EP0177676B1 - Process carried out by heat recuperation for suspension hydrogenation with integrated gas phase hydrogenation - Google Patents
Process carried out by heat recuperation for suspension hydrogenation with integrated gas phase hydrogenation Download PDFInfo
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- EP0177676B1 EP0177676B1 EP85107962A EP85107962A EP0177676B1 EP 0177676 B1 EP0177676 B1 EP 0177676B1 EP 85107962 A EP85107962 A EP 85107962A EP 85107962 A EP85107962 A EP 85107962A EP 0177676 B1 EP0177676 B1 EP 0177676B1
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- hydrogenation
- gas phase
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- temperature
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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
- C10G1/002—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
Definitions
- a process is also known in which hydrocarbon mixtures which are foreign to the process are advantageously used as grinding oils for mashing the coal instead of oils of process origin (EP-A-123161).
- a defined phase equilibrium temperature is set in the intermediate separator in order to achieve the predetermined quantity splitting by partial condensation of the hydrogenation products from the bottom phase.
- This temperature in the intermediate separator is set by cooling the hot bottom phase hydrogenation products in heat exchangers, coal mash and hydrogenation gas being heated by indirect heat exchange.
- bypass lines are often used in technology on the heat exchanger in order to keep the heat transfer capacity of the system almost constant by means of controlled bypass valves despite incrusting heat exchangers.
- the large overdimensioning of the heat exchangers for the clean state and the risk of a flange fan in hot high-pressure lines which have bypasses with a large control range are disadvantageous.
- the temperature of the gas phase feedstocks has to be increased as the operating time increases due to the deactivation of the gas phase catalyst (e.g. 390 degrees Celsius to 430 degrees Celsius).
- the invention has for its object to achieve a defined setting of the phase equilibrium temperature in the intermediate separator and a defined increase in the inlet temperature of the gas phase feedstocks with increasing runtime with economic heat recovery despite increasing unavoidable incrustation of the heat exchanger - especially at high mash temperatures.
- This object is achieved in that in order to set the defined phase equilibrium temperature in the intermediate separator, the gaseous hydrogenation products from the bottom phase are cooled in a mash heat exchanger, a head cooler and a final cooler in front of the intermediate separator and the heating of the cold mash-hydrogenation gas mixture in Heat exchangers are carried out by indirect heat exchange with the hot hydrogenation products from the gas phase hydrogenation.
- the temperature of the gas phase feedstocks must be raised gradually. This takes place - without an additional heating furnace - according to the invention in that the temperature level of the head cooler upstream of the intermediate separator is also increased as the mash heat exchanger progresses. At the same time, with increasing reduction in the heat transfer capacity of the mash heat exchanger, the waste heat generated from the bottom phase hydrogenation is transferred to the upstream mash preheating of the bottom phase hydrogenation via the path of gas phase hydrogenation and thus used economically.
- the desired temperature in the intermediate separator is set by means of a final cooler, in which steam is expediently generated or hydrogenation gas is preheated.
- the temperature level of the bottom phase gases / vapors entering the mash heat exchanger can also be reduced. This reduces the usual fast incrustation of clean pipes of the mash heat exchanger, since the max. occurring mash temperature (at the same averaged mash outlet temperature) is reduced.
- the desired temperature of the starting materials for the gas phase hydrogenation can be set by means of a head cooler (incl. Bypass) after the bottom phase hydrogenation.
- the bypass around the mash heat exchanger serves to limit the max. Mash outlet temperature of the mash heat exchanger (especially when the heat exchanger tubes are clean).
- the start-up process is carried out quickly by heating the gas phase feedstocks using a head cooler behind the bottom phase hydrogenation.
- the process is explained in more detail using two examples:
- the gaseous and vaporous products from the bottom phase reactor 4 are partially cooled by means of mash heat exchanger 2 by indirect heat exchange, the mash-hydrogenation gas mixture being heated to the starting temperature of the bottom phase hydrogenation of approximately 440 ° C. on the heating side.
- the bottom phase products are further cooled by indirect heat exchange in the head cooler 7 and in the final cooler 8.
- the products from the bottom phase hydrogenation are divided into the solvent fraction (liquid) and the feed stream for the gas phase hydrogenation (gases / vapors). The latter is heated in the head cooler 7 and then in the indirect heat exchanger 10 to the gas phase reaction temperature of approximately 390 ° C.
- the gas phase products are partially cooled by indirect heat exchange in the mash heat exchanger 1, whereby the mash-hydrogenation gas mixture is preheated.
- the hydrogenation gas is preheated by further cooling of the gas phase products.
- the entire process is self-sufficient in stationary operation.
- the mash heating furnace 3 serves only as a start-up furnace.
- the waste heat from the heat exchanger 8 is preferably used to generate MD steam or to preheat the hydrogenation gas.
- head cooler 6 the gaseous and vaporous products can be used.
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- 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)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Industrial Gases (AREA)
Description
Das Verfahren zur mehrstufigen Hydrierung von Kohle, wobei feingemahlene Kohle mit Öl bei Drücken von 250 bis 350 bar und Temperaturen von 440 bis 500 Grad Celsius in der Sumpfphase mit Wasserstoff hydriert wird und nach Abtrennung der bei der Reaktionstemperatur flüssige Feststoffe enthaltenden Phase die gasförmigen Hydrierprodukte bei gleichem Prozeßdruck in Gegenwart eines Festbettkatalysators weiterhydriert werden, ist durch die Deutschen Offenlegungsschriften 3209143 und 3222730 bekannt. Hierbei werden mittels Teilkondensation der gasförmigen Hydrierprodukte aus der Sumpfphase die schwer siedenden Ölkomponenten als flüssige Phase in einem Zwischen-Abscheider abgezogen und zur Kohleanmaischung zurückgeführt, so daß nur die gasförmigen Ölfraktionen mit leichter bzw. mittlerer Siedelage in die Gasphasehydrierung geleitet werden.The process for the multi-stage hydrogenation of coal, where finely ground coal is hydrogenated with oil at pressures of 250 to 350 bar and temperatures of 440 to 500 degrees Celsius in the bottom phase with hydrogen and, after separating off the phase containing liquid solids at the reaction temperature, the gaseous hydrogenation products the same process pressure in the presence of a fixed bed catalyst, is known from German Offenlegungsschriften 3209143 and 3222730. Here, by means of partial condensation of the gaseous hydrogenation products from the bottom phase, the high-boiling oil components are drawn off as a liquid phase in an intermediate separator and returned to the pulp mashing, so that only the gaseous oil fractions with a light or medium boiling point are passed into the gas phase hydrogenation.
Weiterhin ist ein Verfahren bekannt, bei welchem als Anreiböle für die Kohleanmaischung statt prozeßstämmiger Öle mit Vorteil prozeßfremde Kohlenwasserstoffgemische eingesetzt werden (EP-A-123161).A process is also known in which hydrocarbon mixtures which are foreign to the process are advantageously used as grinding oils for mashing the coal instead of oils of process origin (EP-A-123161).
Bei diesem bekannten Verfahren ist es erforderlich, daß eine definierte Phasengleichgewichtstemperatur im Zwischen-Abscheider eingestellt wird, um die vorgegebene Mengeaufsplittung durch Teilkondensation der Hydrierprodukte aus der Sumpfphase zu erreichen. Diese Temperatur im Zwischen-Abscheider wird durch eine Abkühlung der heißen Sumpfphase-Hydrierprodukte in Wärmeaustauschern eingestellt, wobei durch indirekten Wärmeaustausch Kohlemaische und Hydriergas aufgeheizt werden.In this known method, it is necessary that a defined phase equilibrium temperature is set in the intermediate separator in order to achieve the predetermined quantity splitting by partial condensation of the hydrogenation products from the bottom phase. This temperature in the intermediate separator is set by cooling the hot bottom phase hydrogenation products in heat exchangers, coal mash and hydrogenation gas being heated by indirect heat exchange.
Infolge zunehmender Inkrustierung auf der Maischeseite der Wärmeaustauscher fällt bei den bekannten Verfahren die Wärmeübertragungsleistung stark ab und somit die Phasengleichgewichtstemperatur im Zwischen-Abscheider mit zunehmender Laufzeit ansteigt. Aus Versuchsanlagen der Kohlehydrierung ist die Erkenntnis gekommen, daß die Wärmeaustauscher inbesondere bei hohen Maischetemperaturen stark inkrustieren, wobei der Wärmedurchgangskoeffizient auf unter 50 % - im Extremfall auf 25 % - bezogen auf den sauberen Zustand abfällt. Hierdurch resultiert ein Anstieg der Phasengleichgewichtstemperatur im Zwischen-Abscheider, so daß die vorgegebene Mengenaufteilung durch Teilkondensation nicht aufrechterhalten werden kann. Es ist weiterhin aus Versuchsanlagen die Erkenntnis gekommen, daß Wärmeaustauscher bei niedrigen Maischetemperaturen nahezu frei von Inkrustierungen bleiben.As a result of increasing incrustation on the mash side of the heat exchanger, the heat transfer power drops sharply in the known processes and the phase equilibrium temperature in the intermediate separator thus increases with increasing running time. Experimental coal hydrogenation plants have come to the conclusion that the heat exchangers, particularly at high mash temperatures, become heavily encrusted, with the heat transfer coefficient falling to below 50% - in extreme cases to 25% - in relation to the clean state. This results in an increase in the phase equilibrium temperature in the intermediate separator, so that the predetermined quantity distribution cannot be maintained by partial condensation. It has also come to light from experimental plants that heat exchangers remain almost free of incrustations at low mash temperatures.
In der Technik werden in anderen Prozessen häufig Bypaßleitungen am Wärmeaustauscher eingesetzt, um mittels geregelter Bypaßventile trotz inkrustierender Wärmeaustauscher die Wärmeübertragungsleistung des Systems nahezu konstant zu halten. Nachteilig sind jedoch die starke Überdimensionierung der Wärmeaustauscher für den sauberen Zustand sowie die Gefahr eines Flanschbläsers in heißgehenden Hochdruckleitungen, welche Bypässe mit großem Regelbereich haben.In other processes, bypass lines are often used in technology on the heat exchanger in order to keep the heat transfer capacity of the system almost constant by means of controlled bypass valves despite incrusting heat exchangers. However, the large overdimensioning of the heat exchangers for the clean state and the risk of a flange fan in hot high-pressure lines which have bypasses with a large control range are disadvantageous.
Für die Sumpfphasehydrierung mit integriertem Gasphasereaktor ist weiterhin zu berücksichtigen, daß mit zunehmender Laufzeit infolge der Desaktivierung des Gasphase-Katalysators die Temperatur der Gasphase-Einsatzstoffe angehoben werden muß (z. B. 390 Grad Celsius auf 430 Grad Celsius).For the bottom phase hydrogenation with an integrated gas phase reactor, it must also be taken into account that the temperature of the gas phase feedstocks has to be increased as the operating time increases due to the deactivation of the gas phase catalyst (e.g. 390 degrees Celsius to 430 degrees Celsius).
Bei den bekannten Verfahren wird keine Aussage darüber gemacht, wie bei zunehmender Inkrustierung der Wärmeaustauscher definierte Werte der Phasengleichgewichtstemperatur im Zwischenabscheider und der Eintrittstemperatur in die Gasphasehydrierung eingestellt werden können.In the known methods, no statement is made as to how defined values of the phase equilibrium temperature in the intermediate separator and the entry temperature into the gas phase hydrogenation can be adjusted with increasing incrustation of the heat exchanger.
Der Erfindung liegt die Aufgabe zugrunde, trotz zunehmender unvermeidbarer Inkrustierung der Wärmeaustauscher - insbesondere bei hohen Maischetemperaturen - eine definierte Einstellung der Phasengleichgewichtstemperatur im Zwischen-Abscheider und einen definierten Anstieg der Eintrittstemperatur der Gasphase-Einsatzstoffe mit zunehmender Laufzeit bei einer wirtschaftlichen Wärmerückgewinnung zu erreichen.The invention has for its object to achieve a defined setting of the phase equilibrium temperature in the intermediate separator and a defined increase in the inlet temperature of the gas phase feedstocks with increasing runtime with economic heat recovery despite increasing unavoidable incrustation of the heat exchanger - especially at high mash temperatures.
Diese Aufgabe wird erfindungsgemäß dadurch gelöst, daß zur Einstellung der definierten Phasengleichgewichtstemperatur im Zwischen-Abscheider die gasförmigen Hydrierprodukte aus der Sumpfphase in einem Maische-Wärmeaustauscher, einem Kopfkühler und einem Schlußkühler vor dem Zwischen-Abscheider gekühlt werden und die Aufheizung des kalten Maische-Hydriergasgemisches in Wärmeaustauschern durch indirekten Wärmeaustausch mit den heißen Hydrierprodukten aus der Gasphasehydrierung erfolgt.This object is achieved in that in order to set the defined phase equilibrium temperature in the intermediate separator, the gaseous hydrogenation products from the bottom phase are cooled in a mash heat exchanger, a head cooler and a final cooler in front of the intermediate separator and the heating of the cold mash-hydrogenation gas mixture in Heat exchangers are carried out by indirect heat exchange with the hot hydrogenation products from the gas phase hydrogenation.
Mit zunehmender Laufzeit muß die Temperatur der Gasphase-Einsatzstoffe allmählich angehoben werden. Dies erfolgt - ohne zusätzlichen Aufheizofen - erfindungsgemäß dadurch, daß mit fortschreitender Inkrustierung des Maische-Wärmeaustauschers auch das Temperaturniveau des Kopfkühlers vor dem Zwischenabscheider angehoben wird. Gleichzeitig wird hierdurch - bei zunehmender Verringerung der Wärmeübertragungsleistung des Maische-Wärmeaustauschers - die anfallende Abwärme aus der Sumpfphasehydrierung über den Weg der Gasphasehydrierung auf die vorgeschaltete Maischevorwärmung der Sumpfphasehydrierung übertragen und damit wirtschaftlich genutzt.As the running time increases, the temperature of the gas phase feedstocks must be raised gradually. This takes place - without an additional heating furnace - according to the invention in that the temperature level of the head cooler upstream of the intermediate separator is also increased as the mash heat exchanger progresses. At the same time, with increasing reduction in the heat transfer capacity of the mash heat exchanger, the waste heat generated from the bottom phase hydrogenation is transferred to the upstream mash preheating of the bottom phase hydrogenation via the path of gas phase hydrogenation and thus used economically.
Die Einstellung der gewünschten Temperatur im Zwischenabscheider erfolgt mittels Schlußkühler, in welchem zweckmäßig Dampf erzeugt oder Hydriergas vorgewärmt wird.The desired temperature in the intermediate separator is set by means of a final cooler, in which steam is expediently generated or hydrogenation gas is preheated.
Mit dem Kopfkühler hinter der Sumpfphasehydrierung kann zusätzlich das Temperaturniveau der in den Maische-Wärmeaustauscher eintretenden Sumpfphase-Gase/Dämpfe reduziert werden. Hierdurch verringert sich die sonst übliche schnelle Inkrustierung von sauberen Rohren des Maische-Wärmeaustauschers, da die max. auftretende Maischetemperatur (bei gleicher gemittelter Maischeaustrittstemperatur) gesenkt wird.With the head cooler behind the bottom phase hydrogenation, the temperature level of the bottom phase gases / vapors entering the mash heat exchanger can also be reduced. This reduces the usual fast incrustation of clean pipes of the mash heat exchanger, since the max. occurring mash temperature (at the same averaged mash outlet temperature) is reduced.
Mittels Kopfkühler (incl. Bypass) hinter der Sumpfphasehydrierung kann die gew+ünschte Temperatur der Einsatzstoffe der Gasphasehydrierung eingestellt werden.The desired temperature of the starting materials for the gas phase hydrogenation can be set by means of a head cooler (incl. Bypass) after the bottom phase hydrogenation.
Der Bypass um den Maische-Wärmeaustauscher dient zur Begrenzung der max. Maischeaustrittstemperatur des Maische-Wärmeaustauschers (speziell im sauberen Zustand der Wärmeaustauscher-Rohre).The bypass around the mash heat exchanger serves to limit the max. Mash outlet temperature of the mash heat exchanger (especially when the heat exchanger tubes are clean).
Mit dem o.g. Verfahren können somit alle prozeßrelevanten Temperaturen - auch bei zeitlich unabhängig fortschreitender Verschmutzung der Maische-Wärmeaustauscher sowie Desaktivierung des Gasphase-Katalysators - eingestellt werden.With the above-mentioned method, all process-relevant temperatures can thus be set, even if the mash heat exchanger progresses independently of time and the gas phase catalyst is deactivated.
Der Anfahrvorgang erfolgt zügig durch Aufheizung der Gasphase-Einsatzstoffe mittels Kopfkühler hinter der Sumpfphasehydrierung. An zwei Beispielen wird das Verfahren näher erläutert:The start-up process is carried out quickly by heating the gas phase feedstocks using a head cooler behind the bottom phase hydrogenation. The process is explained in more detail using two examples:
In der Zeichnung sind zwei Ausführungsbeispiele der Erfindung dargestellt.Two exemplary embodiments of the invention are shown in the drawing.
Anhand von Fig. 1 wird ein Betriebsfall nach kurzer Laufzeit - d. h. nur geringe Inkrustierung der Maische-Wärmeaustauscher 1 und 2 sowie frischer Katalysator des Gasphase-Reaktors 11 - beschrieben.1, an operating case after a short running time - d. H. only slight incrustation of the mash heat exchangers 1 and 2 and fresh catalyst of the gas phase reactor 11 - described.
Die gas- und dampfförmigen Produkte aus dem Sumpfphase-Reaktor 4 werden mittels Maische-Wärmeaustauscher 2 durch indirekten Wärmeaustausch teilweise abgekühlt, wobei auf der Aufheizseite das Maische-Hydriergasgemisch auf Anspringtemperatur der Sumpfphasehydrierung von ca. 440 °C aufgeheizt wird. Zwecks Einstellung der prozeßtechnisch vorgegebenen Temperatur von ca. 300 °C im Zwischenabscheider 9 werden die Sumpfphaseprodukte durch indirekten Wärmeaustausch in dem Kopfkühler 7 und in dem Schlußkühler 8 weiter abgekühlt. Im Zwischenabscheider 9 werden die Produkte aus der Sumpfphasehydrierung in den Lösungsmittelanteil (flüssig) und in den Feedstrom für die Gasphasehydrierung (Gase/Dämpfe) aufgeteilt. Letzterer wird im Kopfkühler 7 und dann im indirekten Wärmeaustauscher 10 auf Gasphase-Reaktionstemperatur von ca. 390 °C aufgeheizt.The gaseous and vaporous products from the bottom phase reactor 4 are partially cooled by means of mash heat exchanger 2 by indirect heat exchange, the mash-hydrogenation gas mixture being heated to the starting temperature of the bottom phase hydrogenation of approximately 440 ° C. on the heating side. In order to set the process temperature of approx. 300 ° C. in the
Die gasphase-Produkte werden durch indirekten Wärmeaustausch im Maische-Wärmeaustauscher 1 teilweise abgekühlt,
wodurch das Maische-Hydriergasgemisch vorgewärmt wird. Im indirekten Wärmeaustauscher 12 wird durch weitere Abkühlung der Gasphase-Produkte das Hydriergas vorgewärmt.
Im stationären Betriebsfall ist der Gesamtprozeß wärmeautark. Der Maische-Aufheizofen 3 dient nur als Anfahrofen.The gas phase products are partially cooled by indirect heat exchange in the mash heat exchanger 1,
whereby the mash-hydrogenation gas mixture is preheated. In the
The entire process is self-sufficient in stationary operation. The
Die Abwärme des Wärmeaustauschers 8 wird vorzugsweise zur Erzeugung von MD-Dampf oder zur Hydriergasvorwärmung verwendet. Mittels Kopfkühler 6 können die gas- und dampfförmigen ProdukteThe waste heat from the
aus dem Heißabscheider 5 vor Eintritt in den Maischevorwärmer 2 etwas abgekühlt werden. Auf diese Weise wird die Inkrustierung im Maische-Wärmeaustauscher reduziert.be cooled somewhat from the
Anhand von Fig. 2 wird ein Betriebsfall nach langer Laufzeit - d. h. starke Inkrustierung der Maische-Wärmeaustauscher 1 und 2 und desaktivierter Katalysator des Gasphase-Reaktors 11 - beschrieben. Infolge verminderter Wärmeübertragungsleistung des Maische-Wärmeaustauschers 2 wird die Feedtemperatur hinter dem Kopfkühler 7 gegenüber Beispiel 1 um ca. 20 °C angehoben. Die Gasphase-Eintrittstemperatur steigt auf ca. 425 °C an.2, an operating case after a long running time - d. H. strong incrustation of the mash heat exchanger 1 and 2 and deactivated catalyst of the gas phase reactor 11 - described. As a result of reduced heat transfer capacity of the mash heat exchanger 2, the feed temperature behind the head cooler 7 is increased by approximately 20 ° C. compared to example 1. The gas phase inlet temperature rises to approx. 425 ° C.
Claims (5)
- Process for suspension phase (semi-solid phase) hydrogenation with indirect gas phase hydrogenation, with defined temperature setting in the intermediate separator and in the gas phase reactor accompanied by economical heat recovery, characterized in that, for setting the defined phase equilibrium temperature in the intermediate separator, the gaseous hydrogenation products from the suspension phase are cooled in a slurry preheater, a head cooler and a final cooler upstream of the intermediate separator.
- Process according to Claim 1, characterized in that, for the purpose of defined temperature setting (intermediate separator), the waste heat of the suspension phase products is partly used in a head cooler connected behind the slurry heat exchanger for heating up the charge materials to the gas phase hydrogenation, so that the waste heat of the gas phase products can be economically used with high temperature level for the slurry preheating of the suspension phase hydrogenation.
- Process according to Claim 1, characterized in that, by means of head coolers behind the suspension phase hydrogenation, waste heat of the suspension phase products is used for heating up charge materials for the gas phase hydrogenation, in order on the one hand to start-up the gas phase hydrogenation and on the other hand to adjust the desired inlet temperature of the gas phase charge materials.
- Process according to Claim 1, characterized in that, for setting the slurry outlet temperature from the slurry heat exchanger, a head cooler behind the suspension phase hydrogenation and a bypass around the slurry preheater are used.
- Process according to Claim 1, characterized in that, for the purpose of setting the defined intermediate separator temperature, a final cooler is used, in which steam is generated or hydrogenation gas is preheated.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE3433625 | 1984-09-13 | ||
| DE3433625 | 1984-09-13 |
Publications (3)
| Publication Number | Publication Date |
|---|---|
| EP0177676A2 EP0177676A2 (en) | 1986-04-16 |
| EP0177676A3 EP0177676A3 (en) | 1988-03-02 |
| EP0177676B1 true EP0177676B1 (en) | 1992-03-04 |
Family
ID=6245308
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| EP85107962A Expired - Lifetime EP0177676B1 (en) | 1984-09-13 | 1985-06-27 | Process carried out by heat recuperation for suspension hydrogenation with integrated gas phase hydrogenation |
Country Status (8)
| Country | Link |
|---|---|
| US (1) | US4636300A (en) |
| EP (1) | EP0177676B1 (en) |
| JP (1) | JPS6172097A (en) |
| AU (1) | AU586430B2 (en) |
| CA (1) | CA1251753A (en) |
| DE (1) | DE3585485D1 (en) |
| PL (1) | PL255319A1 (en) |
| ZA (1) | ZA856989B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3741104A1 (en) * | 1987-12-04 | 1989-06-15 | Ruhrkohle Ag | METHOD FOR HYDROGENATING SOLID CARBON-CONTAINING SUBSTANCES |
| DE3741105A1 (en) * | 1987-12-04 | 1989-06-15 | Veba Oel Entwicklungs Gmbh | METHOD FOR HYDROGENATING LIQUID CARBONATED SUBSTANCES |
| DE102018108989A1 (en) | 2018-04-16 | 2019-10-17 | Thyssenkrupp Ag | Industrial plant with start-up furnace and method for initiating chemical reactions |
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| DE3042984C2 (en) * | 1980-11-14 | 1986-06-26 | Saarbergwerke AG, 6600 Saarbrücken | Process for hydrogenating coal |
| DE3101598A1 (en) * | 1981-01-20 | 1982-08-26 | Basf Ag, 6700 Ludwigshafen | METHOD FOR HYDROGENATING COAL |
| US4400263A (en) * | 1981-02-09 | 1983-08-23 | Hri, Inc. | H-Coal process and plant design |
| DE3105030A1 (en) * | 1981-02-12 | 1982-09-02 | Basf Ag, 6700 Ludwigshafen | METHOD FOR THE CONTINUOUS PRODUCTION OF HYDROCARBON OILS FROM COAL BY PRESSURE HYDROGENATION IN TWO STAGES |
| DE3133562C2 (en) * | 1981-08-25 | 1987-01-15 | Fried. Krupp Gmbh, 4300 Essen | Process for the production of liquid hydrocarbons by catalytic hydrogenation of coal in the presence of water |
| DE3141380C2 (en) * | 1981-10-17 | 1987-04-23 | GfK Gesellschaft für Kohleverflüssigung mbH, 6600 Saarbrücken | Process for hydrogenating coal |
| US4406744A (en) * | 1981-11-16 | 1983-09-27 | Clyde Berg | Process for the production of hydrogenated tar and distillates and low sulfur coke from coal |
| US4411765A (en) * | 1982-02-10 | 1983-10-25 | Electric Power Development Co. | Method for liquefying low rank coal |
| US4387015A (en) * | 1982-09-30 | 1983-06-07 | International Coal Refining Company | Coal liquefaction quenching process |
| DE3300365A1 (en) * | 1983-01-07 | 1984-07-12 | Veba Oel Entwicklungsgesellschaft mbH, 4660 Gelsenkirchen-Buer | METHOD FOR SMELLING HYDRATION RESIDUES |
| DE3311552A1 (en) * | 1983-03-30 | 1984-10-04 | Veba Oel Entwicklungsgesellschaft mbH, 4660 Gelsenkirchen-Buer | METHOD FOR HYDROGENATING COAL |
-
1985
- 1985-06-27 EP EP85107962A patent/EP0177676B1/en not_active Expired - Lifetime
- 1985-06-27 DE DE8585107962T patent/DE3585485D1/en not_active Expired - Lifetime
- 1985-07-12 AU AU44854/85A patent/AU586430B2/en not_active Ceased
- 1985-09-11 PL PL25531985A patent/PL255319A1/en unknown
- 1985-09-12 CA CA000490562A patent/CA1251753A/en not_active Expired
- 1985-09-12 ZA ZA856989A patent/ZA856989B/en unknown
- 1985-09-12 JP JP60200719A patent/JPS6172097A/en active Granted
- 1985-09-13 US US06/775,920 patent/US4636300A/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| PL255319A1 (en) | 1986-08-12 |
| JPS6172097A (en) | 1986-04-14 |
| AU4485485A (en) | 1986-03-20 |
| AU586430B2 (en) | 1989-07-13 |
| US4636300A (en) | 1987-01-13 |
| DE3585485D1 (en) | 1992-04-09 |
| CA1251753A (en) | 1989-03-28 |
| JPH0569157B2 (en) | 1993-09-30 |
| ZA856989B (en) | 1986-04-30 |
| EP0177676A2 (en) | 1986-04-16 |
| EP0177676A3 (en) | 1988-03-02 |
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