EP0068524B1 - Verfahren zur Gewinnung von Öl aus ölhaltigen Mineralien - Google Patents

Verfahren zur Gewinnung von Öl aus ölhaltigen Mineralien Download PDF

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Publication number
EP0068524B1
EP0068524B1 EP82200571A EP82200571A EP0068524B1 EP 0068524 B1 EP0068524 B1 EP 0068524B1 EP 82200571 A EP82200571 A EP 82200571A EP 82200571 A EP82200571 A EP 82200571A EP 0068524 B1 EP0068524 B1 EP 0068524B1
Authority
EP
European Patent Office
Prior art keywords
retorting
gases
oil
reactor
mineral
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
EP82200571A
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German (de)
English (en)
French (fr)
Other versions
EP0068524A1 (de
Inventor
Norbert Dipl.-Ing. Magedanz
Horst Dipl.-Ing. Seidel
Hans Jurgen Dr.-Ing. Dipl.-Ing. Weiss
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.)
GEA Group AG
Original Assignee
Metallgesellschaft AG
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Filing date
Publication date
Application filed by Metallgesellschaft AG filed Critical Metallgesellschaft AG
Publication of EP0068524A1 publication Critical patent/EP0068524A1/de
Application granted granted Critical
Publication of EP0068524B1 publication Critical patent/EP0068524B1/de
Expired legal-status Critical Current

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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
    • 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

Definitions

  • the invention relates to a method for extracting oil from oil-containing minerals by smoldering and separating oil from the smoldering gases containing the smoldering products, whereby after the smoldering solid carbon present in the smoldered mineral is burned by supplying oxygen-containing gases, part of the burned hot mineral with the oily mineral is charged into a shaft-shaped smoldering reactor and the oily mineral in the mixture is heated to the smoldering temperature.
  • Oily minerals such as oil sand, diatomaceous earth and in particular oil shale are thermally treated and swelled to extract their oil content. During smoldering, they are heated to the smoldering temperature of around 400 to 600 "C in a neutral or reducing atmosphere with the exclusion of oxygen. This produces various gases and vapors from the organic components. The oils are condensed from the smoldering gases. The gas leaving the condensation The carbonized residue contains solid carbon as a carbonized product, which carbon has to be burned for heat-economic reasons and the heat generated in this process must be used for the process.
  • the invention is based, to process even coarser minerals with high throughput with high oil output using a shaft-shaped smoldering reactor.
  • This object is achieved according to the invention in that part of the smoldering takes place in a shaft-shaped smoldering reactor, the mineral from the smoldering reactor is charged onto a traveling grate, in a post-smoldering zone the remaining smoldering takes place with the passage of inert or reducing gases, the smoldering gases from the smoldering reactor and passed from the post-smoldering zone into the separation stage and freed of oil, the smoldered mineral on the traveling grate is led into a combustion zone, at the beginning of the combustion zone the solid carbon contained in the surface of the board is ignited, then the combustion zone by sucking in oxygen-containing gases is led through the bed, the amount of the sucked-in oxygen-containing gases is controlled so that the bed is brought to the maximum possible temperature by the combustion of solid carbon, the burned mineral is thrown off the traveling grate, and part of the burned M is returned to the smoldering reactor.
  • the fresh oil-containing mineral and the recirculated, hot, burned mineral are charged into the smoldering reactor with the exclusion of air. Batching can take place continuously or in batches.
  • the materials can be charged in layers on the surface of the material column in the smoldering reactor, or the material streams can be mixed in free fall before hitting the surface.
  • the amount of the recycled fired material is measured so that its heat content is sufficient to carry out the smoldering after mixing with the fresh oil-containing material.
  • the smoldering reactor can be arranged in front of the moving grate and can only be connected to the moving grate via a discharge device. It can also be arranged above the beginning of the traveling grate, with the discharged mineral being supported directly on the traveling grate.
  • the discharge opening or discharge device of the smoldering reactor is shielded against the ingress of air.
  • the smoldering in the smoldering reactor can take place with or without the introduction of gases into the smoldering reactor. If no gases are introduced, the smoldering gases consist only of the gases generated during the smoldering itself.
  • the smoldering gases consist of a mixture consisting of the introduced gases and the gases produced during the smoldering.
  • the distribution of the smoldering process to the smoldering in the shaft-shaped smoldering reactor and the remaining smoldering in the post-smoldering zone on the traveling grate takes place under the aspect of processing minerals that are coarse or contain a proportion of coarse grain size while introducing the smallest possible amounts of inert or reducing gases into the smoldering reactor and into the post-smoldering zone on the traveling grate for the purpose of controlling the reaction-kinetic sequence of the smoldering.
  • the smoldering process can preferably take place in the shaft-shaped smoldering reactor or in the post-smoldering zone be carried out on the traveling grate.
  • the specific amounts of the gas streams introduced into the two smoldering zones also depend on the reaction kinetic requirements.
  • the carbonization gases are preferably sucked out of the carbonization reactor from the lower part because this leads the gases away from the mixing point of the recirculated hot mineral with the fresh oil-containing mineral and better temperature control is possible, and because there are shorter routes to the separation stage. Gases freed from oil from the separation stage or foreign gases can be used as inert or reducing gases.
  • a preferred embodiment consists in that the smoldering reactor is arranged over the first part of the traveling grate and the smoldering gases are sucked out of the smoldering reactor through the traveling grate.
  • a preferred embodiment is that inert or reducing gases are introduced into the upper part of the shaft-shaped smoldering reactor. This accelerates the reaction kinetics of the smoldering process in the smoldering reactor. The amount of gases introduced is kept as small as possible.
  • a preferred embodiment consists in that a partial flow of the gases freed from oil is returned to the smoldering stages as smoldering gas. Since the gases emerging from the separation stage still contain the non-condensable smoldering products that arise during the smoldering process, the recycle results in a gas with a high calorific value.
  • a preferred embodiment is that the gases in the smoldering zones are set in oscillating vibrations. As a result, the reaction kinetics can be improved with the same amounts of gas in the smoldering zones, or smaller amounts of gas are required to achieve the desired reaction kinetics.
  • a preferred embodiment is that a smaller specific amount of gas is introduced into the smoldering reactor than into the post-smoldering zone. As a result, the entire carbonization process can be carried out with a smaller amount of carbonization gas.
  • a longer residence time of the mineral in the smoldering shaft results in a longer reaction kinetic process and requires a low specific volume of smoldering gas there.
  • the remaining smoldering on the traveling grate is then carried out with a larger specific smoldering gas volume (gas volume per unit of mineral).
  • a preferred embodiment is that the partial stream of the recirculated burned mineral is reheated in the smoldering reactor before being fed into the reactor.
  • the reheating is expediently carried out by combustion of the gas from the separation stage, but can also be carried out using external energy.
  • the post-heating can compensate for heat losses of the burned, returned mineral due to longer transport routes or cold outside temperature and the amount of the returned mineral can be kept smaller.
  • a preferred embodiment is that the heat of the exhaust gas from the combustion zone is used to dry and preheat the oil-containing material and / or to heat gases which are introduced into the process.
  • Gases that are introduced into the process are those gases that are directed into the smoldering zones, into the ignition for the solid carbon, and into the reheating of the returned mineral.
  • the waste heat of the exhaust gas can be used in a favorable manner for the process.
  • a preferred embodiment is that the hot mineral thrown off and not returned by the traveling grate is in a cooler and the heated cooling gases are used for preheating the oil-containing mineral and / or for heating gases which are introduced into the process.
  • the non-recycled mineral is preferably cooled by air in direct contact to the temperature required for removal. The heat content of the heated cooling air, or the heat content of the hottest part of the cooling air, can then be used in a favorable manner for the process.
  • the invention is illustrated by a figure.
  • the shaft-shaped smoldering reactor 1 has two double locks 2a, 2b and 3a, 3b.
  • lock 2a hot, burned, recycled mineral is charged onto the lock 2b by means of a transport device 4.
  • lock 3a oil-containing mineral is charged onto the lock 3b by means of a transport device 5. Then the locks 2a and 3a closed and the locks 2b and 3b opened, whereby the material is distributed over the surface of the mineral mixture 6 via distribution devices, not shown.
  • a small amount of oil-free carbonization gas is introduced into the upper part of the carbonization reactor 1 via a ring line 7.
  • the carbonization gases from the carbonization reactor 1 are passed into the suction box 8 and via line 9 into the separation stage 10.
  • the partially smoldered mineral is charged from the smoldering reactor 1 through the discharge opening 11 onto the moving grate 12 in the form of a bed 13 with a defined layer height.
  • Smelting gases freed from oil are introduced into the post-carbonization zone 14 by means of the gas hood 15 and passed through the bed 13.
  • the carbonization gases from the post-carbonization zone 14 are passed into the suction boxes 16 and via lines 17 into the separation stage 10.
  • the oil separated in the separation stage 10 is discharged via line 18.
  • the oil-free carbonization gases which contain the non-condensable carbonization products, are partly fed via line 19 into the ring line 7, partly via line 20 into the gas hood 15, partly via line 21 into the ignition furnace 22 at the beginning of the combustion zone 23 and to Part derived via line 24.
  • air 25 is sucked through the bed 13 and the combustion zone is thereby passed through the bed 13 from top to bottom.
  • the amount of air 25 is controlled so that the bed 13 has the maximum possible temperature at the end of the combustion zone 23. This means that the exhaust gases also have the maximum possible temperature.
  • the hot exhaust gases are fed into the suction boxes 26 and via lines 27 into the drying and preheating 28, into which fresh, oil-containing mineral is fed via 23a.
  • the preheated mineral is charged into the smoldering reactor 1 by means of a transport device 5.
  • the cooled exhaust gas is passed via line 29 into the gas cleaning system 30 and from there into the chimney 31.
  • the hot bed 13 is thrown off the traveling grate 12 into a separation station 32.
  • the part required for the smoldering in the smoldering reactor is separated off and passed via a transport device 33 into the reheating 34, where it is reheated by means of a partial flow of the oil-free gases from the separation stage 10 (not shown) and charged into the smoldering reactor 1 by means of transport device 4 .
  • the remaining hot mineral from the separation station 32 is charged into a cooler 33, where it is cooled by air 34 to the temperature required for the removal and discharged via 35.
  • the heated cooling air is discharged via line 36. It is used to heat the gases in lines 19, 20, 21 (not shown) and the gases that are used in the reheating.
  • the line 35 shown in broken lines is open, the line 20 can be closed. Then, however, the gas cannot be passed into the smoldering reactor 1 and into the post-melting zone 14 at different pressures.
  • the advantages of the invention are that the operating costs for the smoldering can be reduced considerably, since only very large oversize particles have to be crushed, that very large throughputs can be achieved with relatively little effort and that tried and tested units can be used that have been used since Years of high throughput in other areas.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Gasification And Melting Of Waste (AREA)
EP82200571A 1981-06-19 1982-05-11 Verfahren zur Gewinnung von Öl aus ölhaltigen Mineralien Expired EP0068524B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3124019 1981-06-19
DE19813124019 DE3124019A1 (de) 1981-06-19 1981-06-19 Verfahren zur gewinnung von oel aus oelhaltigen mineralien

Publications (2)

Publication Number Publication Date
EP0068524A1 EP0068524A1 (de) 1983-01-05
EP0068524B1 true EP0068524B1 (de) 1984-09-19

Family

ID=6134872

Family Applications (1)

Application Number Title Priority Date Filing Date
EP82200571A Expired EP0068524B1 (de) 1981-06-19 1982-05-11 Verfahren zur Gewinnung von Öl aus ölhaltigen Mineralien

Country Status (7)

Country Link
US (1) US4388174A (enrdf_load_stackoverflow)
EP (1) EP0068524B1 (enrdf_load_stackoverflow)
AU (1) AU549064B2 (enrdf_load_stackoverflow)
CA (1) CA1175373A (enrdf_load_stackoverflow)
DE (2) DE3124019A1 (enrdf_load_stackoverflow)
IN (1) IN154825B (enrdf_load_stackoverflow)
ZA (1) ZA823257B (enrdf_load_stackoverflow)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4436611A (en) 1983-07-01 1984-03-13 Dravo Corporation Process for heating recycle gas in oil shale retorting
US4439307A (en) * 1983-07-01 1984-03-27 Dravo Corporation Heating process gas for indirect shale oil retorting through the combustion of residual carbon in oil depleted shale
US4490237A (en) * 1983-07-01 1984-12-25 Dravo Corporation Process for recovering heat from the combustion of residual carbon in oil depleted shale
US4689120A (en) * 1985-06-14 1987-08-25 Phillips Petroleum Company Apparatus for the recovery of oil from shale

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1918162A (en) * 1928-11-01 1933-07-11 Lehigh Coal And Navigation Com Method of carbonizing briquettes
US2406810A (en) * 1944-03-18 1946-09-03 Universal Oil Prod Co Treatment of hydrocarbonaceous solids
US3350280A (en) * 1963-10-31 1967-10-31 Standard Oil Co Retort for oil-bearing shales
US3325395A (en) * 1965-04-19 1967-06-13 Mcdowell Wellman Eng Co Travelling grate method for the recovery of oil from oil bearing minerals
US3483115A (en) * 1966-04-13 1969-12-09 Mobil Oil Corp Travelling grate shale retorting
US3449211A (en) * 1967-04-28 1969-06-10 Sun Oil Co Apparatus for pyrolysis of solids
US3560369A (en) * 1968-06-05 1971-02-02 Allis Chalmers Mfg Co Retorting oil shale including agglomerated fines
DE1909263C3 (de) * 1969-02-25 1974-04-25 Metallgesellschaft Ag, 6000 Frankfurt Verfahren und Vorrichtung zum Schwelen von feinkörnigen bituminösen Stoffen, die einen staubförmigen Schwelrückstand bilden
US4082645A (en) * 1975-04-14 1978-04-04 The Superior Oil Company Recovery of hydrocarbon values by controlled eduction and oxidation of oil shale
US4193862A (en) * 1978-06-26 1980-03-18 Mcdowell-Wellman Company Recovery of oil and gas from oil shale
JPS5560113A (en) * 1978-10-31 1980-05-07 Ebara Corp Flow layer type combustion device for city refuse and the like
US4347119A (en) * 1980-11-21 1982-08-31 Thomas Delbert D Horizontal oil shale and tar sands retort

Also Published As

Publication number Publication date
DE3260772D1 (en) 1984-10-25
AU549064B2 (en) 1986-01-09
EP0068524A1 (de) 1983-01-05
AU8499682A (en) 1982-12-23
US4388174A (en) 1983-06-14
DE3124019A1 (de) 1982-12-30
IN154825B (enrdf_load_stackoverflow) 1984-12-15
ZA823257B (en) 1983-03-30
CA1175373A (en) 1984-10-02

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