EP0151399A2 - Hydrogen gas distribution in coal liquefaction plants - Google Patents
Hydrogen gas distribution in coal liquefaction plants Download PDFInfo
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- EP0151399A2 EP0151399A2 EP85100277A EP85100277A EP0151399A2 EP 0151399 A2 EP0151399 A2 EP 0151399A2 EP 85100277 A EP85100277 A EP 85100277A EP 85100277 A EP85100277 A EP 85100277A EP 0151399 A2 EP0151399 A2 EP 0151399A2
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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
- the invention relates to a hydrogenation gas flow in coal liquefaction plants, light and medium oil obtained after the hydrogenation being refined.
- Dried coal is usually mashed with solvent and hydrogenated with the addition of hydrogen.
- the reaction products are separated in the separators downstream of the hydrogenation reactors. Gases and vapors are drawn off overhead in the hot separator; a liquid phase, which contains the solids, is removed from the sump into the vacuum distillation.
- the top product of the hot separator is fed to the downstream cold separator. Together with the KOHLEUL, water is obtained as the liquid phase, from which the valuable ingredients (ammonia, phenol) are obtained in subsequent process stages.
- the overhead gas phase of the cold separator is put into circulation and discharge gas after an oil wash carried out under process pressure.
- the circuit oas is returned to the hvdrieruno with a circuit aa compressor after the pressure has been lost.
- the Ausschleusoas is ⁇ reiniot in a gas scrubber and in a Tieftem D eratur- zerleounasanlaae in hydrogen, fuel gas, LPG and SNG disassembled.
- the hydrogen fraction is mixed with the fresh hydrogen from the hydrogenation.
- the COAL OIL In atmospheric distillation, the COAL OIL is separated into light, medium and heavy oil.
- the heavy oil is returned as a solvent to the mashing mixture.
- the light and medium oil fractions are each subjected to a hydrogenating refining in order to remove sulfur, nitrogen and similar undesirable additives. This is done after adding water
- the raw light or raw medium oil evaporates and is introduced into fixed bed reactors. Refining is carried out on the Co-Mo or Ni-Mo catalyst layers.
- hydrogen fluoride is introduced into the hydrogenation reactors.
- the emerging refined products are cooled in heat exchangers and single-seated by fresh water and separated into raffinate, water and gas in separators.
- the state of the art is to return a portion of the H 2 -rich excess gas to the fresh hydrogen for refining as a recycle gas after compensation for the pressure loss with a recycle gas compressor and to discharge the other excess gas portion for cleaning and recovery of the hydrogen and the gaseous hydrocarbons and to supply appropriate process stages.
- the solid-containing residue of the hot separator is topped in a vacuum distillation.
- the heavy oil obtained is together with heavy and medium oil from the atm. Distillation as a solvent returned to the mash.
- Synthesis gas (CO + H x ) is obtained from the residue from the vacuum distillation in a gasification stage or, after conversion and gas scrubbing, hydrogen hydrogen.
- the deficit can be covered by coal gasification with downstream conversion and gas cleaning or external supply.
- the invention has for its object to simplify the Hydrierqas Office and improve it economically.
- this is achieved in that the total amount of gases obtained in the refining stages (20 + 21) is fed to the fresh hydrogen for hydrogenation.
- the organic (C 1 -C 4 ) and inorganic (CO, CO 2 , H 2 S) gaseous compounds contained in the gas in addition to the hydrogen produced during refining impair the hydrogenation of the coal in the present concentration
- they are discharged or extracted with the same gaseous compounds that are additionally formed during the hydrogenation of the coal via gas scrubbing and low-temperature separation.
- the hydrogenation gas guide according to the invention is shown in the form of a flow diagram.
- Dried coal is mashed with solvent in a slurry (1) and hydrogenated in a reactor (2) with the addition of hydrogen.
- a phase separation is carried out in the hot separator (3) downstream of the hydrogenation reactor (2).
- the gases and vapors are drawn off overhead.
- a liquid phase, which contains the solids, is removed from the sump into the vacuum distillation (5).
- the top product of the hot separator is passed into the cold separator (4).
- water is produced here, which is pumped off separately to recover valuable ingredients (ammonia, phenol).
- the KOHLEOL is drawn off and atmospheric with the addition of stripping steam in one atm. Distillation (6) distilled. Light and medium oil of atm. Distillation is fed to separate refining stages (21 and 22).
- the gas phase leaving the cold separator at the top is divided in an oil scrubber (7) into recirculated and discharged gas.
- the discharge gas is cleaned in a gas scrubber (8) and broken down into hydrogen, heating gas, SNG and LPG in a low-temperature separation plant (9).
- the solid-containing liquid phase obtained in the hot separator is topped in vacuum distillation (5).
- the resulting heavy oil is extracted from the atm together with heavy and medium oil. Distillation as solvent in the slurry (1).
- Hydrogen hydrogen is obtained from the residue from the vacuum distillation in a gasification stage (10) synthesis gas (CO + H z ) or in a conversion and gas scrubbing (11).
- the cycle gas obtained from the ul wash (7) is compressed to the necessary operating pressure by a cycle gas compressor (27).
- the total amount of hydrogen-rich gases emerging from the refining stages (21 + 22) is fed in again. These gases are fed as a mixture to the hydrogenation (2) and compressed by a compressor (28) to the operating pressure required for the hydrogenation.
- the raw light oil is refined in two stages with the addition of 3,138 kg / h (stage I) and 2,587 kg / h (stage II) hydrogen with a purity of 98.5% by volume at 60 bar.
- stage I 3,138 kg / h
- stage II 2,587 kg / h
- hydrogen-rich gas phase total amount 5,629 kg / h
- This amount of gas is fed directly to the hydrogenation gas.
- the raw oil is refined in one step with the addition of 9,873 kg / h of hydrogen (98.5% by volume), also at 60 bar.
- the gas produced in the downstream separator (9,565 kg / h is in turn fed directly to the coal hydrogenation.
- the hydrogen content of the hydrogenation gas flowing through the refining stages drops to 98.0 vol.% In the case of the light oil or to 97.5 vol .% for middle oil.
- H 2 partial pressures are significantly higher than that of the hydrogenation gas from the coal hydrogenation (216,252 kg / h, 85% by volume), so that feeding is possible without problems.
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- 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)
Abstract
Description
Die Erfindung betrifft eine Hydriergasführung in Kohleverflüssigungsanlagen, wobei nach der Hydrierung gewonnenes Leicht- und Mittelöl einer Raffination unterzogen wird.The invention relates to a hydrogenation gas flow in coal liquefaction plants, light and medium oil obtained after the hydrogenation being refined.
Oblicherweise wird getrocknete Kohle mit Lösungsmittel angemaischt und unter Zugabe von Wasserstoff hydriert. In den den Hydrierreaktoren nachgeschalteten Abscheidern erfolgt eine Trennung der Reaktionsprodukte. Im Heißabscheider werden Gase und Dämpfe über Kopf abgezogen; aus dem Sumpf wird eine - die Feststoffe enthaltene Flüssigphase - in die Vakuumdestillation abgeführt.Dried coal is usually mashed with solvent and hydrogenated with the addition of hydrogen. The reaction products are separated in the separators downstream of the hydrogenation reactors. Gases and vapors are drawn off overhead in the hot separator; a liquid phase, which contains the solids, is removed from the sump into the vacuum distillation.
Das Kopfprodukt des Heißabscheiders wird nach Abkühlung dem nachgeschalteten Kaltabscheider zugeleitet. Zusammen mit dem KOHLEUL fällt hier als flüssige Phase Wasser an, aus dem die wertvollen Inhaltsstoffe (Ammoniak, Phenol) in nachfolgenden Prozeßstufen gewonnen werden.After cooling, the top product of the hot separator is fed to the downstream cold separator. Together with the KOHLEUL, water is obtained as the liquid phase, from which the valuable ingredients (ammonia, phenol) are obtained in subsequent process stages.
Die über Kopf abgehende Gasphase des Kaltabscheiders wird nach einer unter Prozeßdruck vollzogenen Ölwäsche in Kreislauf- und Ausschleusgas aufætellt. Das Kreislaufoas wird nach Ausoleich des Druckverlustes mit einem Kreislaufaaskomoressor in die Hvdrieruno zurückgeführt. Das Ausschleusoas wird in einer Gaswäsche æreiniot und in einer TieftemDeratur- zerleounasanlaae in Wasserstoff, Heizgas, SNG und LPG zerlegt. Die Wasserstoff-Fraktion wird dem Frischwasserstoff der Hydrierung zugemischt.The overhead gas phase of the cold separator is put into circulation and discharge gas after an oil wash carried out under process pressure. The circuit oas is returned to the hvdrieruno with a circuit aa compressor after the pressure has been lost. The Ausschleusoas is æreiniot in a gas scrubber and in a Tieftem D eratur- zerleounasanlaae in hydrogen, fuel gas, LPG and SNG disassembled. The hydrogen fraction is mixed with the fresh hydrogen from the hydrogenation.
In der atmosphärischen Destillation wird das KOHLEÖL in Leicht-, Mittel-und Schweröl ætrennt. Das Schweröl wird als LösunQsmittel zur Anmaischuna zurückaeführt.In atmospheric distillation, the COAL OIL is separated into light, medium and heavy oil. The heavy oil is returned as a solvent to the mashing mixture.
Die Leicht- und Mittelölfraktionen werden zur Entfernung von Schwefel, Stickstoff und ähnlichen unerwünschten Beqleitstoffen jeweils einer hydrierenden Raffination unterworfen. Hierzu wird nach Zuqabe von Wasserstoff das Rohleicht- bzw. Rohmittelöl verdampft und in Festbettreaktoren eingeleitet. An den Co-Mo- bzw. Ni-Mo-Katalysatorschichten wird die Raffination durchgeführt. Um den Temperaturanstieg, bedingt durch die Reaktionswärme der Hydrierung, einzugrenzen, wird in die Hydrierreaktoren Ouenchwasserstoff einæschleust. Die austretenden raffinierten Produkte werden in Wärmeaustauschern und durch Einsoritzen von Ouenchwasser abgekühlt und in Abscheidern in Raffinat, Wasser und Gas getrennt. Stand der Technik ist, einen Teil des H2-reichen Oberschußgases zum Frischwasserstoff der Raffination als Kreislaufgas nach Ausgleich des Druckverlustes mit einem Kreislaufgaskompressor zurückzufahren und den anderen Oberschußgasanteil zur Reinigung und Rückgewinnung des Wasserstoffs und der gasförmigen Kohlenwasserstoffe auszuschleusen und entsprechenden Verfahrensstufen zuzuführen.The light and medium oil fractions are each subjected to a hydrogenating refining in order to remove sulfur, nitrogen and similar undesirable additives. This is done after adding water The raw light or raw medium oil evaporates and is introduced into fixed bed reactors. Refining is carried out on the Co-Mo or Ni-Mo catalyst layers. In order to limit the rise in temperature due to the heat of reaction of the hydrogenation, hydrogen fluoride is introduced into the hydrogenation reactors. The emerging refined products are cooled in heat exchangers and single-seated by fresh water and separated into raffinate, water and gas in separators. The state of the art is to return a portion of the H 2 -rich excess gas to the fresh hydrogen for refining as a recycle gas after compensation for the pressure loss with a recycle gas compressor and to discharge the other excess gas portion for cleaning and recovery of the hydrogen and the gaseous hydrocarbons and to supply appropriate process stages.
Der feststoffhaltige Rückstand des Heißabscheiders wird in einer Vakuumdestillation getoppt. Das gewonnene Schweröl wird zusammen mit Schwer- und Mittelöl aus der atm. Destillation als Lösungsmittel in die Anmaischung zurückgefahren. Aus dem Rückstand der Vakuumdestillation wird in einer Vergasungsstufe Synthesegas (CO + Hx) bzw. nach Konvertierung und Gaswäsche Hydrierwasserstoff gewonnen.The solid-containing residue of the hot separator is topped in a vacuum distillation. The heavy oil obtained is together with heavy and medium oil from the atm. Distillation as a solvent returned to the mash. Synthesis gas (CO + H x ) is obtained from the residue from the vacuum distillation in a gasification stage or, after conversion and gas scrubbing, hydrogen hydrogen.
Reicht der über Rückstandsvergasung, Tieftemperaturzerlegung und Kreislaufgas gewonnene bzw. rückgeführte Wasserstoff für Hydrierung und Stabilisierung nicht aus, kann über eine Kohlevergasung mit nachgeschalteter Konvertierung und Gasreinigung oder externen Bezug das Defizit gedeckt werden.If the hydrogen obtained via residue gasification, low-temperature decomposition and recycle gas is not sufficient for hydrogenation and stabilization, the deficit can be covered by coal gasification with downstream conversion and gas cleaning or external supply.
Der Erfindung liegt die Aufgabe zugrunde die Hydrierqasführung zu vereinfachen und wirtschaftlich zu verbessern.The invention has for its object to simplify the Hydrierqasführung and improve it economically.
Nach der Erfindunq wird das dadurch erreicht, daß die Gesamtmenge der in den Raffinationsstufen (20 + 21) anfallenden Gase dem Frischwasserstoff der Hydrierung zugeführt werden. D.h. es wird keine Aufteilung des aus den Raff.stufen austretenden, wasserstoffreichen Gases in Kreislauf- und Oberschußgas vorgenommen, sondern der Gesamtmenge der Hydrierung zugeführt. Die im Gas neben dem Wasserstoff enthaltenen, bei der Raffination entstehenden organischen (C1-C4) und anorganischen (CO, CO2, H2S) gasförmigen Verbindungen beeinträchtigen in der vorliegenden Konzentration die Hydrierung der Kohle Entsprechend der Aufteilung der Gasphase des Kaltabscheiders in -Kreislauf- und Ausschleusgas werden sie mit den zusätzlich bei der Hydrierung der Kohle entstehenden, gleichen gasförmigen Verbindungen über die Gaswäsche und Tieftemperaturzerlegung ausgeschleust bzw. gewonnen.According to the invention, this is achieved in that the total amount of gases obtained in the refining stages (20 + 21) is fed to the fresh hydrogen for hydrogenation. This means that there is no division of the hydrogen-rich gas emerging from the refining stages into circulating and excess gas, but instead the total amount of the hydrogenation is supplied. The organic (C 1 -C 4 ) and inorganic (CO, CO 2 , H 2 S) gaseous compounds contained in the gas in addition to the hydrogen produced during refining impair the hydrogenation of the coal in the present concentration In accordance with the division of the cold separator's gas phase into circulation and discharge gas, they are discharged or extracted with the same gaseous compounds that are additionally formed during the hydrogenation of the coal via gas scrubbing and low-temperature separation.
Der Fortfall eigener Kreislaufgaskompressoren, Gaswäscher und Wasserstoffrückgewinnungsstufen für die Raffination des Leicht- und Mittelöls bedeutet ein wesentlicher Vorteil für Investition und Betrieb.The elimination of our own cycle gas compressors, gas scrubbers and hydrogen recovery stages for the refining of light and medium oil means a significant advantage for investment and operation.
In der Zeichnung ist die erfindungsgemäße Hydriergasführung in Form eines Fließschemas-dargestellt.In the drawing, the hydrogenation gas guide according to the invention is shown in the form of a flow diagram.
Getrocknete Kohle wird mit Lösungsmittel in einer Anmaischung (1) angemaischt und unter Zugabe von Wasserstoff in einem Reaktor (2) hydriert. In dem dem Hydrierreaktor (2) nachgeschalteten Heißabscheider (3), wird eine Phasentrennung durchgeführt. Die Gase und Dämpfe werden über Kopf abgezogen. Aus dem Sumpf wird eine - die Feststoffe enthaltene Flüssigphase - in die Vakuumdestillation (5) abgeführt.Dried coal is mashed with solvent in a slurry (1) and hydrogenated in a reactor (2) with the addition of hydrogen. A phase separation is carried out in the hot separator (3) downstream of the hydrogenation reactor (2). The gases and vapors are drawn off overhead. A liquid phase, which contains the solids, is removed from the sump into the vacuum distillation (5).
Das Kopfprodukt des Heißabscheiders wird nach Abkühlung in den Kaltabscheider (4) geleitet. Neben KOHLEUL fällt hier Wasser an, das getrennt zur Wiedergewinnung von wertvollen Inhaltstoffen (Ammoniak, Phenol) abgepumpt wird.After cooling, the top product of the hot separator is passed into the cold separator (4). In addition to KOHLEUL, water is produced here, which is pumped off separately to recover valuable ingredients (ammonia, phenol).
Das KOHLEOL wird abgezogen und atmosphärisch unter Zugabe von Strippdampf in einer atm. Destillation (6) destilliert. Leicht- und Mittelöl der atm. Destillation werden jeweils getrennt Raffinationsstufen (21 und 22) zugeführt.The KOHLEOL is drawn off and atmospheric with the addition of stripping steam in one atm. Distillation (6) distilled. Light and medium oil of atm. Distillation is fed to separate refining stages (21 and 22).
Die über Kopf aus dem Kaltabscheider abgehende Gasphase wird in einer Ölwäsche (7) in rückgeführtes Kreislauf- und Ausschleusgas aufgeteilt. Das Ausschleusgas wird in einer Gaswäsche (8) gereinigt und in einer Tieftemperaturzerlegungsanlage ( 9) in Wasserstoff, Heizgas, SNG und LPG zerlegt.The gas phase leaving the cold separator at the top is divided in an oil scrubber (7) into recirculated and discharged gas. The discharge gas is cleaned in a gas scrubber (8) and broken down into hydrogen, heating gas, SNG and LPG in a low-temperature separation plant (9).
Die im Heißabscheider anfallende feststoffhaltige Flüssigphase wird in der Vakuumdestillation (5) getoppt. Das dabei gewonnene Schweröl wird zusammen mit Schwer- und Mittelöl aus der atm. Destillation als Lösungsmittel in die Anmaischung (1) zurückgefahren.The solid-containing liquid phase obtained in the hot separator is topped in vacuum distillation (5). The resulting heavy oil is extracted from the atm together with heavy and medium oil. Distillation as solvent in the slurry (1).
Aus dem Rückstand der Vakuumdestillation wird in einer Vergasungsstufe (10) Synthesegas (CO + Hz) bzw. in einer Konvertierung und Gaswäsche (11) Hydrierwasserstoff gewonnen.Hydrogen hydrogen is obtained from the residue from the vacuum distillation in a gasification stage (10) synthesis gas (CO + H z ) or in a conversion and gas scrubbing (11).
Reicht der über Kreislaufgas, Tieftemperaturzerlegung (9), Rückstands. vergasung (10) rückgefuhrte Wasserstoff für die Hydrierung nicht aus, so wird über eine zusätzliche Kohlevergasung (12) mit nachgeschaltetel Konvertierung und Gaswäsche (13) das Defizit abgedeckt.Is that enough about recycle gas, low temperature decomposition (9), residue. gasification (10) recycled hydrogen for the hydrogenation, so the deficit is covered by an additional coal gasification (12) with downstream conversion and gas scrubbing (13).
Die teersäurehaltigen Abwässer des Kaltabscheider der atm. Destillation werden einer Ammoniakgewinnung (23) und einer Phenolgewinnung (24) zugeführt. Die Abwässer werden nach biologischer Aufbereitung (25) in das öffentliche Abwassernetz eingeleitet. Desgleichen erfolgt eine Ableitung der bei der Vergasung (12) anfallenden Abwässer sowie der aus der Rückstandsvergasung (10) anfallenden Abwässer nach Neutralisation (26) in das öffentliche Abwassernetz.The tar-containing wastewater from the atmospheric cold separator. Distillation is fed to an ammonia recovery (23) and a phenol recovery (24). After biological treatment (25), the wastewater is discharged into the public wastewater network. Likewise, the wastewater from gasification (12) and the wastewater from residue gasification (10) are discharged into the public sewage network after neutralization (26).
Das aus der Ulwäsche (7) anfallende Kreislaufgas wird über einen Kreisgaskompressor (27) auf den notwendigen Betriebsdruck verdichtet. Zusätzlich zum Kreislaufgas und den aus der Tieftemperaturzerlegung (9) anfallenden Frischwasserstoff wird die Gesamtmenge der aus den Raffinationsstufen (21 + 22) austretenden wasserstoffreichen Gase wieder zugeführt. Diese Gase werden in Mischung der Hydrierung (2) zugeführt und von einem Verdichter (28) auf den für die Hydrierung notwendigen Betriebsdruck verdichtet.The cycle gas obtained from the ul wash (7) is compressed to the necessary operating pressure by a cycle gas compressor (27). In addition to the cycle gas and the fresh hydrogen obtained from the low-temperature decomposition (9), the total amount of hydrogen-rich gases emerging from the refining stages (21 + 22) is fed in again. These gases are fed as a mixture to the hydrogenation (2) and compressed by a compressor (28) to the operating pressure required for the hydrogenation.
In der Kohleverflüssigungsanlage zur Hydrierung einer im Ruhrgebiet geförderten Gasflammkohle mit einem Durchsatz von 5 000 t (waf) Kohle/d, fallen entsprechend einer Stundenleistung von ca. 208 t/h in der atmosphärischen Destillation 31.833 kg/h Rohleicht- und 64.006 kg/h Rohmittelöl an.In the coal liquefaction plant for the hydrogenation of a gas flame coal extracted in the Ruhr area with a throughput of 5,000 t (waf) coal / d, 31,833 kg / h of raw light and 64,006 kg / h fall in the atmospheric distillation, corresponding to an hourly output of approx. 208 t / h Crude oil.
Die Raffination des Rohleichtöles erfolgt zweistufig unter Zugabe von 3.138 kg/h (Stufe I) und 2.587 kg/h (Stufe II) Wasserstoff mit einer Reinheit von 98,5 Vol. % bei 60 bar. In den Raffinationsreaktoren nachgeschalteten Abscheidern erfolgt eine Abtrennung der wasserstoffreichen Gasphase (Gesamtmenge 5.629 kg/h) vom Hydrierprodukt bei 55 bar. Diese Gasmenge wird dem Hydriergas direkt zugeführt.The raw light oil is refined in two stages with the addition of 3,138 kg / h (stage I) and 2,587 kg / h (stage II) hydrogen with a purity of 98.5% by volume at 60 bar. In the separators connected downstream of the refining reactors, the hydrogen-rich gas phase (total amount 5,629 kg / h) is separated from the hydrogenation product at 55 bar. This amount of gas is fed directly to the hydrogenation gas.
Die Raffination des Rohmittelöles erfolgt einstufig unter Zugabe von 9.873 kg/h Wasserstoff (98,5 Vol.%) ebenfalls bei 60 bar. Das im nachgeschalteten Abscheider anfallende Gas (9.565 kg/h wird wiederum der Kohlehydrierung direkt zugeführt.The raw oil is refined in one step with the addition of 9,873 kg / h of hydrogen (98.5% by volume), also at 60 bar. The gas produced in the downstream separator (9,565 kg / h is in turn fed directly to the coal hydrogenation.
Durch Anreicherung an C1- C4 - Kohlenwasserstoffgasanteilen sowie an CO-, C02 und H2S-Mengen sinkt der Wasserstoffgehalt des durch die Raffinationsstufen strömenden Hydriergases auf 98,0 Vol.% im Falle des Leichtöles bzw. auf 97,5 Vol.% beim Mittelöl.By enriching in C 1 - C 4 - hydrocarbon gas fractions as well as in CO, C0 2 and H 2 S quantities, the hydrogen content of the hydrogenation gas flowing through the refining stages drops to 98.0 vol.% In the case of the light oil or to 97.5 vol .% for middle oil.
Diese H2-Partialdrücke liegen wesentlich über dem des Hydriergases der Kohlehydrierung (216.252 kg/h, 85 Vol.%) , so daß eine Zuspeisung unproblematisch möglich ist.These H 2 partial pressures are significantly higher than that of the hydrogenation gas from the coal hydrogenation (216,252 kg / h, 85% by volume), so that feeding is possible without problems.
Claims (1)
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19843401650 DE3401650A1 (en) | 1983-12-10 | 1984-01-19 | Hydrogenation gas arrangement in coal liquefaction plants |
| DE3401650 | 1984-01-19 |
Publications (3)
| Publication Number | Publication Date |
|---|---|
| EP0151399A2 true EP0151399A2 (en) | 1985-08-14 |
| EP0151399A3 EP0151399A3 (en) | 1987-05-13 |
| EP0151399B1 EP0151399B1 (en) | 1989-08-02 |
Family
ID=6225291
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| EP85100277A Expired EP0151399B1 (en) | 1984-01-19 | 1985-01-12 | Hydrogen gas distribution in coal liquefaction plants |
Country Status (10)
| Country | Link |
|---|---|
| EP (1) | EP0151399B1 (en) |
| JP (1) | JPS60161483A (en) |
| AU (1) | AU582133B2 (en) |
| BR (1) | BR8500578A (en) |
| CA (1) | CA1239366A (en) |
| DD (1) | DD236340A5 (en) |
| DE (1) | DE3572001D1 (en) |
| PL (1) | PL141658B1 (en) |
| SU (1) | SU1473714A3 (en) |
| ZA (1) | ZA85428B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3519830A1 (en) * | 1985-06-03 | 1986-12-18 | Ruhrkohle Ag, 4300 Essen | METAL OF COAL HYDRATION WITH INTEGRATED REFINING STAGES |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3141649A1 (en) * | 1981-02-09 | 1982-09-30 | Hydrocarbon Research Inc., 08648 Lawrenceville, N.J. | METHOD FOR CONVERTING COAL AND / OR OTHER HYDROCARBONS TO VALUABLE LIQUID PRODUCTS |
| GB2121817A (en) * | 1982-06-17 | 1984-01-04 | Chevron Res | Two-stage hydroprocessing of heavy oils |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4179352A (en) * | 1975-08-07 | 1979-12-18 | Exxon Research & Engineering Co. | Coal liquefaction process |
| JPS5681390A (en) * | 1979-12-07 | 1981-07-03 | Chiyoda Chem Eng & Constr Co Ltd | Multistage hydrogenation treatment of coal |
-
1985
- 1985-01-12 EP EP85100277A patent/EP0151399B1/en not_active Expired
- 1985-01-12 DE DE8585100277T patent/DE3572001D1/en not_active Expired
- 1985-01-16 JP JP60004178A patent/JPS60161483A/en active Pending
- 1985-01-16 AU AU37720/85A patent/AU582133B2/en not_active Ceased
- 1985-01-17 PL PL1985251583A patent/PL141658B1/en unknown
- 1985-01-18 CA CA000472170A patent/CA1239366A/en not_active Expired
- 1985-01-18 SU SU853837677A patent/SU1473714A3/en active
- 1985-01-18 ZA ZA85428A patent/ZA85428B/en unknown
- 1985-01-18 DD DD85272651A patent/DD236340A5/en unknown
- 1985-02-08 BR BR8500578A patent/BR8500578A/en unknown
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3141649A1 (en) * | 1981-02-09 | 1982-09-30 | Hydrocarbon Research Inc., 08648 Lawrenceville, N.J. | METHOD FOR CONVERTING COAL AND / OR OTHER HYDROCARBONS TO VALUABLE LIQUID PRODUCTS |
| GB2121817A (en) * | 1982-06-17 | 1984-01-04 | Chevron Res | Two-stage hydroprocessing of heavy oils |
Also Published As
| Publication number | Publication date |
|---|---|
| DD236340A5 (en) | 1986-06-04 |
| ZA85428B (en) | 1986-04-30 |
| AU3772085A (en) | 1985-07-25 |
| JPS60161483A (en) | 1985-08-23 |
| BR8500578A (en) | 1985-09-24 |
| EP0151399A3 (en) | 1987-05-13 |
| PL251583A1 (en) | 1985-11-05 |
| PL141658B1 (en) | 1987-08-31 |
| AU582133B2 (en) | 1989-03-16 |
| CA1239366A (en) | 1988-07-19 |
| EP0151399B1 (en) | 1989-08-02 |
| SU1473714A3 (en) | 1989-04-15 |
| DE3572001D1 (en) | 1989-09-07 |
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