EP0073355A1 - Procédé de fabrication d'hydrocarbures liquides - Google Patents

Procédé de fabrication d'hydrocarbures liquides Download PDF

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Publication number
EP0073355A1
EP0073355A1 EP82107035A EP82107035A EP0073355A1 EP 0073355 A1 EP0073355 A1 EP 0073355A1 EP 82107035 A EP82107035 A EP 82107035A EP 82107035 A EP82107035 A EP 82107035A EP 0073355 A1 EP0073355 A1 EP 0073355A1
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EP
European Patent Office
Prior art keywords
coal
water
process according
pressure
temperature
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Granted
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EP82107035A
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German (de)
English (en)
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EP0073355B1 (fr
Inventor
Hubert Dr. Coenen
Rainer Hagen
Ernst Dr. Kriegel
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Fried Krupp AG
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Fried Krupp AG
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Publication of EP0073355A1 publication Critical patent/EP0073355A1/fr
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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
    • C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
    • 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
    • C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining 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
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
    • C10G1/086—Characterised by the catalyst used
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S208/00—Mineral oils: processes and products
    • Y10S208/952—Solid feed treatment under supercritical conditions

Definitions

  • the invention relates to a method for producing liquid hydrocarbons from coal.
  • the liquid hydrocarbons which are produced by this process include the alkanes, the cycloalkanes and the aromatics, which have a boiling point of 20 to approx. 350 ° C. and whose molecules contain 5 to approx. 30 carbon atoms.
  • These liquid hydrocarbons are processed into fuels and lubricants in particular and used as heating oil and chemical raw materials.
  • hydrocarbons can be obtained from coal by catalytic hydrogenation.
  • ground coal with heavy oil or tar with the addition of a molybdenum-containing catalyst is finely stirred to form a dough and then hydrogenated at 200 to 300 atm and 450 C to 50 0 0 with hydrogen.
  • the reaction mixture obtained after the hydrogenation is separated by distillation and provides gasoline, gas oil and a residue which is mixed again with coal dust and is returned to the hydrogenation process.
  • the hydrocarbons produced by the Bergius process mainly consist of alkanes and cycloalkanes (see H. Beyer, "Textbook of Organic Chemistry” S. Hirzel Verlag, Leipzig, 1962, pages 63 to 64).
  • the invention has for its object to provide a process for the production of liquid hydrocarbons from coal, which provides a high yield, works inexpensively and reliably, can be operated with coal of different origins and only provides a small amount of waste products.
  • the underlying the invention object is achieved by the fact that crushed coal is treated at 380 to 6 0 0 0 C and 260 up to 450 bar with water, that at the same time or immediately after the water treatment at the same pressure and temperature in the presence of a catalyst a hydrogenation with Hydrogen occurs that the gas phase is then broken down into its constituents, which are obtained in several fractions, by lowering the pressure and the temperature, and that energy and / or gas is obtained from the coal residue.
  • the requirement to carry out the water treatment and the hydrogenation at the same pressure and temperature naturally includes the possibility that certain system-related pressure and temperature changes can occur.
  • liquid hydrocarbons obtained by the process according to the invention consist predominantly of paraffin hydrocarbons and contain a fluctuating amount of aromatic hydrocarbons, the proportion of aromatics in the higher-boiling fractions being greater than in the low-boiling fractions.
  • aromatic content is from the Her of the coal, the composition of the coal and the reaction conditions of the process according to the invention.
  • the method according to the invention works cost-effectively, reliably and in particular in an environmentally friendly manner.
  • the cost-effective and environmentally friendly method of operation of the process is based primarily on the fact that the coal residue that arises after the water treatment and hydrogenation is very suitable for gasification because of its high porosity and that the water can be easily separated from the liquid hydrocarbons.
  • the water prevents the coal bed from caking, which favors an even reaction process.
  • the method according to the invention can be carried out particularly advantageously if the comminuted coal has a particle size of 1 / um to 5 mm, if a quantity of water of 100 to 1000% by weight, based on coal, is used to treat the coal and if an amount of hydrogen of 2 to 10% by weight, based on coal, is used for the hydrogenation.
  • the comminuted coal while carrying out the water treatment and the hydrogenation contains a catalyst in an amount of 2 to 30 wt .-%, based on coal, which remains in the coal residue.
  • the catalyst is Fe 2 0 3 with very small particles size is used.
  • the water treatment of the coal and the hydrogenation run side by side without interference if the coal contains a solid catalyst, preferably Fe 2 O 3 , in a very fine distribution.
  • the Fe 2 0 3 can remain in the coal residue since it is very inexpensive and does not hinder the further use of the coal residue.
  • a catalyst when the water treatment and the hydrogenation are carried out simultaneously, a catalyst is dissolved in an amount of 0.001 to 0.5% by weight, based on water.
  • N a OH, KOH, Na 4 SiO 4, KBO 2 and NaBO. 2 Since the catalyst is dissolved in the aqueous phase, it is present in the reaction system in a very homogeneous distribution and therefore has a particularly great effect.
  • the invention provides as a further alternative that after the water treatment of the coal, the water vapor phase is separated from the coal, mixed with hydrogen and passed over a fixed bed catalyst.
  • the fixed bed catalyst consists of an acidic component and a redox component, Al 2 O 3 , Si0 2 , Fe 2 0 3 and / or zeolites as the acid component and MoO 3 as the redox component with CoO and / or W0 3 with NiO is used.
  • the fixed bed catalyst is only very slightly damaged by the sulfur and nitrogen compounds present in the water vapor phase, and on the catalyst satorteilchen no solid carbon compounds or no carbon are deposited, so that the fixed bed catalyst has an advantageously long life of several weeks.
  • the spatial separation of the water treatment of the coal and the hydrogenation results in an advantageous reduction in the residence time.
  • the process according to the invention is carried out in such a way that the water treatment and the hydrogenation take place in 10 to 120 minutes. If the water treatment and the hydrogenation are carried out spatially separated from one another, the dwell time for both steps is clearly less than 120 minutes, with each step preferably getting by with 10 to 30 minutes.
  • the invention provides that the gas phase be separated from the coal or the fixed bed catalyst so that its pressure is reduced to 230 to 250 bar and that the resulting inorganic compounds are separated off in a cyclone or filter.
  • This measure according to the invention ensures that the inorganic compounds dissolved in the gas phase, which are ash constituents of the coal and / or catalysts, are separated in solid form from the gas phase, which considerably facilitates the subsequent separation of the reaction mixture.
  • the gas phase is separated from the coal or the fixed bed catalyst, that its pressure is reduced to 200 to 220 bar and its temperature to 360 to 370 C and that the solid inorganic compounds and the water from the gas phase precipitate and be separated as a solution or suspension. This procedure is possible because both the inorganic compounds and the water precipitate out of the gas phase under the conditions mentioned.
  • the water can only be partially circulated, but on the other hand it facilitates the separation of the reaction mixture, which takes place according to the invention in such a way that the The gas phase freed from the solid inorganic compounds and the water is released to a pressure of 20 to 55 bar and then in a rectification column at a top temperature of 360 to 370 C and a bottom temperature of 210 to 335 C in a heavy oil, medium oil and crude gasoline fraction is disassembled.
  • the position of the high-pressure phase equilibrium means that, according to the invention, crude gasoline is obtained as the top product and heavy oil as the bottom product in the rectification column.
  • the middle oil fraction is taken from the rectification column as a side stream.
  • the heavy oil fraction is wholly or partly mixed with the comminuted coal, whereby the higher-boiling hydrocarbons and most of the aromatic hydrocarbons are recycled.
  • This process procedure increases the yield of lower-boiling hydrocarbons and paraffin hydrocarbons, and the comminuted coal can be stored and transported with minimal dust formation, it being entirely possible to use a pumpable coal-heavy oil mixture as raw material in the process according to the invention.
  • the economy of the process according to the invention can be improved in that the gases remaining after the separation of the solid inorganic compounds, the liquid hydrocarbons and the water are first freed of H 2 S and / or NH 3 and then burned to obtain energy.
  • the successful feasibility of the method according to the invention obviously has the following causes.
  • the extractable organic compounds present in the coal are almost quantitatively dissolved by the water, which is in the supercritical state, because the supercritical water also penetrates into the micropores of the coal due to its low viscosity and surface tension.
  • the high-molecular hydrocarbons are cracked, with lower-boiling hydrocarbons being formed.
  • the cracking is accelerated by the catalysts present.
  • the unsaturated aliphatic hydrocarbons present in the supercritical water vapor phase are converted almost quantitatively into alkanes or cycloalkanes in the catalytic hydrogenation.
  • the aromatics present in the supercritical steam phase are partially hydrogenated so that their proportion in the end products of the process is comparatively low, the heavy oil fraction having the largest proportion of aromatics.
  • Many cycloalkanes in turn form alkanes under the influence of cracking and hydrogenation.
  • the sulfur and nitrogen compounds present in the coal are cracked and ultimately form hydrocarbons as well as H Z S and NH 3 .
  • the catalysts present in the process according to the invention are only insignificantly poisoned by the sulfur and nitrogen compounds present.
  • the coal is conveyed from the storage bunker 1 into the mill 2, where it is ground to a grain size of approximately 0.2 to 1 mm.
  • the coal is mixed with water, which reaches the mill 2 via the line 3.
  • the coal-water suspension is mixed in the mixer 4 via line 5 with heavy oil.
  • the coal-oil-water mixture passes through the line 6 and the pressure pump 7 into the heated high-pressure reactor 8, where it remains for about 30 minutes at a pressure of 350 to 380 bar and a temperature of 450 to 500 ° C.
  • the coal residue is discharged from the high-pressure reactor 8 via the line 9, while the supercritical water vapor phase laden with organic compounds reaches the hydrogenation reactor 11 via the line 10.
  • hydrogen is added to the water vapor phase via line 12.
  • the hydrogenation reactor 11 is in In the form of a fixed bed, a catalyst is arranged which accelerates both the cracking and the hydrogenation reactions.
  • the residence time of the gas phase in the hydrogenation reactor 11 is approximately 15 minutes.
  • the gas phase passes through line 13, expansion valve 14 and heat exchanger 15 into cyclone 16, in which a pressure of approximately 240 bar is set and the working temperature prevailing in hydrogenation reactor 11 is maintained.
  • cyclone 16 the inorganic compounds dissolved in the gas phase precipitate out in solid form and are discharged via line 17.
  • the gas phase freed from the inorganic compounds is fed via line 18 into the expansion valve 19, where it is expanded to 140 to 160 bar.
  • the gas phase passes through the heat exchanger 20, in which the temperature is reduced to 350 ° C., into the separator 21, from which the heavy oil fraction is removed through the line 22 and conveyed into the tank 23.
  • the gas phase emerging from the separator 21 passes via the line 24 and the expansion valve 45 into the heat exchanger 25, the pressure and temperature of the gas phase being reduced to approximately 5 bar or approximately 170 ° C.
  • the middle oil fraction precipitates out of the gas phase and reaches the collecting tank 28 via the line 27.
  • the gas phase coming from the separator enters via line 29 into the expansion valve 30 and the heat exchanger 31, where cooling and pressure reduction to ambient temperature and pressure take place.
  • the in the Gas phase still existing crude gasoline fraction and the water are separated together in the separator 32.
  • the gas phase freed from the liquid hydrocarbons consists of H 2 ' CO, C0 2 and a hydrocarbon fraction (C 1 to C 4 ) and is contaminated with NH 3 and / or H 2 S.
  • This gas is conveyed via line 33 into a gas cleaning device 34, where H 2 S and / or NH 3 are separated.
  • the cleaned gas is then burned in the boiler system 35, where energy is obtained.
  • the crude gasoline-water fraction obtained in the separator 32 passes via the line 36 into the separation column 37, from which the crude gasoline flows out at the top and the water at the bottom of the column.
  • the raw gasoline reaches the tank / 39 via line 38 and is then separated into the individual gasoline fractions by known distillation methods.
  • the water can be fed to line 3 via line 40 and thus returns to the process cycle.
  • the coal residue passes through line 9 into the reactor 41, where it is gasified with air and water.
  • the gasification reactions run very evenly due to the high porosity of the coal residue.
  • the gas produced in the reactor 41 becomes the conversion plant 42 supplied in whole or in part and there according to the equation processed into hydrogen, which is supplied to the tank 43 via the line 44.
  • the carbon dioxide present in the hydrogen is washed out with water in the pressure washer 46. Energy can be obtained from the part of the gas that is not processed into hydrogen by combustion in the boiler system 35. It is also possible to directly burn the coal residue obtained in the high-pressure reactor 8 and thus convert it into energy.
  • the coal is conveyed from the storage bunker 1 into the mill 2, where it is ground to a grain size of approximately 0.2 to 1 mm.
  • the coal is mixed with water, which reaches the mill 2 via the line 3.
  • the coal-water suspension is mixed in the mixer 4 via line 5 with heavy oil.
  • Fe 2 O 3 is conveyed from the storage container 10 into the mixer 4, which has a particle size of less than 1 / um.
  • the amount of Fe 2 0 3 fed to the mixer 4 is approximately 5% by weight, based on coal.
  • the coal-water- ⁇ 1-Fe 2 O 3 mixture reaches the heated high-pressure reactor 8 via line 6 and the pressure pump 7.
  • Heated hydrogen from line 9 is metered into this mixture before it enters the high-pressure reactor 8.
  • the high pressure reactor 8 run at a pressure of 350 to 380 bar and a temperature of 450 to 550 C during a reaction time of about 40 minutes under the influence of the Fe 2 0 3 extraction processes acting as a catalyst and cracking and hydrogenation reactions.
  • the coal residue is discharged from the high-pressure reactor 8 via the line 11, while the supercritical water vapor phase laden with organic compounds emerges from the high-pressure reactor 8 via the line 12.
  • the supercritical water vapor phase is expanded to a pressure of approx. 210 bar in the expansion valve 13 and cooled to a temperature of 360 C in the heat exchanger 14. Under these conditions, the inorganic compounds dissolved in the supercritical gas phase and the water precipitate out in the separator 15. Both components are discharged as a suspension or solution via line 16.
  • the gas phase passes from the separator 15 via the line 17 into the expansion valve 18, where the pressure is reduced to approximately 40 bar.
  • the gas phase is then fed via line 19 into the heated rectification column 20, at the top of which a temperature of 360 ° C., in the middle part of which a temperature of 280 ° C. and in the bottom thereof a temperature of 210 ° C.
  • a gas phase is removed from the top of the rectification column 20 via line 21, the middle oil fraction in the middle part via line 22 and the heavy oil fraction from the bottom via line 23.
  • the heavy oil fraction or the middle oil fraction is expanded in the expansion vessels 24 and 25, the gases released being fed to the line 21. After cooling, the middle oil fraction led into the tank 26 and the heavy oil fraction in the tank 27.
  • the gas phase passes from line 21 into expansion valve 28 and heat exchanger 29, where the pressure and temperature are reduced to the values prevailing in the environment.
  • the crude gasoline fraction precipitates, which flows off via the line 31 into the tank 32, at the bottom of which the remaining water collects, which is removed discontinuously via the line 33.
  • the gas emerging from the separator 30 consists of H 2 , CO, C0 2 and a hydrocarbon fraction (C 1 to C 4 ) and is contaminated with NH 3 and / or H 2 S. This gas is conveyed into a gas cleaning device 34, where H 2 S and / or NH 3 are separated. The cleaned gas is then burned in the boiler system 35, energy being obtained.
  • the heavy oil fraction is fed to the mixer 4 in whole or in part from the tank 27 via the line 5.
  • the medium oil and crude gasoline fractions are processed according to known distillation methods.
  • the coal residue passes through line 11 into the reactor 36, where it is gasified with air and water. All or part of the gas produced in the reactor 36 is fed to the conversion system 37 and processed there to form hydrogen, which, after removal of the CO 2 in the pressure washer 38, is fed to the tank 39 via the line 40. The part of the gas that is not processed into hydrogen can be burned 35 energy can be obtained in the boiler system.
  • the solids are filtered off in the filter 41 from the aqueous suspension which emerges from the line 16 and are deposited together with the ash accumulating in the reactor 36 in a landfill.
  • the filtrate emerging from the filter 41 is introduced via line 42 into a wastewater treatment plant.
  • the water has the following critical data:

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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)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
EP82107035A 1981-08-25 1982-08-04 Procédé de fabrication d'hydrocarbures liquides Expired EP0073355B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3133562 1981-08-25
DE19813133562 DE3133562A1 (de) 1981-08-25 1981-08-25 "verfahren zur herstellung fluessiger kohlenwasserstoffe"

Publications (2)

Publication Number Publication Date
EP0073355A1 true EP0073355A1 (fr) 1983-03-09
EP0073355B1 EP0073355B1 (fr) 1985-03-13

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EP82107035A Expired EP0073355B1 (fr) 1981-08-25 1982-08-04 Procédé de fabrication d'hydrocarbures liquides

Country Status (7)

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US (1) US4485003A (fr)
EP (1) EP0073355B1 (fr)
JP (1) JPS5842689A (fr)
AU (1) AU546829B2 (fr)
CA (1) CA1191468A (fr)
DE (1) DE3133562A1 (fr)
ZA (1) ZA826132B (fr)

Cited By (5)

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WO1996004598A1 (fr) * 1994-08-01 1996-02-15 Rpc Waste Management Services, Inc. Doing Business As Eco Waste Technologies Systeme et procede de reduction de pression
WO2012167791A3 (fr) * 2011-06-10 2013-04-11 Steeper Energy Aps Procédé et appareil pour produire un hydrocarbure liquide
US9982199B2 (en) 2012-08-30 2018-05-29 Steeper Energy Aps Method for preparing start up of process and equipment for producing liquid hydrocarbons
US10005962B2 (en) 2012-08-30 2018-06-26 Steeper Energy Aps Method for preparing shut down of process and equipment for producing liquid hydrocarbons
US10087373B2 (en) 2012-08-30 2018-10-02 Steeper Energy Aps Method for controlling cleaning of an apparatus for producing liquid hydrocarbons

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US7553475B2 (en) 2003-04-16 2009-06-30 Energy & Environmental Research Center Foundation Process for producing high-pressure hydrogen
US7947165B2 (en) * 2005-09-14 2011-05-24 Yeda Research And Development Co.Ltd Method for extracting and upgrading of heavy and semi-heavy oils and bitumens
JP2009513113A (ja) * 2005-10-28 2009-04-02 ベーリンガー インゲルハイム インターナショナル ゲゼルシャフト ミット ベシュレンクテル ハフツング Ｃ型肝炎ウイルスｎｓ２／３活性のアッセイ法
WO2009059369A1 (fr) * 2007-11-06 2009-05-14 Advanced Biofuels Ltd Procédé de liquéfaction
US7754067B2 (en) * 2008-02-20 2010-07-13 Air Products And Chemicals, Inc. Process and apparatus for upgrading heavy hydrocarbons using supercritical water
US20090206007A1 (en) * 2008-02-20 2009-08-20 Air Products And Chemicals, Inc. Process and apparatus for upgrading coal using supercritical water
CN102165036B (zh) * 2008-07-28 2015-05-20 福布斯油气私人有限公司 一种将含碳材料液化成液态烃的方法
RU2408649C2 (ru) * 2008-12-29 2011-01-10 Сергей Васильевич Пашкин Способ переработки органических отходов и устройство для его осуществления
EP2513252A1 (fr) 2009-12-11 2012-10-24 Altaca Insaat ve Dis Ticaret A.S. Conversion de matière organique en huile
LT2718404T (lt) 2011-06-10 2021-05-10 Steeper Energy Aps Skystų angliavandenilių gamybos būdas

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Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1996004598A1 (fr) * 1994-08-01 1996-02-15 Rpc Waste Management Services, Inc. Doing Business As Eco Waste Technologies Systeme et procede de reduction de pression
WO2012167791A3 (fr) * 2011-06-10 2013-04-11 Steeper Energy Aps Procédé et appareil pour produire un hydrocarbure liquide
WO2012167790A3 (fr) * 2011-06-10 2013-04-11 Steeper Energy Aps Procédé et appareil pour produire un hydrocarbure liquide
WO2012167793A3 (fr) * 2011-06-10 2013-04-25 Steeper Energy Aps Procédé et appareil pour produire un hydrocarbure liquide
US9695364B2 (en) 2011-06-10 2017-07-04 Steeper Energy Aps Process for producing liquid hydrocarbon
US9758729B2 (en) 2011-06-10 2017-09-12 Steeper Energy Aps Process and apparatus for producing liquid hydrocarbon
US9902908B2 (en) 2011-06-10 2018-02-27 Steeper Energy Aps Process and apparatus for producing liquid hydrocarbon
US9982199B2 (en) 2012-08-30 2018-05-29 Steeper Energy Aps Method for preparing start up of process and equipment for producing liquid hydrocarbons
US10005962B2 (en) 2012-08-30 2018-06-26 Steeper Energy Aps Method for preparing shut down of process and equipment for producing liquid hydrocarbons
US10087373B2 (en) 2012-08-30 2018-10-02 Steeper Energy Aps Method for controlling cleaning of an apparatus for producing liquid hydrocarbons

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Publication number Publication date
DE3133562A1 (de) 1983-03-10
JPS5842689A (ja) 1983-03-12
US4485003A (en) 1984-11-27
CA1191468A (fr) 1985-08-06
EP0073355B1 (fr) 1985-03-13
AU8721182A (en) 1983-03-03
AU546829B2 (en) 1985-09-19
ZA826132B (en) 1983-07-27
DE3133562C2 (fr) 1987-01-15

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