EP1242565B1 - Procede de distillation court-terme douce d'huiles residuelles - Google Patents

Procede de distillation court-terme douce d'huiles residuelles Download PDF

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Publication number
EP1242565B1
EP1242565B1 EP00987253A EP00987253A EP1242565B1 EP 1242565 B1 EP1242565 B1 EP 1242565B1 EP 00987253 A EP00987253 A EP 00987253A EP 00987253 A EP00987253 A EP 00987253A EP 1242565 B1 EP1242565 B1 EP 1242565B1
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EP
European Patent Office
Prior art keywords
coke
mixer
residual oil
stirred tank
heat
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
Application number
EP00987253A
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German (de)
English (en)
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EP1242565A1 (fr
Inventor
Hans-Jürgen WEISS
Ingo Dreher
Udo Zentner
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MG Technologies AG
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MG Technologies AG
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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
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/16—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form
    • C10B49/20—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form in dispersed form
    • 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)
    • 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
    • C10G9/28—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid material

Definitions

  • the invention relates to a method for gentle Short-term distillation of a residual oil from the Processing of petroleum, natural bitumen or oil sand, where the residual oil with granular, hot coke as Heat transfer medium (heat transfer coke) in a mixing plant in the Weight ratio of 1: 3 to 1:30 mixes and through the Mixing process in the mixer on the grains of the heat transfer coke initially forms a liquid residue film that partially evaporated in the mixer. The gases formed and Vapors are withdrawn from the mixer.
  • Heat transfer coke Heat transfer medium
  • the invention has for its object the known Develop processes further and cost-effectively the highest possible product oil yield in the best possible way To produce quality. According to the invention, this is achieved by that the coke-residue oil mixture formed in the mixer conducts into a downstream stirring pot, in which the mixture adds with mechanical stirring a temperature of 450 to 600 ° C and preferably at 480 to 550 ° C slowly downwards, and that one from the Stirring pot of dry, free-flowing coke. This free-flowing coke is largely free of liquid Residual oil and therefore has a good flow behavior.
  • the residence times are Heat transfer coke in the mixer is usually between 1 and 120 Seconds and in the stirring pot at 1 to 30 minutes.
  • This Mixer can be built with a relatively short length, so that the residence times of the gases and vapors in the mixing plant are desirably short and are usually 0.5 to 5 Seconds.
  • the subsequent stirring pot is given coke-containing ones Solids from the mixer that are still damp and are sticky.
  • the content of residual oil in the mixture is placed in the stirring pot, is still 5 to 90 wt.% And mostly 10 to 70% by weight of the feed to the mixer Amount of residual oil.
  • the mixing bowl in which the Moving solids down gradually can be a single Have agitator shaft or several agitator shafts.
  • the Mixing promotes the deduction of the released Gases and vapors that are extracted from the mixing bowl and as well as the gases withdrawn from the mixer and Vapors condenses.
  • the mixer (1) of Fig. 1 leads through the line (2) are called heat transfer coke and through line (3) residual oil to be processed.
  • the heat transfer coke has temperatures in the range of 500 to 700 ° C, and one leads the mixer (1) heat transfer coke and Residual oil in a weight ratio of 3: 1 to 30: 1 too.
  • the Mixer (1) has several in the present case horizontal, interlocking snails on as it is is known. Stand in the mixer (1) Temperatures in the range of 450 to 600 ° C and mostly 480 up to 550 ° C. Formed gases and vapors leave it Mixing unit (1) after a short dwell time in the range of 0.5 to 5 sec through the drain channel (5) and are in a Condensation (6) performed. One draws from this condensation separated gases through line (7) and crude product oil through line (8), which one is not can perform further treatment shown.
  • a mechanical Cleaning device (11) e.g. snail, scraper
  • the solid / residual oil mixture is stirred mechanically as it moves downward, the temperatures being kept in the range from 450 to 600 ° C. and mostly in the range from 480 to 550 ° C.
  • the residence times of the solids in the stirring pot are in the range from 1 to 30 minutes and are preferably at least 3 minutes. This means that you can work in the mixing bowl at the lowest possible temperatures to convert the residual oil to oil vapor, gas and coke.
  • gases and vapors formed flow upward through the channel (10) and reach the condensation (6) through the discharge channel (5) together with the gases and vapors from the mixer (1).
  • a stripping gas e.g. water vapor, C 4 hydrocarbon gas or nitrogen
  • a partial flow of 1 to 30 wt .-%, based on the total amount of distillation fed Heat transfer coke can be reached through line (4) of the mixer (1).
  • This additional heat transfer coke is then particularly effective in the solid mixture, which one leads into the stirring pot (12).
  • the coke residue oil mixture can be coke fed in
  • stir the mixing bowl which is the conversion of the the residual oil in the coke accelerates.
  • the Z axis gives the percentage (% by weight) different pollutants in the product oil, based on the Initial content in the treated residual oil, namely for Sulfur (S), nitrogen (N), Conradson residue (CCR) and the sum of nickel and vanadium (Ni + V).
  • 10 t per hour of a vacuum residue formed during the distillation of crude oil are injected into the mixer (1) at 330 ° C. and mixed with 80 t / h of heat transfer coke at 570 ° C.
  • the vacuum residue contains 20% by weight CCR, 3% by weight sulfur, 200 mg / kg vanadium and 100 mg / kg nickel.
  • a reaction temperature of 500 ° C is set in the mixer.
  • the still oil-containing heat transfer coke is thrown out of the mixer into a stirring pot (12) after approx. 30 seconds.
  • the residual oil content is still 25% by weight, based on the amount of residue supplied.
  • the mixture is reacted within a further 5 minutes to dry coke (1.2 t / h) as well as oil vapor and gas.
  • the mixture of oil vapor and gas is drawn off through the channels (10) and (5) and fed to a condensation (6).
  • 2 and 3 8.3 t / h of product oil (C 5+ ) with 4% by weight CCR, 2.1% by weight S, 7 mg / kg V and 3.5 mg / kg Ni fall and 500 kg / h of gas (C 4- ).
  • the heat transfer coke (80 t / h) and the freshly formed coke on its surface are largely removed from the mixing pot free of liquid components and thus dry and free-flowing.

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

Claims (5)

  1. Procédé de distillation ménagée pendant une durée courte d'une huile résiduelle provenant du traitement du pétrole, du bitume naturel ou du sable pétrolifère, dans lequel on mélange l'huile résiduelle à du coke chaud en grains servant d'agent caloporteur (coke caloporteur) dans un mélangeur, en un rapport en poids de 1:3 à 1:30, et on forme par l'opération de mélange dans le mélangeur sur les grains du coke caloporteur d'abord une pellicule liquide de résidu qui s'évapore en partie dans le mélangeur, on soutire les gaz et les vapeurs formés du mélangeur et on soutire du mélangeur du coke humide et collant, caractérisé en ce que l'on envoie ce mélange de coke et d'huile résiduelle dans un pot de brassage en aval, dans lequel le mélange est déplacé lentement vers le bas sous brassage mécanique à une température de 450 à 600°C, de préférence de 480 à 550°C, et on soutire du coke sec et susceptible de s'écouler du pot de brassage.
  2. Procédé suivant la revendication 1, caractérisé en ce que la durée de séjour du coke caloporteur dans le mélangeur est comprise entre 1 et 120 secondes.
  3. Procédé suivant la revendication 1, caractérisé en ce que la durée de séjour du coke caloporteur dans le pot de brassage est comprise entre 1 et 30 minutes.
  4. Procédé suivant la revendication 1 ou 2, caractérisé en ce que l'on ajoute du coke caloporteur frais au mélange contenant du coke que l'on envoie avec une teneur résiduelle en huile résiduelle de 5 à 90 % en poids, rapportée à la quantité d'huile résiduelle chargée dans le mélangeur, dans le pot de brassage.
  5. Procédé suivant la revendication 1 ou l'une des suivantes, caractérisé en ce que le conduit entre le mélangeur et le pot de brassage comporte un dispositif mécanique de nettoyage.
EP00987253A 1999-12-10 2000-11-16 Procede de distillation court-terme douce d'huiles residuelles Expired - Lifetime EP1242565B1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE19959587A DE19959587B4 (de) 1999-12-10 1999-12-10 Verfahren zur schonenden Kurzzeit-Destillation von Rückstandsölen
DE19959587 1999-12-10
PCT/EP2000/011320 WO2001042394A1 (fr) 1999-12-10 2000-11-16 Procede de distillation court-terme douce d'huiles residuelles

Publications (2)

Publication Number Publication Date
EP1242565A1 EP1242565A1 (fr) 2002-09-25
EP1242565B1 true EP1242565B1 (fr) 2003-05-28

Family

ID=7932145

Family Applications (1)

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EP00987253A Expired - Lifetime EP1242565B1 (fr) 1999-12-10 2000-11-16 Procede de distillation court-terme douce d'huiles residuelles

Country Status (11)

Country Link
US (1) US6841064B1 (fr)
EP (1) EP1242565B1 (fr)
JP (1) JP4741136B2 (fr)
AT (1) ATE241683T1 (fr)
AU (1) AU2357401A (fr)
CA (1) CA2394256C (fr)
DE (2) DE19959587B4 (fr)
ES (1) ES2197891T3 (fr)
MX (1) MXPA02005168A (fr)
SA (1) SA00210351B1 (fr)
WO (1) WO2001042394A1 (fr)

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DE10259450B4 (de) * 2002-12-19 2006-08-10 Lurgi Lentjes Ag Verfahren zur Hochtemperatur-Kurzzeit-Destillation von Rückstandsöl
DE10321350B4 (de) * 2003-05-13 2005-04-21 Lurgi Ag Mischvorrichtung
ITMI20071044A1 (it) 2007-05-23 2008-11-24 Eni Spa Sistema e procedimento per l'idroconversione di oli pesanti
GB0808739D0 (en) 2008-05-14 2008-06-18 Univ Aston Thermal treatment of biomass
US9249265B1 (en) 2014-09-08 2016-02-02 Sirrus, Inc. Emulsion polymers including one or more 1,1-disubstituted alkene compounds, emulsion methods, and polymer compositions
US9279022B1 (en) 2014-09-08 2016-03-08 Sirrus, Inc. Solution polymers including one or more 1,1-disubstituted alkene compounds, solution polymerization methods, and polymer compositions
US10414839B2 (en) 2010-10-20 2019-09-17 Sirrus, Inc. Polymers including a methylene beta-ketoester and products formed therefrom
US8884051B2 (en) 2010-10-20 2014-11-11 Bioformix Inc. Synthesis of methylene malonates using rapid recovery in the presence of a heat transfer agent
US9828324B2 (en) 2010-10-20 2017-11-28 Sirrus, Inc. Methylene beta-diketone monomers, methods for making methylene beta-diketone monomers, polymerizable compositions and products formed therefrom
MX360463B (es) 2011-10-19 2018-11-05 Sirrus Inc Monomeros de beta-cetoester de metileno, procedimientos de fabricación de monomeros de beta-cetoester de metileno, composiciones polimerizables y productos formados a partir de las mismas.
CA2869108A1 (fr) 2012-03-30 2013-10-03 Bioformix Inc. Procedes d'activation de compositions polymerisables, systemes polymerisables, et produits formes
JP6345644B2 (ja) 2012-03-30 2018-06-20 シラス・インコーポレイテッド インク配合物およびコーティング配合物ならびにこれらを作製するための重合性の系
EP3153530B1 (fr) 2012-03-30 2021-02-24 Sirrus, Inc. Articles composites et laminés et systèmes polymérisables pour leur production
US10047192B2 (en) 2012-06-01 2018-08-14 Sirrus, Inc. Optical material and articles formed therefrom
WO2014078689A1 (fr) 2012-11-16 2014-05-22 Bioformix Inc. Systèmes et procédés de liaison de matières plastiques
US10607910B2 (en) 2012-11-30 2020-03-31 Sirrus, Inc. Composite compositions for electronics applications
EP2943462B1 (fr) 2013-01-11 2018-06-27 Sirrus, Inc. Procédé d'obtention de malonate de méthylène par l'intermédiaire de la voie du bis(hydroxyméthyl)malonate
US9315597B2 (en) 2014-09-08 2016-04-19 Sirrus, Inc. Compositions containing 1,1-disubstituted alkene compounds for preparing polymers having enhanced glass transition temperatures
US9416091B1 (en) 2015-02-04 2016-08-16 Sirrus, Inc. Catalytic transesterification of ester compounds with groups reactive under transesterification conditions
US10501400B2 (en) 2015-02-04 2019-12-10 Sirrus, Inc. Heterogeneous catalytic transesterification of ester compounds with groups reactive under transesterification conditions
US9334430B1 (en) 2015-05-29 2016-05-10 Sirrus, Inc. Encapsulated polymerization initiators, polymerization systems and methods using the same
US9217098B1 (en) 2015-06-01 2015-12-22 Sirrus, Inc. Electroinitiated polymerization of compositions having a 1,1-disubstituted alkene compound
US9518001B1 (en) 2016-05-13 2016-12-13 Sirrus, Inc. High purity 1,1-dicarbonyl substituted-1-alkenes and methods for their preparation
US9617377B1 (en) 2016-06-03 2017-04-11 Sirrus, Inc. Polyester macromers containing 1,1-dicarbonyl-substituted 1 alkenes
US9567475B1 (en) 2016-06-03 2017-02-14 Sirrus, Inc. Coatings containing polyester macromers containing 1,1-dicarbonyl-substituted 1 alkenes
US10428177B2 (en) 2016-06-03 2019-10-01 Sirrus, Inc. Water absorbing or water soluble polymers, intermediate compounds, and methods thereof
US10196481B2 (en) 2016-06-03 2019-02-05 Sirrus, Inc. Polymer and other compounds functionalized with terminal 1,1-disubstituted alkene monomer(s) and methods thereof
CA3195665A1 (fr) * 2020-10-16 2022-04-21 Giuseppe FALCO Appareil destine au traitement des matieres plastiques

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Also Published As

Publication number Publication date
CA2394256C (fr) 2007-03-27
DE19959587A1 (de) 2001-06-13
SA00210351B1 (ar) 2006-09-04
ES2197891T3 (es) 2004-01-16
EP1242565A1 (fr) 2002-09-25
CA2394256A1 (fr) 2001-06-14
ATE241683T1 (de) 2003-06-15
JP4741136B2 (ja) 2011-08-03
DE50002404D1 (de) 2003-07-03
DE19959587B4 (de) 2006-08-24
JP2003516463A (ja) 2003-05-13
AU2357401A (en) 2001-06-18
MXPA02005168A (es) 2003-09-25
WO2001042394A1 (fr) 2001-06-14
US6841064B1 (en) 2005-01-11

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