EP0049324B1 - Procédé et appareil pour la semi-cokéfaction de schiste bitumineux - Google Patents

Procédé et appareil pour la semi-cokéfaction de schiste bitumineux Download PDF

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Publication number
EP0049324B1
EP0049324B1 EP81104562A EP81104562A EP0049324B1 EP 0049324 B1 EP0049324 B1 EP 0049324B1 EP 81104562 A EP81104562 A EP 81104562A EP 81104562 A EP81104562 A EP 81104562A EP 0049324 B1 EP0049324 B1 EP 0049324B1
Authority
EP
European Patent Office
Prior art keywords
distillation
gas
reactor
oil shale
smoldering
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
EP81104562A
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German (de)
English (en)
Other versions
EP0049324A1 (fr
Inventor
Gerd Dr. Escher
Heinz Frohnert
Hans-Peter Wenning
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.)
Veba Oel Technologie und Automatisierung GmbH
Original Assignee
Veba Oel Technologie und Automatisierung GmbH
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Publication date
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Publication of EP0049324A1 publication Critical patent/EP0049324A1/fr
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Publication of EP0049324B1 publication Critical patent/EP0049324B1/fr
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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
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
    • 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
    • C10B49/02—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 hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
    • C10B49/04—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 hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
    • C10B49/08—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 hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form
    • 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
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/06—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of oil shale and/or or bituminous rocks

Definitions

  • GB-A 668 808 describes a process for smoldering oil shale with a hot gas in a shaft furnace, the condensable constituents being separated from the smoldering gas, a proportion of the smoldering gas corresponding to the increase in the gas quantity being removed and the rest after heating up in the smoldering reactor is returned.
  • the solid, still carbon-containing smoldering residue introduces an oxygen-containing gas, in particular air, into another part of the shaft furnace separated from the smoldering part in order to burn part of the carbon and to increase the temperature of the residue.
  • the cooled, de-condensable gas is passed through the residue heated in this way, in order to heat it up again, whereupon it flows in countercurrent through the smoldering part of the smoldering furnace, where it causes the oil shale to smolder, and is then passed through fresh oil shale so that the oil contained in it after condensation at least partially condenses.
  • the shaft furnace principle can no longer be used for finely shredded goods.
  • Other methods using fines such as US-A 3 844 930 work with solids as heat carriers.
  • the amount of solids to be handled is further increased by the amount of heat transfer medium which is a multiple of the amount of shale used.
  • the carbonization gas mixed with the carrier gases is separated from the solids - heat transfer particles and carbonization residue.
  • the smoldering gases are produced in dilution by the carrier gases, which makes their work-up more difficult.
  • the smoldering residue leaves the cyclone in a mixture with the solid heat transfer media, so that larger amounts of ballast must also be carried along during its further processing.
  • the smoldering temperatures are generally above 450 ° C and should not exceed 650 ° C, otherwise the reduction in yield due to cracking reactions cannot be avoided despite the short smoldering times. Temperatures between 470 and 550 ° C. are preferred.
  • the attached Fig. 1 shows the yields in the cyclone swelling of a Schandelah oil shale compared to the yields according to the Fischer test.
  • the oil shale used contained 10.3% by weight of organic carbon and had the following Fischer test yields:
  • the carbonization gas is preheated to temperatures which are 150 to 250 K above the carbonization temperature.
  • This overheating depends on the ratio of carbonization gas to oil shale, which is usually between 0.8 and 1.4 Nm 3 / kg, preferably between 1.0 and 1.2 Nm 3 / kg lies on the temperature of the slate used, on the residual moisture, on the carbonate decomposition of the carbonates contained, and on the heat losses of the system.
  • coarser feed material can be used in the method according to the invention than in the known method. Oil shale with a grain size of up to 3 mm, even up to 5 mm, can be used. These coarse-grained slates have the advantage of containing less dust, which considerably facilitates both the processing of the carbonization gas and the further treatment of the carbonization residue.
  • the condensable components are separated from the carbonization gas by cooling it directly with cold oil, possibly with subsequent electrostatic precipitation of the oil mist.
  • deposition by means of electrofiltration has proven to be particularly expedient. This is quite surprising, because it was not to be expected that the high temperatures of more than 450 ° C would allow electrofiltration of the carbonization gases, since the electrical field would collapse in a reducing atmosphere without the presence of sulfuric vapors.
  • the smoldering residue is withdrawn from the cyclone reactor; its carbon is expediently burned with oxygen-containing gases, in particular air, it being possible for the hot combustion gas to be used for preheating the circulating carbonization gas.
  • the carbon of the carbonization residue is expediently burned with oxygen-containing gases in a fluidized bed.
  • the combustion conditions must be set so that S0 2 produced during combustion is integrated into the residue due to dolomite and calcite which may be found in the shale.
  • the smoldering residue discharged from the smoldering cyclone reactor can first be degassed in a container before its carbon is burned with oxygen-containing gases.
  • smoldering gas can be passed through for faster removal of the gases still present, it being expedient to loosen up the smoldering residue with stirrers or to shift it in a rotating drum.
  • the known device in which the gas discharge of the smoldering reactor is connected to an oil separator and the inlet connector of the smoldering reactor is connected to the oil separator via a blower, has a cyclone reactor with a tangential inlet connector and a heat exchanger between the blower and the tangential inlet connector of the smoldering cyclone reactor for carrying out the method according to the invention .
  • a preheater for the oil shale to be smoldered is preferably provided in front of the tangential inlet connection of the smoldering cyclone reactor.
  • a dust separator operating at temperatures of the dew point of the carbonization gases in particular an electrostatic filter, is arranged between the carbonization cyclone reactor and the oil separator.
  • the solids discharge of the smoldering cyclone reactor is connected to a combustion furnace and its hot gas outlet is connected to the heat exchanger provided for heating the smoldering gas serving as carrier gas. It has also proven to be expedient to provide a post-carbonization drum on the solid discharge port of the smoldering cyclone reactor or between this discharge port and the combustion device for smoldering residue.
  • a device according to the invention is shown schematically in the attached FIG. 3.
  • the method according to the invention is explained on the basis of this:
  • the oil shale 1 is comminuted to a grain size of less than 3 mm.
  • the comminution and screening is expediently carried out together with the drying and preheating in a mill dryer 2, for which purpose the flue gases 3 are used after the cycle gas preheater 4.
  • the cooled flue gas is discharged via line 5.
  • the crushed, dried and preheated oil shale 6 to approx. 110 ° C is mixed in the riser 7 with circulating hot gas 8, a substantial part of the heat being transferred from the heating gas to the slate in the riser pipe, and this mixture via the tangential feed 9 in led the smoldering cyclone 10.
  • the oil and dust-containing carbonization gases leave the carbonization cyclone 10 via line 11, while the carbonization residue is fed via line 12 into a re-carbonation drum 13.
  • part of the hot recycle gas is passed through line 14 into the re-carbonation drum 13.
  • the smoldering and cycle gas 15 from the after-carbonization 13 is led together with the smoldering gases 11 from the smoldering cyclone into a dedusting system 16.
  • the separated dust is fed via line 17 into the post-carbon drum 13.
  • the dedusted gas passes through the pipeline 18 into the oil separator 19, where it is freed of the condensable fractions which are supplied as product via the line 20 to the further processing.
  • From the oil separation 19, a part of the smoldering gas corresponding to the amount of gas obtained during the pre-carbonization is likewise produced as a product via the line 21 dissipated.
  • the remaining carbonization gas is fed via line 22 to the compressor 23 and, after compression through line 24, reaches the cycle gas preheater 4.
  • the hot smoldering residue 25 behind the post-carbonization drum 13 is fed to a fluidized bed incinerator 26, in which the residual carbon is burned off.
  • the temperature control for setting the optimal SO 2 integration is carried out by the heat exchanger 27 in the fluidized bed, which is designed as a steam generator.
  • the hot flue gas leaves the fluidized bed furnace via line 28.
  • the heat content of this gas is used in the cycle gas heat exchanger 4 for smoldering and in mill drying 2 for drying and preheating the oil shale.
  • the burned-off oil shale from the fluidized bed furnace is fed through line 29 to a cooler 30 and leaves the cooler via line 31.
  • the combustion air 32 which is compressed in the compressor 33, is led via line 34 to the cooler 30 and via the line 35 reaches the fluidized bed furnace 26.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Dispersion Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Claims (15)

1. Procédé pour la distillation lente d'un schiste bitumeux ou huileux, dans un réacteur de distillation, à l'aide d'un gaz chaud, où les fractions condensables sont séparées du gaz de distillation, un volume partiel correspondant à l'augmentation du volume dû à la formation de gaz au cours de la distillation lente est éliminé, et le reste est à nouveau réchauffé et recyclé dans le réacteur de distillation, procédé caractérisé en ce que l'on utilise un réacteur à cyclone, réchauffe indirectement le gaz de distillation, et le recycle dans le réacteur de distillation à cyclone comme fluide unique caloporteur.
2. Procédé suivant la revendication 1, caractérisé en ce que le schiste huileux est séché et préchauffé à une température inférieure à la température de distillation lente, avant son introduction dans le courant de gaz de distillation recyclé.
3. Procédé suivant l'une des revendications 1 et 2, caractérisé en ce que le schiste huileux soumis à la distillation lente possède une granulométrie pouvant aller jusqu'à 5 mm.
4. Procédé selon l'une quelconque des revendications 1 à 3, caractérisé en ce que l'on sépare les poussières du gaz de distillation lente à une température supérieure au point de rosée des constituants condensables.
5. Procédé selon la revendication 4, caractérisé en ce que le dépoussiérage est effectué par électro- filtration.
6. Procédé suivant l'une quelconque des revendications 1 à 5, caractérisé en ce que le carbone contenu dans le résidu de distillation est brûlé dans un mélange gazeux contenant de l'oxygène, et le gaz de combustion ainsi formé est employé, en totalité ou en partie, pour le pré-chauffage du gaz de distillation lente à recycler.
7. Procédé suivant l'une quelconque des revendications 1 à 6, caractérisé en ce que le gaz de combustion, après avoir servi au pré-chauffage du gaz de distillation à recycler, est utilisé pour le séchage et le pré-chauffage du schiste à traiter.
8. Procédé suivant l'une quelconque des revendications 1 à 7, caractérisé en ce que le résidu de distillation évacué du réacteur de distillation lente à cyclone est maintenu dans un réservoir à la température de distillation.
9. Procédé suivant la revendication 8, caractérisé en ce que l'on fait passer du gaz de distillation, dont ont été séparés les composants condensables, à travers le résidu de distillation maintenu en agitation par des agitateurs ou un tambour rotatif.
10. Installation pour la réalisation du procédé selon l'une quelconque des revendications 1 à 9, où le conduit d'évacuation des gaz d'un réacteur de distillation (10) est relié à un séparateur d'huile (19) et les tuyaux d'alimentation du réacteur de distillation (10) sont reliés au séparateur d'huile en passant par un compresseur (23) de gaz, installation caractérisée en ce que le réacteur (10) est un réacteur à cyclone avec des tuyaux d'alimentation (9) tangentiels et qu'il est disposé un échangeur de chaleur (4) entre le compresseur de gaz et les tuyaux d'alimentation (9) tangentiels du réacteur de distillation à cyclone.
11. Installation suivant la revendication 10, caractérisée en ce qu'elle comprend une installation de pré-chauffage (2) du schiste à traiter en amont du tuyau d'alimentation tangentiel (9) duréacteur à cyclone (10).
12. Installation selon l'une des revendications 10 et 11, caractérisée en ce qu'un séparateur de poussières (16) fonctionnant à une température supérieure au point de rosée du gaz de distillation est intercalé entre le réacteur de distillation à cyclone (10) et le séparateur d'huile (19).
13. Installation suivant l'une quelconque des revendications 10 à 12, caractérisée en ce que le conduit d'évacuationdes matières solides (12) du réacteur à cyclone (10) est connecté à un four de combustion (26).
14. Installation selon l'une quelconque des revendications 10 à 13, caractérisée en ce que le conduit d'évacuation des matières solides (12) du réacteur à cyclone (10) est relié à un four de combustion (26), et le conduit d'évacuation des gaz chauds du réacteur est relié à l'échangeur de chaleur (4).
15. Installation selon l'une quelconque des revendications 10 à 14, caractérisée en ce qu'un tambour de post-distillation (13) est prévu sur le conduit d'évacuation des matières solides (12) du réacteur de distillation à cyclone (10), ou entre ce conduit (12) et le four de combustion (26) prévu pour le résidu de distillation.
EP81104562A 1980-06-25 1981-06-13 Procédé et appareil pour la semi-cokéfaction de schiste bitumineux Expired EP0049324B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3023670 1980-06-25
DE3023670A DE3023670C2 (de) 1980-06-25 1980-06-25 Verfahren und Vorrichtung zum Schwelen von Ölschiefer

Publications (2)

Publication Number Publication Date
EP0049324A1 EP0049324A1 (fr) 1982-04-14
EP0049324B1 true EP0049324B1 (fr) 1984-09-12

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ID=6105369

Family Applications (1)

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EP81104562A Expired EP0049324B1 (fr) 1980-06-25 1981-06-13 Procédé et appareil pour la semi-cokéfaction de schiste bitumineux

Country Status (9)

Country Link
US (1) US4388173A (fr)
EP (1) EP0049324B1 (fr)
AU (1) AU545951B2 (fr)
BR (1) BR8103968A (fr)
DE (2) DE3023670C2 (fr)
ES (1) ES8207580A1 (fr)
JO (1) JO1113B1 (fr)
MA (1) MA19167A1 (fr)
YU (1) YU42719B (fr)

Families Citing this family (10)

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BR8302810A (pt) * 1983-05-27 1985-01-15 Petroleo Brasileiro Sa Processo para a retornagem de solidos contendo hidrocarbonetos
DE3323770A1 (de) * 1983-07-01 1985-01-03 Metallgesellschaft Ag, 6000 Frankfurt Verfahren zum trocknen und erhitzen von oelhaltigen feststoffen
US4585543A (en) * 1984-03-09 1986-04-29 Stone & Webster Engineering Corp. Method for recovering hydrocarbons from solids
US4601812A (en) * 1985-01-07 1986-07-22 Conoco Inc. Oil shale retorting process
DE3715158C1 (de) * 1987-05-07 1988-09-15 Veba Oel Entwicklungs Gmbh Verfahren zur Gewinnung von Schweloel
GB2276631A (en) * 1993-02-24 1994-10-05 Great Eastern Process for removal of petroleum contaminants from particulate materials
CA2546940C (fr) * 2006-05-15 2010-09-21 Olav Ellingsen Processus de recuperation et de craquage/d'amelioration simultanes du petrole a partir de materiaux solides
US10030199B2 (en) * 2007-11-23 2018-07-24 Bixby Energy Systems, Inc. Pyrolisis apparatus
US9795972B2 (en) 2012-08-07 2017-10-24 Cameron International Corporation High temperature high pressure electrostatic treater
CN104745221B (zh) * 2015-04-01 2016-04-27 曲靖众一精细化工股份有限公司 一种细、小颗粒干馏油气高品质回收方法及其回收装置

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US2414586A (en) * 1942-09-05 1947-01-21 Universal Oil Prod Co Distillation of hydrocarbonaceous solids
US2434567A (en) * 1944-01-19 1948-01-13 Standard Oil Dev Co Method and apparatus for contacting hydrocarbons with catalyst particles
GB668808A (en) * 1949-09-17 1952-03-19 California Research Corp Process for retorting shale
DE1160823B (de) * 1954-10-14 1964-01-09 Kloeckner Humboldt Deutz Ag Verfahren zum kontinuierlichen Entgasen, wie Schwelen und/oder Verkoken, von feinkoernigen, nicht backenden, wasserhaltigen Brennstoffen mittels heisser Gasstroeme
US2942043A (en) * 1955-01-03 1960-06-21 Hoechst Ag Process for carrying out endothermic chemical reactions
US3475319A (en) * 1966-12-22 1969-10-28 Exxon Research Engineering Co Retorting of oil shale
DE1809874B2 (de) * 1968-11-20 1974-10-31 Metallgesellschaft Ag, 6000 Frankfurt Vorrichtung zur trockenen Destillation von bituminösen oder ölhaltigen, feinkörnigen Materialien zwecks Gewinnung von flüssigen Kohlenwasserstoffen
US3577338A (en) * 1969-02-19 1971-05-04 Phillip H Gifford Process for recovery of oil from oil shale simultaneously producing hydrogen
GB1326455A (en) * 1971-01-26 1973-08-15 Texaco Development Corp Hydrotorting of shale to produce shale oil
BR7105857D0 (pt) * 1971-09-06 1973-04-10 Brasileiros Sa Petrob Petroleo Processo aprefeicoado para obtencao de oleo gas e subprodutos de xisto pirobetuminosos ou outros materiais impregnados com hidrocarbonetos
DE2244753B1 (de) * 1972-09-08 1973-10-18 Mannesmann Ag, 4000 Duesseldorf Verfahren und Vorrichtung zur Ver mchtung von Mull
US4003797A (en) * 1976-05-05 1977-01-18 Union Oil Company Of California Superatmospheric pressure shale retorting process
US4066529A (en) * 1976-05-07 1978-01-03 Paraho Corporation Method of design for vertical oil shale retorting vessels and retorting therewith
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US4199432A (en) * 1978-03-22 1980-04-22 Chevron Research Company Staged turbulent bed retorting process
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DE2923048C2 (de) * 1979-06-07 1984-11-08 Rheinische Braunkohlenwerke AG, 5000 Köln Verfahren zum Schwelen von Ölschiefer oder Teersand in Gegenwart von Wasserstoff

Also Published As

Publication number Publication date
YU129481A (en) 1983-12-31
EP0049324A1 (fr) 1982-04-14
DE3023670C2 (de) 1982-12-23
YU42719B (en) 1988-12-31
DE3023670A1 (de) 1982-01-14
JO1113B1 (en) 1982-07-10
ES503316A0 (es) 1982-10-01
BR8103968A (pt) 1982-03-09
AU545951B2 (en) 1985-08-08
US4388173A (en) 1983-06-14
ES8207580A1 (es) 1982-10-01
DE3165997D1 (en) 1984-10-18
AU7167081A (en) 1982-01-07
MA19167A1 (fr) 1981-12-31

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