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