EP0306164B1 - Hydrogénation d'un courant d'hydrocarbures usés sensibles à la température - Google Patents

Hydrogénation d'un courant d'hydrocarbures usés sensibles à la température Download PDF

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Publication number
EP0306164B1
EP0306164B1 EP88307448A EP88307448A EP0306164B1 EP 0306164 B1 EP0306164 B1 EP 0306164B1 EP 88307448 A EP88307448 A EP 88307448A EP 88307448 A EP88307448 A EP 88307448A EP 0306164 B1 EP0306164 B1 EP 0306164B1
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Prior art keywords
stream
hydrocarbonaceous
hydrogen
distillable
temperature
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German (de)
English (en)
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EP0306164A1 (fr
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Tom N. Kalnes
Robert B. James
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Honeywell UOP LLC
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UOP LLC
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
    • C10M175/0025—Working-up used lubricants to recover useful products ; Cleaning by thermal processes
    • C10M175/0041—Working-up used lubricants to recover useful products ; Cleaning by thermal processes by hydrogenation processes
    • 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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
    • 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
    • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
    • C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
    • C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps

Definitions

  • This invention relates to the production of a hydrogenated distillable and reusable hydrocarbonaceous product stream from a temperature-sensitive hydrocarbonaceous waste stream containing a non-distillable component. More specifically, the invention relates to a process using a combination of flash vaporization and selective hydrogenation for treating a temperature-sensitive hydrocarbonaceous waste stream containing a non-distillable component to produce a hydrogenated distillable and reusable hydrocarbonaceous product stream and a heavy non-distillable product, while minimizing thermal degradation of the hydrocarbonaceous waste stream.
  • EP-A-0301758 which is a document to be considered as comprised in the state of the art in accordance with Article 54(3) EPC discloses a process for treating a temperature-sensitive hydrocarbonaceous waste stream containing a non-distillable component to produce a distillable hydrocarbonaceous product and a heavy product comprising the non-distillable component while minimizing thermal degradation of the hydrocarbonaceous stream by
  • EP-A-0270813 which is also a document to be considered as comprised in the state of the art in accordance with Article 54(3) EPC discloses a process for the treatment of waste oil which is mixed with hydrogen at an elevated pressure of 50 to 250 bars (5 to 25 MPa), and heated by an external heater to 350 to 500°C. After separation of solids as a slurry, the vaporized oil rich phase is catalytically hydrogenated at 300 to 400°C.
  • the invention provides an improved process for the production of a hydrogenated distillable and reusable hydrocarbonaceous product from a temperature-sensitive hydrocarbonaceous waste stream containing a non-distillable component by contacting the hydrocarbonaceous feed stream with a hot hydrogen-rich gaseous stream to increase the temperature of the feed stream and vaporizing at least a portion of the distillable hydrocarbonaceous compounds, thereby producing a distillable hydrocarbonaceous product which, according to the present invention, is immediately hydrogenated in an integrated hydrogenation zone.
  • Important elements of the improved process are the relatively short time that the feed stream is maintained at elevated temperature, the avoidance of heating the feed stream by indirect heat exchange whereby to preclude the coke formation that could otherwise occur, and the minimization of utility costs due to the integration of the hydrogenation zone.
  • One embodiment of the invention is a process for treating a temperature-sensitive hydrocarbonaceous waste stream containing a non-distillable component to produce a hydrogenated distillable and reusable hydrocarbonaceous product and a heavy non-distillable product, while minimizing thermal degradation of the hydrocarbonaceous stream, which comprises (a) contacting the waste stream with a first hydrogen-rich gaseous stream having a temperature greater than the waste stream in a flash zone at flash conditions, thereby increasing the temperature of the waste stream and vaporizing at least a portion thereof to provide a hydrocarbonaceous vapour stream comprising hydrogen, and a heavy product comprising the non-distillable component; immediately (b) catalytically hydrogenating the vapour stream in a hydrogenation reaction zone at hydrogenation conditions to increase the degree of hydrogenation of the hydrocarbonaceous compounds contained in the vapour stream; (c) condensing at least a portion of the resulting effluent from the hydrogenation reaction zone to provide a second hydrogen-rich gaseous stream, suitable for recycle to step (
  • the liquid stream obtained in the condensation step (c) is a first liquid stream comprising fuel gas and hydrogenated distillable hydrocarbonaceous compounds, and in step (d) fuel gas is separated from the first liquid stream to provide a second hydrocarbonaceous vapour stream comprising normally gaseous hydrocarbons and a normally liquid hydrogenated distillable hydrocarbonaceous product.
  • the catalytic hydrogenation generates at least one water-soluble inorganic compound by reaction of the hydrocarbonaceous compounds and the effluent from the hydrogenation zone is contacted with a fresh aqueous scrubbing solution, the resulting mixture of effluent and aqueous scrubbing solution is separated to provide the second hydrogen-rich gaseous stream suitable for recycle to step (a), a first liquid stream comprising fuel gas and hydrogenated distillable hydrocarbonaceous compounds, and a spent aqueous scrubbing solution containing at least a portion of the water-soluble inorganic compound; and fuel gas is separated from the first liquid stream to provide a second hydrocarbonaceous vapour stream comprising normally gaseous hydrocarbons and a normally liquid hydrogenated distillable hydrocarbonaceous product.
  • the present invention provides an improved integrated process for the removal of heavy non-distillable components from a temperature-sensitive hydrocarbonaceous waste stream and the subsequent hydrogenation of the distillable hydrocarbonaceous stream.
  • a wide variety of temperature-sensitive hydrocarbonaceous waste stream can be treated in accordance with the process of the present invention.
  • suitable hydrocarbonaceous streams are dielectric fluids, hydraulic fluids, heat transfer fluids, used lubricating oil, used cutting oils, used solvents, still bottoms from solvent recycle operations, coal tars, atmospheric residuum, oils contaminated with polychlorinated biphenyls (PCB), halogenated wastes and other hydrocarbonaceous industrial waste.
  • non-distillable components which include, for example, organometallic compounds, inorganic metallic compounds, finely divided particulate matter and non-distillable hydrocarbonaceous compounds.
  • the present invention is particularly advantageous when the non-distillable components comprise sub-micron particulate matter, and the conventional techniques of filtration or centrifugation tend to be highly ineffective.
  • a non-distillable component including finely divided particulate matter in a hydrocarbonaceous feed to a hydrogenation zone greatly increases the difficulty of the hydrogenation.
  • a non-distillable component tends 1) to foul the hot heat exchange surfaces which are used to heat the feed to hydrogenation conditions, 2) to form coke, or in some other manner deactivate the hydrogenation catalyst, thereby shortening its active life and 3) to hinder in other ways a smooth and facile hydrogenation operation.
  • Particulate matter in a feed stream tends to be deposited within the hydrogenation zone and to plug a fixed hydrogenation catalyst bed, thereby reducing the time on stream.
  • the resulting distillable hydrocarbonaceous stream is introduced into a hydrogenation zone. If the feed stream contains compounds of metals such as zinc, copper, iron, barium, phosphorus, magnesium, aliminium, lead, mercury, cadmium, cobalt, arsenic, vanadium, chromium, and nickel, these compounds will be isolated in the relatively small volume of recovered non-distillable product, which may then be treated for metals recovery, or otherwise disposed of as desired.
  • metals such as zinc, copper, iron, barium, phosphorus, magnesium, aliminium, lead, mercury, cadmium, cobalt, arsenic, vanadium, chromium, and nickel
  • the hydrogenation step will remove or convert such components as desired.
  • the hydrogenation of the resulting distillable hydrocarbonaceous stream is preferably conducted immediately after flashing the feed, without intermediate separation or condensation.
  • the hot first hydrogen-rich gaseous stream preferably comprises more than 70 mole % hydrogen, and more preferably more than 90 mole % hydrogen.
  • the hot hydrogen-rich gaseous stream is multi-functional and serves as 1) a heat source used for direct heating of the hydrocarbonaceous feed stream, to preclude the coke formation that could otherwise occur when using an indirect heating apparatus such as a heater or heat-exchanger, 2) a diluent to reduce the partial pressure of the hydrocarbonaceous compounds during vaporization in the flash zone, 3) a possible reactant to minimize the formation of hydrocarbonaceous polymers at elevated temperatures, 4) a stripping medium and 5) at least a portion of the hydrogen required in the hydrogenation reaction zone.
  • the temperature-sensitive hydrocarbonaceous feed stream is preferably maintained at a temperature less than 482°F (250°C) before being introduced into the flash zone in order to prevent or minimize the thermal degradation of the feed stream.
  • the hot hydrogen-rich gaseous stream is introduced into the flash zone at a temperature greater than the hydrocarbonaceous feed stream, and preferably at a temperature from 200 to 1200°F (93 to 649°C).
  • the flash zone is preferably maintained at flash conditions which include a temperature from 150 to 860°F (165 to 460°C), a pressure from atmospheric to 2000 psig (13788 kPa gauge), a hydrogen circulation rate of 1000 to 30,000 SCFB (168 to 5056 normal m/m3), based on the temperature-sensitive hydrocarbonaceous feed stream and an average residence time of the hydrogen-containing, hydrocarbonaceous vapour stream in the flash zone from 0.1 to 50 seconds.
  • a more preferred average residence time of the hydrogen-containing, hydrocarbonaceous vapour stream in the flash zone is from 1 to 10 seconds.
  • the resulting heavy non-distillable portion of the feed stream is removed from the bottom of the flash zone as required, to yield a heavy non-distillable product.
  • the heavy non-distillable product may contain a relatively small amount of distillable components, but since essentially all of non-distillable components contained in the hydrocarbonaceous feed stream are recovered in this product stream, the term "heavy non-distillable product" is nevertheless used for the convenient description of this product stream.
  • the heavy non-distillable product preferably contains a distillable component of less than 10 weight percent, and more preferably less than 5 weight percent.
  • an additional liquid may be utilized to flush the heavy non-distillables from the flash zone.
  • a flush liquid may, for example, be a high boiling range vacuum gas oil having a boiling range from 700 to 1000°F (371 to 538°C), or a vacuum tower bottoms stream boiling at a temperature greater than 1000°F (538°C).
  • the selection of a flush liquid depends upon the composition of the hydrocarbonaceous feed stream and the prevailing flash conditions in the flash separator, and the volume of the flush liquid is preferably limited to that required for removal of the heavy non-distillable component.
  • the resulting hydrogen-containing, hydrocarbonaceous vapour stream is removed from the flash zone and is immediately introduced into a catalytic hydrogenation zone containing hydrogenation catalyst and maintained at hydrogenation conditions.
  • the catalytic hydrogenation zone may contain a fixed, ebullated or fluidized catalyst bed.
  • This reaction zone is preferably maintained under an imposed pressure from atmospheric pressure to 2000 psig (0 to 13790 kPa gauge) and more preferably under a pressure from 100 to 1800 psig (689.5 to 12411 kPa gauge).
  • a maximum catalyst bed temperature of 122 to 850°F (50 to 454°C) selected to perform the desired hydrogenation conversion to reduce or eliminate the undesirable characteristics or components of the hydrocarbonaceous vapour stream.
  • the desired hydrogenation conversion may be, for example, dehalogenation, desulphurization, denitrification, olefin saturation, oxygenate conversion or hydrocracking.
  • Further preferred operating conditions include liquid hourly space velocities from 0.05 to 20 hr ⁇ 1 and hydrogen circulation rates from 200 to 50,000 standard cubic feet per barrel (SCFB) (33.71 to 8427 normal m3/m3), preferably from 300 to 20,000 SCFB (50.6 to 3371 normal m3/m3).
  • SCFB standard cubic feet per barrel
  • the temperature of the hydrogen-containing, hydrocarbonaceous vapour stream which is removed from the flash zone is not deemed to be exactly the temperature selected for the catalytic hydrogenation zone
  • the temperature of the hydrogen-containing, hydrocarbonaceous stream may be adjusted either upwards or downwards by any means known to those skilled in the art in order to achieve the desired temperature in the catalytic hydrogenation zone. Such a temperature adjustment may be accomplished, for example, by the addition of either cold or hot hydrogen.
  • the preferred catalyst composite disposed within the hereinabove described hydrogenation zone can contain a metal component having hydrogenation activity, combined with a suitable refractory inorganic oxide carrier material of either synthetic or natural origin.
  • a suitable refractory inorganic oxide carrier material of either synthetic or natural origin.
  • Preferred carrier materials are alumina, silica and mixtures thereof.
  • Suitable metal components having hydrogenation activity are metals of Groups VI-B and VIII of the Periodic Table, as set forth in the Periodic Table of the Elements, E. H. Sargent and Company, 1964.
  • the catalyst composites may comprise one or more of molybdenum, tungsten, chromium, iron, cobalt, nickel, platinum, palladium, iridium, osmium, rhodium, ruthenium, and mixtures thereof.
  • concentration of the catalytically active metal component, or components is primarily dependent upon the particular metal as well as the physical and/or chemical characteristics of the particular hydrocarbon feedstock.
  • metals of Group VI-B are generally present in an amount from 1 to 20 weight percent, the iron-group metals in an amount from 0.2 to 10 weight percent, whereas the noble metals of Group VIII are preferably present in an amount from 0.1 to 5 weight percent, all of which are calculated as if these components existed within the catalyst composite in the elemental state.
  • any catalyst employed commercially for hydrogenating middle distillate hydrocarbonaceous compounds to remove nitrogen and sulphur may function effectively in the hydrogenation zone of the present invention.
  • hydrogenation catalyst composites may comprise one or more of: caesium, francium, lithium, potassium, rubidium, sodium, copper, gold, silver, cadmium, mercury and zinc.
  • the hydrocarbonaceous effluent stream from the hydrogenation zone is preferably subjected to cooling conditions sufficient to condense at least a portion thereof, and thereafter contacted with an aqueous scrubbing solution.
  • the aqueous scrubbing solution may be used to accomplish a portion of the desired condensation.
  • the resulting mixture is admitted to a separation zone in order to separate a spent aqueous stream, a hydrogenated hydrocarbonaceous liquid phase and a hydrogen-rich gaseous phase.
  • the contact of the hydrocarbonaceous effluent from the hydrogenation zone with the aqueous scrubbing solution may be performed in any convenient manner, and is preferably conducted by co-current, in-line mixing, which may be promoted by inherent turbulence, mixing orifices or any other suitable mixing means.
  • the aqueous scrubbing solution is preferably introduced in an amount from 1 to 100 volume percent, based on the hydrocarbonaceous effluent from the hydrogenation zone.
  • the aqueous scrubbing solution is selected depending on the characteristics of the hydrocarbonaceous vapour stream introduced into the hydrogenation zone.
  • the aqueous scrubbing solution preferably contains a basic compound such as calcium hydroxide, potassium hydroxide or sodium hydroxide in order to neutralize the acid such as hydrogen chloride, hydrogen bromide and hydrogen fluoride, for example, which is formed during the hydrogenation of the halogen compounds.
  • a basic compound such as calcium hydroxide, potassium hydroxide or sodium hydroxide in order to neutralize the acid such as hydrogen chloride, hydrogen bromide and hydrogen fluoride, for example, which is formed during the hydrogenation of the halogen compounds.
  • water may be a suitable aqueous scrubbing solution to dissolve the resulting hydrogen sulphide and ammonia.
  • the resulting hydrogenated hydrocarbonaceous liquid phase is recovered and the hydrogen-rich gaseous phase may be recycled to the hydrogenation zone if desired.
  • the resulting hydrogenated hydrocarbonaceous liquid phase is preferably recovered from the hydrogen-rich gaseous phase in a separation zone which is maintained at essentially the same pressure as the hydrogenation reaction zone and as a consequence contains dissolved hydrogen and low molecular weight normally gaseous hydrocarbons (if present).
  • the hydrogenation hydrocarbonaceous liquid phase comprising the hereinabove mentioned gases be stabilized in a convenient manner, for example, by stripping or flashing to remove the normally gaseous components to provide a stable hydrogenated distillable hydrocarbonaceous product.
  • a liquid hydrocarbonaceous feed waste stream having a non-distillable component is introduced into the process via conduit (1) and is contacted with a hot gaseous hydrogen-rich recycle stream which is provided via conduit (10) from a source hereinafter described.
  • the liquid hydrocarbonaceous feed waste stream and the hydrogen-rich recycle stream are intimately contacted in hot hydrogen flash separator (2).
  • a hydrocarbonaceous vapour stream comprising hydrogen is removed from separator (2) via conduit (3) and immediately introduced into hydrogenation reaction zone (5) which is maintained at hydrogenation conditions, without intermediate separation thereof.
  • a heavy non-distillable stream is removed from the bottom of separator (2) via conduit (4) and recovered.
  • the resulting hydrogenated hydrocarbonaceous vapour stream is removed from reaction zone (5) via conduit (6) and is contacted with an aqueous scrubbing solution, which is introduced via conduit (7), to cause condensation of at least a portion of the vapour stream.
  • the resulting mixture of the effluent and the aqueous scrubbing solution is passed via conduit (6) and cooled in heat-exchanger (8) to cause a further portion of the vapour stream to be condensed.
  • the resulting cooled effluent from heat-exchanger (8) is passed via conduit (6) into high pressure vapour/liquid separator (9).
  • a hydrogen-rich gaseous stream is removed from high pressure vapour/liquid separator (9) via conduit (10), heated to a suitable temperature in heat-exchanger (12) and utilized to contact the waste oil feed stream (1) as hereinabove described. Since hydrogen is lost from the process, because a portion of the hydrogen will dissolve in the liquid hydrocarbon product and hydrogen will be consumed during the hydrogenation reaction, it is necessary to supplement the hydrogen-rich gaseous stream with make-up hydrogen from some suitable external source, for example, a catalytic reforming unit or a hydrogen plant. Make-up hydrogen may be introduced into the system at any convenient and suitable point, and is introduced in the embodiment shown in the Drawing via conduit (11).
  • a liquid hydrogenated hydrocarbonaceous stream comprising hydrogen in solution is removed from high pressure vapour/liquid separator (9) via conduit (14) and is introduced into low pressure vapour/liquid separator (15).
  • a spent aqueous scrubbing solution is removed from high pressure vapour/liquid separator (9) via conduit (13) and is recovered.
  • a gaseous stream comprising hydrogen and any normally gaseous hydrocarbons present is removed from low pressure vapour/liquid separator (15) via conduit (17) and recovered.
  • a normally liquid distillable hydrogenated hydrocarbonaceous product is removed from low pressure vapour/liquid separator (15) via conduit (16) and recovered. In the event that the waste oil feed stream contains water, this water is recovered from high pressure vapour/liquid separator (9) via conduit (13) together with the spent aqueous scrubbing solution as hereinabove described.
  • a waste lube oil having the characteristics presented in Table 1 and contaminated with 1020 ppm by weight of polychlorinated biphenyl (PCB) was charged in admixture with a hot hydrogen stream at a rate of 100 mass units per hour to a hot hydrogen flash separation zone.
  • the hot hydrogen was introduced into the hot hydrogen flash separation zone at a rate of 31 mass units per hour.
  • the waste lube oil was preheated to a temperature of ⁇ 482°F ( ⁇ 250°C) before introduction into the hot hydrogen flash separation zone, which temperature precluded any significant detectable thermal degradation.
  • the waste lube oil was intimately contacted in the hot flash separation zone with a hot hydrogen-rich gaseous stream having a temperature upon introduction into the hot hydrogen flash separation zone of >748°F (>398°C).
  • the hot hydrogen flash separation zone was operated at conditions which included a temperature of 748°F (398°C), a pressure of 500 psig (3447 kPa gauge), a hydrogen circulation rate of 18,000 SCFB (3034 normal m3/m3) and an average residence time of the vapour stream of 5 seconds.
  • a hydrocarbonaceous vapour stream comprising hydrogen was recovered from the hot hydrogen flash separation zone, and directly and immediately introduced, without separation, into a hydrogenation reaction zone containing a hydrogenation catalyst comprising alumina, cobalt and molybdenum.
  • the hydrogenation reaction is conducted with a catalyst peak temperature of 700°F (371°C), a pressure of 500 psig (3447 kPa gauge), a liquid hourly space velocity of 0.5, based on hydrocarbon feed to the hydrogenation reaction zone, and a hydrogen circulation rate of 18,000 SCFB (3034 normal m3/m3).
  • the hydrogenated effluent from the hydrogenation reaction zone including hydrogen chloride
  • an aqueous scrubbing solution containing sodium hydroxide cooled to 100°F (38°C)
  • a vapour-liquid high pressure separator wherein a gaseous hydrogen-rich stream is separated from the normally liquid hydrocarbonaceous products and spent aqueous scrubbing solution containing sodium and chloride ions.
  • the resulting gaseous hydrogen-rich stream is heated, and then recycled to the hot hydrogen flash separation zone, together with a fresh supply of hydrogen in an amount sufficient to maintain the hydrogenation reaction zone pressure.
  • a hydrogenated hydrocarbonaceous stream comprising dissolved hydrogen is removed from the vapour-liquid high pressure separator and introduced into a product stabilizer which is maintained at a pressure of 10 psia (68.9 kPa absolute) and a temperature of 100°F (38°C).
  • An overhead gaseous stream in an amount of ⁇ 1 mass unit per hour and having the characteristics presented in Table 2 is recovered from the hereinabove mentioned product stabilizer.

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Claims (9)

  1. Procédé de traitement d'un courant hydrocarboné résiduaire sensible à la température, (1) contenant un composant non distillable, pour obtenir un produit hydrocarboné hydrogéné, distillable (16) et un produit lourd (4) comprenant ledit composant non distillable, selon lequel :
    (a) on met en contact ledit courant résiduaire (1) avec un premier courant gazeux riche en hydrogène (10) ayant une température supérieure à celle du courant résiduaire (1), dans une zone d'évaporation flash (2) avec des conditions d'évaporation flash, de façon à accroître ainsi la température dudit courant résiduaire et d'évaporer au moins une partie de celui-ci pour produire un courant de vapeur (3) comprenant de l'hydrogène et des composés hydrocarbonés, et un courant de produit lourd (4) comprenant ledit composant non distillable ;
    caractérisé en ce qu'on effectue immédiatement les étapes consistant :
    (b) à mettre en contact ledit courant de vapeur (3) avec un catalyseur d'hydrogénation dans une zone réactionnelle d'hydrogénation (5) dans des conditions d'hydrogénation, afin d'accroître le degré d'hydrogénation des composés hydrocarbonés contenus dans celui-ci ;
    (c) à condenser au moins une partie de l'effluent résultant (6) issu de la zone réactionnelle d'hydrogénation (5), pour former un deuxième courant gazeux riche en hydrogène (10) et un courant liquide (14) comprenant un gaz combustible et des composés hydrocarbonés hydrogénés distillables ; et
    (d) à récupérer à partir du courant liquide (14), un courant de produit hydrocarboné hydrogéné distillable (16) et un courant de gaz combustible (17) ; et
    (e) à chauffer au moins une partie de ce deuxième courant gazeux riche en hydrogène (10) récupéré dans l'étape (c) et à recycler le courant chauffé résultant dans l'étape (a).
  2. Procédé selon la revendication 1, caractérisé en ce que le courant hydrocarboné résiduaire sensible à la température comprend (1) un fluide diélectrique, un fluide hydraulique, un fluide de transfert de chaleur, une huile lubrifiante usée, une huile de coupe usée, un solvant usé, des résidus de distillation issus d'une opération de recyclage de solvant, du goudron de houille, un résidu de distillation atmosphérique, une huile souillée avec du biphényle polychloré, un résidu halogéné ou un autre résidu industriel hydrocarboné, et en ce que le composant non distillable comprend un composé organométallique, un composé métallique inorganique, des particules finement divisées ou un composé hydrocarboné non distillable.
  3. Procédé selon la revendication 1 ou 2, caractérisé en ce que le courant hydrocarboné résiduaire sensible à la température (1) est introduit dans ladite zone de séparation flash (2) à une température inférieure à 482 °F (250 °C), et en ce que la température du premier courant chaud riche en hydrogène (10) est de 200 à 1 200 °F (93 à 649 °C).
  4. Procédé selon l'une quelconque des revendications 1 à 3, caractérisé en ce que les conditions de séparation flash comprennent une température de 150 à 860 °F (65 à 460 °C), une pression allant de la pression atmosphérique jusqu'à 2 000 psig (pression relative : 13 788 kPa), un débit de circulation d'hydrogène de 1 000 SCFB jusqu'à 30 000 SCFB (de 168 à 5 056 m³ dans les conditions normales/m³) par rapport au courant hydrocarboné résiduaire sensible à la température, et un temps de séjour moyen du courant en phase vapeur dans la zone de séparation flash (2) de 0,1 à 50 secondes.
  5. Procédé selon l'une quelconque des revendications 1 à 4, caractérisé en ce que la zone réactionnelle d'hydrogénation (5) est mise en oeuvre dans des conditions comprenant une pression allant de la pression atmosphérique jusqu'à 2 000 psig (pression relative : de 0 à 13 790 kPa), une température maximum de catalyseur allant de 122 à 850 °F (de 50 à 454 °C), et un débit de circulation d'hydrogène de 200 à 50 000 SCFB (de 33,7 à 8 427 m³ dans les conditions normales/m³).
  6. Procédé selon l'une quelconque des revendications 1 à 5, caractérisé en ce que le catalyseur d'hydrogénation comprend un oxyde inorganique réfractaire, et au moins un composé ayant une activité d'hydrogénation, d'un métal du groupe VI-B ou VIII du tableau périodique.
  7. Procédé selon l'une quelconque des revendications 1 à 6, dans lequel on produit au moins un composé inorganique soluble dans l'eau dans la zone réactionnelle d'hydrogénation (5), caractérisé en ce que l'effluent (6) issu de la zone d'hydrogénation (5) contenant des composés hydrocarbonés hydrogénés et au moins un composé inorganique soluble dans l'eau, est mis en contact avec une solution aqueuse d'épuration fraîche (7) ; et en ce que l'on fait passer le mélange effluent résultant (6) et la solution d'épuration (7), dans une zone de séparation (9), pour obtenir un deuxième courant gazeux riche en hydrogène (10), un premier courant liquide (14) comprenant un gaz combustible et des composés hydrocarbonés hydrogénés distillables, et une solution aqueuse d'épuration usée (13) contenant au moins une partie du composé inorganique soluble dans l'eau.
  8. Procédé selon la revendication 7, caractérisé en ce que le composé inorganique soluble dans l'eau, est le sulfure d'hydrogène, l'ammoniac, le chlorure d'hydrogène, le bromure d'hydrogène, ou le fluorure d'hydrogène et en ce que la solution d'épuration comprend de l'hydroxyde de calcium, de l'hydroxyde de potassium ou de l'hydroxyde de sodium.
  9. Procédé selon l'une quelconque des revendications 1 à 8, caractérisé en ce que l'on emploie un liquide supplémentaire pour purger les composants non distillables lourds à partir de la zone de séparation flash.
EP88307448A 1987-08-13 1988-08-11 Hydrogénation d'un courant d'hydrocarbures usés sensibles à la température Expired - Lifetime EP0306164B1 (fr)

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Application Number Priority Date Filing Date Title
US8495487A 1987-08-13 1987-08-13
US84954 1987-08-13

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EP0306164A1 EP0306164A1 (fr) 1989-03-08
EP0306164B1 true EP0306164B1 (fr) 1992-10-14

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EP88307448A Expired - Lifetime EP0306164B1 (fr) 1987-08-13 1988-08-11 Hydrogénation d'un courant d'hydrocarbures usés sensibles à la température

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AU (1) AU613714B2 (fr)
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US5141629A (en) * 1990-05-15 1992-08-25 State Of Israel, Atomic Energy Commission Process for the dehalogenation of organic compounds
US5013424A (en) * 1990-07-30 1991-05-07 Uop Process for the simultaneous hydrogenation of a first feedstock comprising hydrocarbonaceous compounds and having a non-distillable component and a second feedstock comprising halogenated organic compounds
US5490919A (en) * 1990-08-14 1996-02-13 State Of Isreal, Atomic Energy Commission Process for the dehalogenation of organic compounds
US5314614A (en) * 1992-06-17 1994-05-24 Uop Process for hydrotreating an organic feedstock containing olefinic compounds and a halogen component
US5397459A (en) * 1993-09-10 1995-03-14 Exxon Research & Engineering Co. Process to produce lube oil basestock by low severity hydrotreating of used industrial circulating oils
ES2626658T5 (es) 2011-01-18 2021-01-26 Neste Oyj Método y disposición para alimentar materiales sensibles al calor a reactores de lecho fijo
CN107574012B (zh) * 2017-10-16 2021-03-12 河北金谷再生资源开发有限公司 一种废润滑油再生基础油的制备方法
CN112940832A (zh) * 2021-02-01 2021-06-11 国家能源集团宁夏煤业有限责任公司 煤基抗磨液压油及其制备方法

Citations (1)

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EP0301758A1 (fr) * 1987-07-23 1989-02-01 Uop Traitement d'un courant d'hydrocarbures usés sensible à la température, contenant une partie non distillable

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CA1107673A (fr) * 1977-05-16 1981-08-25 Gerhard P. Nowack Recyclage des huiles lubrifiantes epuisees
US4265733A (en) * 1979-11-01 1981-05-05 Phillips Petroleum Company De-ashing lubricating oils
DE3637255A1 (de) * 1986-11-03 1988-05-05 Metallgesellschaft Ag Verfahren zum aufarbeiten von altoel

Patent Citations (1)

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Publication number Priority date Publication date Assignee Title
EP0301758A1 (fr) * 1987-07-23 1989-02-01 Uop Traitement d'un courant d'hydrocarbures usés sensible à la température, contenant une partie non distillable

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ES2035302T3 (es) 1993-04-16
DE3875314D1 (de) 1992-11-19
DE3875314T2 (de) 1993-02-25
EP0306164A1 (fr) 1989-03-08
AU613714B2 (en) 1991-08-08
AU3070189A (en) 1990-08-30

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