EP0237702B1 - Process for the continuous coking of pitches, and use of the coke obtained - Google Patents
Process for the continuous coking of pitches, and use of the coke obtained Download PDFInfo
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- EP0237702B1 EP0237702B1 EP87100270A EP87100270A EP0237702B1 EP 0237702 B1 EP0237702 B1 EP 0237702B1 EP 87100270 A EP87100270 A EP 87100270A EP 87100270 A EP87100270 A EP 87100270A EP 0237702 B1 EP0237702 B1 EP 0237702B1
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- Prior art keywords
- coking
- pitch
- coke
- pitches
- weight
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B55/00—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material
Definitions
- the invention relates to a method for the continuous coking of pitches, in particular hard coal tar pitches, and the use of the coke obtained by this method.
- the process according to a) is high-temperature coking and, apart from a few special features, corresponds to the known coal coking process.
- a hard coal tar pitch with a coking residue according to Brockmann-Muck of more than 50% is used as the input product.
- the coke obtained is very hard and generally does not need to be calcined because of the high coking temperature of at least 1000 ° C.
- the process is very labor-intensive. Because of the different physical and chemical properties of the hard pitch, the plants, in particular the brick lining, are much more susceptible to repair than those of coal than those of coal coking.
- the process itself is discontinuous, so that a large number of chambers are necessary in order to enable quasi-continuous operation.
- the process according to b) is a smoldering process at around 500 ° C.
- hard coal tar soft pitches are also used.
- the delayed coker was originally operated as a thermal cracker. However, it was soon recognized that it is an excellent device for producing highly anisotropic special cokes.
- the smoldering coke obtained must be dried and calcined for further use. The plant costs are high, so that profitability is only given in the production of particularly high-quality coke or valuable oils. This is usually not the case with untreated coal tar pitch.
- the method itself can be carried out quasi-continuously with at least two coker drums.
- the process according to c) is also a smoldering process, but is carried out continuously.
- the fluid coker is a thermal cracker for mineral oil residues.
- the coke generated as a waste product is used as fuel. This process is less suitable for coal tar pitches because of the low oil and gas yield.
- the object of the invention is therefore to develop a simple, inexpensive process for the coking of hard coal tar pitches and comparable products and to find suitable fields of application for the coke thus produced.
- the object is achieved in that the hard pitch is coked in a rotary tube furnace provided with a broaching tool and heated from the outside at temperatures of the inner wall between 500 and 800 ° C. and a residence time of 0.5 to 1.5 hours, the resulting gases and Vapors are passed in countercurrent to the coking pitch, and the smoldering coke obtained is then calcined in the usual manner, preferably without prior cooling.
- Aromatic residues with a softening point (EP) according to Kraemer-Sarnow (K.-S.) of at least 130 ° C and a coking residue according to Brockmann-Muck (B.-M.) of at least 45% by weight are referred to as hard pitch.
- E softening point
- K.-S. Kraemer-Sarnow
- B.-M. coking residue
- the rotary kiln should advantageously be divided into several sections that can be heated differently. The segments facing the feed side are heated to an outside temperature of approximately 850 ° C. by external heating. The outside temperature of the following sections can then drop to around 600 ° C.
- the gases and vapors are conducted in countercurrent to the coking pitch.
- the vapors are condensed after leaving the rotary kiln and can be used as a soot oil component or can be used for hard pitch production.
- the feeding of an inert gas on the discharge side of the rotary kiln has proven to be helpful. This shortens the dwell time of the vapors in the coking zone and prevents soot formation and deposits in the subsequent vapor lines.
- a screw that is conical towards the feed side and weighted with granular material has proven itself, which is at least about 1/3, preferably 1/2 times as long as the rotary tube and its inclination is greater than that of the rotary tube.
- the broaching tool is preferably self-centering and is moved non-positively by the drum.
- the pitch can be introduced in pieces, for example via a rotary valve, or in liquid form in the rotary kiln.
- the smoked coke is discharged in pieces via another rotary valve and can be fed directly to the calciner. Since there is no need to cool the coke with water in the coking processes a) and b), considerably less time and energy is required for the calcination.
- Rotary kilns are known to be used for the coking or calcination of solid fuels such as smoked coke and lignite or for the pyrolysis of predominantly solid waste
- solid fuels such as smoked coke and lignite
- pyrolysis of predominantly solid waste
- a rotary kiln with an inner diameter of 0.8 m and a heated length of 7.2 m with a 4 m long conical screw in the front part, 75 kg / h of a hard coal tar pitch with an EP (K.-S.) of 150 ° C and a coking residue (B.-M.) of 50%.
- the oven is divided into 6 sections, which are heated indirectly with gas.
- the temperature of the outer wall in the area of the inlet is 850 ° C and drops to 700 ° C towards the outlet.
- the pipe wall outside temperature is approximately 800 ° C on average over the individual heating zones.
- the rotary tube is driven at 2 rpm.
- the average residence time of the coking pitch in the rotary kiln is about 1.5 hours.
- the oven shows no caking and the green coke is produced in pieces (74% by weight greater than 5 mm, 99% by weight greater than 1 mm).
- the coke has a high density and strength. It is fed into a calcining drum without cooling or intermediate storage and calcined there at 1300 ° C in the usual way.
- Example 1 is repeated with a throughput of 300 kg / h of pitch at a speed of 6 rpm.
- the dwell time of the coking pitch in the rotary kiln is reduced to about 0.5 h. 71% by weight of green coke with 3.5% by weight of volatile and a bulk density of 0.5 g / cm 3, 11% by weight of heavy oil, 14% by weight of light oil and 4% by weight of gas and losses are produced .
- the rotary kiln is flushed with 30 m 3 / h nitrogen in counterflow to the pitch. Gases and vapors leave the furnace on the pitch feed side and are condensed in two stages.
- the green coke is immediately transferred to a conventional calcining drum and calcined there at 1300 ° C. 89% by weight of calcined coke with a residual hydrogen content of 0.1% by weight and a true density of 2.028 g / cm 3 are obtained.
- the analyzes of the oils and the gas are contained in Tables I and II.
- Table 111 the calcined coke (1) obtained according to the invention is compared in its properties with normal petro-coke (2) and with pitch coke from the horizontal chamber furnace (3). As usual, the examinations were carried out on shaped bodies.
- the coke according to the invention is characterized by low CO 2 burnup and high electrical conductivity. Despite the higher conductivity compared to the usual pitch coke, its structure is finer and more uniformly mosaic-like, as the cross-sectional images show.
- the advantages of the coking process according to the invention lie in the short coking time of 1.5 to 0.5 hours, the low capital expenditure and the easy operation. It is also possible to return the fine portion of the coke and coke it together with the bad luck.
- the rods are graphitized at 2700 ° C and their physical properties compared to those of a reactor graphite made from Gilsonite coke:
- the coke according to the invention is outstandingly suitable for the production of reactor graphite. It has an exceptionally low expansion coefficient and a low anisotropy coefficient for pitch coke made from normal, uncleaned hard pitch. Another advantage is its small pore volume.
Abstract
Description
Die Erfindung betrifft ein Verfahren zum kontinuierlichen Verkoken von Pechen, insbesondere von Steinkohlenteerhartpechen, und die Verwendung des nach diesem Verfahren erhaltenen Kokses.The invention relates to a method for the continuous coking of pitches, in particular hard coal tar pitches, and the use of the coke obtained by this method.
Für die Verkokung hochsiedender steinkohlenteerstämmiger oder mineralölstämmiger Rückstände werden heute drei unterschiedliche Verkokungsverfahren angewandt:
- a) das Horizontalkammer-Verkokungsverfahren,
- b) das Delayed-Coking-Verfahren und
- c) das Fluid-Coking-Verfahren.
- a) the horizontal chamber coking process,
- (b) the delayed coking process; and
- c) the fluid coking process.
Das Verfahren nach a) ist eine Hochtemperaturverkokung und entspricht, von einigen Besonderheiten abgesehen, dem bekannten Kohleverkokungsverfahren. Als Einsatzprodukt wird ein Steinkohlenteerhartpech mit einem Verkokungsrückstand nach Brockmann-Muck von mehr als 50 % verwendet. Der erhaltene Koks ist sehr hart und braucht im allgemeinen wegen der hohen Verkokungstemperatur von mindestens 1000 °C nicht kalziniert zu werden. Das Verfahren ist sehr lohnintensiv. Die Anlagen, insbesondere die Ofenausmauerung, sind wegen der anderen physikalischen und chemischen Eigenschaften des Hartpechs gegenüber denen der Kohle wesentlich reparaturanfälliger als die der Kohleverkokung. Das Verfahren selbst ist diskontinuierlich, so daß eine Vielzahl von Kammern notwendig ist, um insgesamt.einen quasi-kontinuierlichen Betrieb zu ermöglichen.The process according to a) is high-temperature coking and, apart from a few special features, corresponds to the known coal coking process. A hard coal tar pitch with a coking residue according to Brockmann-Muck of more than 50% is used as the input product. The coke obtained is very hard and generally does not need to be calcined because of the high coking temperature of at least 1000 ° C. The process is very labor-intensive. Because of the different physical and chemical properties of the hard pitch, the plants, in particular the brick lining, are much more susceptible to repair than those of coal than those of coal coking. The process itself is discontinuous, so that a large number of chambers are necessary in order to enable quasi-continuous operation.
Das Verfahren nach b) ist ein Schwelverfahren bei etwa 500 °C. Als Einsatzprodukte kommen neben Rückständen der Mineralölindustrie auch Steinkohlenteerweichpeche zum Einsatz. Ursprünglich wurde der Delayed-Coker als thermischer Cracker betrieben. Es wurde jedoch bald erkannt, daß er eine ausgezeichnete Vorrichtung zur Herstellung hochanisotroper Spezialkokse ist. Der erhaltene Schwelkoks muß für die Weiterverwendung getrocknet und kalziniert werden. Die Anlagenkosten sind hoch, so daß eine Rentabilität nur bei der Erzeugung besonders hochwertiger Kokse oder wertvoller Öle gegeben ist. Dies ist bei unbehandelten Steinkohlenteerpechen normalerweise nicht der Fall. Das Verfahren selbst ist mit mindestens zwei Kokertrommeln quasi-kontinuierlich durchführbar.The process according to b) is a smoldering process at around 500 ° C. In addition to residues from the mineral oil industry, hard coal tar soft pitches are also used. The delayed coker was originally operated as a thermal cracker. However, it was soon recognized that it is an excellent device for producing highly anisotropic special cokes. The smoldering coke obtained must be dried and calcined for further use. The plant costs are high, so that profitability is only given in the production of particularly high-quality coke or valuable oils. This is usually not the case with untreated coal tar pitch. The method itself can be carried out quasi-continuously with at least two coker drums.
Das Verfahren nach c) ist ebenfalls ein Schwelverfahren, das jedoch kontinuierlich ausgeführt wird. Der Fluid-Coker ist ein thermischer Cracker für Mineralölrückstände. Der als Abfallprodukt entstehende Koks wird als Brennstoff verwendet. Für Steinkohlenteerpeche ist dieses Verfahren wegen der zu geringen ÖI- und Gasausbeute weniger geeignet.The process according to c) is also a smoldering process, but is carried out continuously. The fluid coker is a thermal cracker for mineral oil residues. The coke generated as a waste product is used as fuel. This process is less suitable for coal tar pitches because of the low oil and gas yield.
Aufgabe der Erfindung ist es daher, ein einfaches preiswertes Verfahren für die Verkokung von Steinkohlenteerhartpechen und vergleichbaren Produkten zu entwickeln und für den so erzeugten Koks geeignete Anwendungsgebiete zu finden. Die Aufgabe wird dadurch gelöst, daß das Hartpech in einem mit einem Räumwerkzeug versehenen, von außen beheizten Drehrohrofen bei Temperaturen der Innenwand zwischen 500 und 800 °C und einer Verweilzeit von 0,5 bis 1,5 h verkokt wird, wobei die entstehenden Gase und Dämpfe im Gegenstrom zum verkokenden Pech geführt werden, und der erhaltene Schwelkoks anschließend, vorzugsweise ohne vorherige Kühlung, in üblicher Weise kalziniert wird. Als Hartpech werden aromatische Rückstände mit einem Erweichungspunkt (EP) nach Kraemer-Sarnow (K.-S.) von mindestens 130 °C und einem Verkokungsrückstand nach Brockmann-Muck (B.-M.) von mindestens 45 Gew.-% bezeichnet. Sie können steinkohlenstämmig, wie z. B. Steinkohlenteerhartpech, oder auch mineralölstämmig sein, wie beispielsweise Petrohartpech aus der Benzinpyrolyse zur Herstellung von Olefinen. Der Drehrohrofen sollte zweckmäßigerweise in mehrere, unterschiedlich beheizbare Sektionen unterteilt sein. Durch eine äußere Beheizung werden die der Aufgabeseite zugewandten Segmente bis auf eine Außentemperatur von etwa 850 °C erhitzt. Die Außentemperatur der nachfolgenden Sektionen kann dann bis etwa 600 °C abfallen. Um eine Adsorption der Kondensate am Schwelkoks zu vermeiden, werden die Gase und Dämpfe im Gegenstrom zum verkokenden Pech geführt. Die Dämpfe werden nach dem Verlassen des Drehrohrofens kondensiert und können als Rußölkomponente verwendet oder der Hartpechherstellung zugeführt werden. Dabei hat sich die Einspeisung eines Inertgases an der Austragsseite des Drehrohrofens als hilfreich erwiesen. Die Verweilzeit der Dämpfe in der Verkokungszone wird dadurch verkürzt und die Rußbildung und Ablagerungen in den anschließenden Brüdenleitungen vermieden. Als Räumwerkzeug hat sich vor allem im vorderen Teil eine zur Aufgabeseite hin konische, mit körnigem Material beschwerte Schnecke bewährt, die mindestens etwa 1/3, vorzugsweise 1/2 mal so lang ist wie das Drehrohr und deren Neigung größer als die des Drehrohres ist. Daran kann sich eine Glattwalze anschließen. Das Räumwerkzeug ist vorzugsweise selbstzentrierend und wird kraftschlüssig von der Trommel bewegt. Das Pech kann stückig beispielsweise über eine Zellradschleuse oder flüssig in den Drehrohrofen eingebracht werden. Am Ende wird der Schwelkoks in stückiger Form über eine weitere Zellradschleuse ausgetragen und kann direkt der Kalziniereinrichtung zugeführt werden. Da das bei den Verkokungsverfahren a) und b) übliche Abkühlen des Kokses mit Wasser entfällt, ist wesentlich weniger Zeit und Energie für die Kalzinierung erforderlich.The object of the invention is therefore to develop a simple, inexpensive process for the coking of hard coal tar pitches and comparable products and to find suitable fields of application for the coke thus produced. The object is achieved in that the hard pitch is coked in a rotary tube furnace provided with a broaching tool and heated from the outside at temperatures of the inner wall between 500 and 800 ° C. and a residence time of 0.5 to 1.5 hours, the resulting gases and Vapors are passed in countercurrent to the coking pitch, and the smoldering coke obtained is then calcined in the usual manner, preferably without prior cooling. Aromatic residues with a softening point (EP) according to Kraemer-Sarnow (K.-S.) of at least 130 ° C and a coking residue according to Brockmann-Muck (B.-M.) of at least 45% by weight are referred to as hard pitch. You can come from coal, such as. B. hard coal tar pitch, or mineral oil origin, such as Petrohart pitch from gasoline pyrolysis for the production of olefins. The rotary kiln should advantageously be divided into several sections that can be heated differently. The segments facing the feed side are heated to an outside temperature of approximately 850 ° C. by external heating. The outside temperature of the following sections can then drop to around 600 ° C. In order to prevent the condensates from being adsorbed on the smoked coke, the gases and vapors are conducted in countercurrent to the coking pitch. The vapors are condensed after leaving the rotary kiln and can be used as a soot oil component or can be used for hard pitch production. The feeding of an inert gas on the discharge side of the rotary kiln has proven to be helpful. This shortens the dwell time of the vapors in the coking zone and prevents soot formation and deposits in the subsequent vapor lines. As a broaching tool, especially in the front part, a screw that is conical towards the feed side and weighted with granular material has proven itself, which is at least about 1/3, preferably 1/2 times as long as the rotary tube and its inclination is greater than that of the rotary tube. This can be followed by a smooth roller. The broaching tool is preferably self-centering and is moved non-positively by the drum. The pitch can be introduced in pieces, for example via a rotary valve, or in liquid form in the rotary kiln. At the end, the smoked coke is discharged in pieces via another rotary valve and can be fed directly to the calciner. Since there is no need to cool the coke with water in the coking processes a) and b), considerably less time and energy is required for the calcination.
Drehrohröfen werden zwar bekannterweise für die Verkokung bzw. Kalzinierung fester Brennstoffe wie Schwelkoks und Braunkohle oder zur Pyrolyse von überwiegend festen Abfällen verwendet, aber bei diesen bekannten Verfahren ist eine Verkokung der Einsatzprodukte an der heißen Wandung des Ofens nicht zu befürchten, oder sie tritt nur in vermindertem Umfang auf. Die Erfindung wird anhand der nachfolgenden Beispiele näher erläutert.Rotary kilns are known to be used for the coking or calcination of solid fuels such as smoked coke and lignite or for the pyrolysis of predominantly solid waste In these known processes, there is no fear of coking the feed products on the hot wall of the furnace, or it occurs only to a limited extent. The invention is illustrated by the following examples.
In einem Drehrohrofen mit einem inneren Durchmesser von 0,8 m und einer beheizten Länge von 7,2 m mit einer 4 m langen konischen Schnecke im vorderen Teil werden 75 kg/h eines Steinkohlenteerhartpechs mit einem EP (K.-S.) von 150 °C und einem Verkokungsrückstand (B.-M.) von 50 % eingespeist. Der Ofen ist in 6 Sektionen unterteilt, die indirekt mit Gas beheizt werden. Die Temperatur der Außenwand im Bereich des Eintrags beträgt 850 °C und fällt zum Austrag hin auf 700 °C. Im Mittel über die einzelnen Heizzonen liegt die Rohrwand-Außentemperatur etwa bei 800 °C. Das Drehrohr wird mit 2 Upm angetrieben. Die mittlere Verweilzeit des verkokenden Pechs im Drehrohrofen beträgt etwa 1,5 h. Der Ofen zeigt keinerlei Anbackungen, und der Grünkoks fällt in stückiger Form (74 Gew.-% größer 5 mm, 99 Gew.-% größer 1 mm) an. Der Koks hat eine hohe Dichte und Festigkeit. Er wird ohne Abkühlung oder Zwischenlagerung in eine Kalziniertrommel eingespeist und dort bei 1300 °C in üblicher Weise kalziniert.In a rotary kiln with an inner diameter of 0.8 m and a heated length of 7.2 m with a 4 m long conical screw in the front part, 75 kg / h of a hard coal tar pitch with an EP (K.-S.) of 150 ° C and a coking residue (B.-M.) of 50%. The oven is divided into 6 sections, which are heated indirectly with gas. The temperature of the outer wall in the area of the inlet is 850 ° C and drops to 700 ° C towards the outlet. The pipe wall outside temperature is approximately 800 ° C on average over the individual heating zones. The rotary tube is driven at 2 rpm. The average residence time of the coking pitch in the rotary kiln is about 1.5 hours. The oven shows no caking and the green coke is produced in pieces (74% by weight greater than 5 mm, 99% by weight greater than 1 mm). The coke has a high density and strength. It is fed into a calcining drum without cooling or intermediate storage and calcined there at 1300 ° C in the usual way.
Das Beispiel 1 wird mit einem Durchsatz von 300 kg/h Pech bei einer Drehzahl von 6 Upm wiederholt. Die Verweilzeit des verkokenden Pechs im Drehrohrofen vermindert sich dabei auf etwa 0,5 h. Es entstehen 71 Gew.-% Grünkoks mit 3,5 Gew.-% Flüchtigem und einer Schüttdichte von 0,5 g/cm3, 11 Gew.-% Schweröl, 14 Gew.-% Leichtöl und 4 Gew.-% Gas und Verluste. Während der Verkokung wird der Drehrohrofen im Gegenstrom zum Pech mit 30 m3/h Stickstoff gespült. Gase und Dämpfe verlassen den Ofen an der Pechaufgabeseite und werden in zwei Stufen kondensiert. Der Grünkoks wird sofort in eine übliche Kalziniertrommel überführt und dort bei 1300 °C kalziniert. Es werden 89 Gew.-% kalzinierter Koks mit einem Restwasserstoffgehalt von 0,1 Gew.-% und einer wahren Dichte von 2,028 g/cm3 erhalten. Die Analysen der Öle und des Gases sind in den Tabellen I und II enthalten. In Tabelle 111 wird der erfindungsgemäß gewonnene kalzinierte Koks (1) in seinen Eigenschaften mit normalem Petrokoks (2) und mit Pechkoks aus dem Horizontalkammerofen (3) verglichen. Die Untersuchungen sind wie üblich an Formkörpern durchgeführt.Example 1 is repeated with a throughput of 300 kg / h of pitch at a speed of 6 rpm. The dwell time of the coking pitch in the rotary kiln is reduced to about 0.5 h. 71% by weight of green coke with 3.5% by weight of volatile and a bulk density of 0.5 g / cm 3, 11% by weight of heavy oil, 14% by weight of light oil and 4% by weight of gas and losses are produced . During the coking, the rotary kiln is flushed with 30 m 3 / h nitrogen in counterflow to the pitch. Gases and vapors leave the furnace on the pitch feed side and are condensed in two stages. The green coke is immediately transferred to a conventional calcining drum and calcined there at 1300 ° C. 89% by weight of calcined coke with a residual hydrogen content of 0.1% by weight and a true density of 2.028 g / cm 3 are obtained. The analyzes of the oils and the gas are contained in Tables I and II. In Table 111 the calcined coke (1) obtained according to the invention is compared in its properties with normal petro-coke (2) and with pitch coke from the horizontal chamber furnace (3). As usual, the examinations were carried out on shaped bodies.
Der erfindungsgemäße Koks zeichnet sich durch geringen C02-Abbrand und hohe elektrische Leitfähigkeit aus. Seine Struktur ist trotz der höheren Leitfähigkeit gegenüber der des üblichen Pechkokses feiner und gleichmäßig mosaikartig, wie die Schliffbilder im Vergleich zeigen. Die Vorteile des erfindungsgemäßen Verkokungsverfahrens liegen in der kurzen Verkokungszeit von 1,5 bis 0,5 h, dem geringen Kapitalaufwand und der leichten Bedienung. Außerdem ist es möglich, den Feinanteil des Kokses zurückzuführen und mit dem Pech gemeinsam zu verkoken.The coke according to the invention is characterized by low CO 2 burnup and high electrical conductivity. Despite the higher conductivity compared to the usual pitch coke, its structure is finer and more uniformly mosaic-like, as the cross-sectional images show. The advantages of the coking process according to the invention lie in the short coking time of 1.5 to 0.5 hours, the low capital expenditure and the easy operation. It is also possible to return the fine portion of the coke and coke it together with the bad luck.
Pechkoks aus dem Horizontalkammerofen
Pechkoks nach dem erfindungsgemäßen Verfahren
Wegen der gleichmäßig mosaikartigen Struktur scheint der erfindungsgemäß hergestellte Koks für die Herstellung von Reaktorgraphit geeignet zu sein. Es ist bekannt, daß sich hierfür insbesondere Kokse mit niedrigem Anisotropiekoeffizient eignen. 100 Gew.-Teile des erfindungsgemäß hergestellten Kokses werden daher bis auf eine Korngröße von maximal 0,5 mm gemahlen und mit 27,5 Gew.-Teilen eines Standard-Elektrodenpechs gemischt. Diese Masse wird zu Testelektroden verpreßt und bei 900 °C gebrannt. Aus den Testelektroden werden Stäbchen geschnitten, die bei 1300 °C kalziniert werden. Sie haben eine wahre Dichte von 2,12 g/cm3 und einen thermischen Ausdehnungskoeffizienten (a) in Längs-und Querrichtung im Bereich von 20 bis 200 °C von
- 1/pG(lvon 1,11.
- 1 / pG (l of 1.11.
Die Stäbchen werden bei 2700 °C graphitiert und ihre physikalischen Eigenschaften mit denen eines Reaktorgraphits aus Gilsonite-Koks verglichen:
Wie die Analysendaten zeigen ist der erfindungsgemäße Koks hervorragend für die Herstellung von Reaktorgraphit geeignet. Er hat einen für Pechkoks aus normalem, nicht gereinigtem Hartpech außergewöhnlich niedrigen Ausdehnungskoeffizienten und einen geringen Anisotropiekoeffizienten. Ein weiterer Vorteil ist sein geringes Porenvolumen.As the analysis data show, the coke according to the invention is outstandingly suitable for the production of reactor graphite. It has an exceptionally low expansion coefficient and a low anisotropy coefficient for pitch coke made from normal, uncleaned hard pitch. Another advantage is its small pore volume.
Claims (3)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AT87100270T ATE45587T1 (en) | 1986-03-20 | 1987-01-12 | PROCESS FOR CONTINUOUS COKING OF PITCH AND USE OF THE OBTAINED COKE. |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE3609348 | 1986-03-20 | ||
| DE19863609348 DE3609348A1 (en) | 1986-03-20 | 1986-03-20 | METHOD FOR CONTINUOUS COOKING OF PECHES AND USE OF THE COOK RECOVED |
Publications (3)
| Publication Number | Publication Date |
|---|---|
| EP0237702A2 EP0237702A2 (en) | 1987-09-23 |
| EP0237702A3 EP0237702A3 (en) | 1988-02-10 |
| EP0237702B1 true EP0237702B1 (en) | 1989-08-16 |
Family
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| EP87100270A Expired EP0237702B1 (en) | 1986-03-20 | 1987-01-12 | Process for the continuous coking of pitches, and use of the coke obtained |
Country Status (11)
| Country | Link |
|---|---|
| US (1) | US4764318A (en) |
| EP (1) | EP0237702B1 (en) |
| JP (1) | JPS62227991A (en) |
| AT (1) | ATE45587T1 (en) |
| AU (1) | AU585436B2 (en) |
| CA (1) | CA1268438A (en) |
| CS (1) | CS274289B2 (en) |
| DE (2) | DE3609348A1 (en) |
| ES (1) | ES2000091B3 (en) |
| PL (1) | PL151853B1 (en) |
| ZA (1) | ZA87673B (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH07118066A (en) * | 1993-10-22 | 1995-05-09 | Tokai Carbon Co Ltd | Production of high strength isotropic graphite material |
| US20060074598A1 (en) * | 2004-09-10 | 2006-04-06 | Emigholz Kenneth F | Application of abnormal event detection technology to hydrocracking units |
| US7720641B2 (en) * | 2006-04-21 | 2010-05-18 | Exxonmobil Research And Engineering Company | Application of abnormal event detection technology to delayed coking unit |
| US8862250B2 (en) | 2010-05-07 | 2014-10-14 | Exxonmobil Research And Engineering Company | Integrated expert system for identifying abnormal events in an industrial plant |
| US10836969B2 (en) * | 2016-09-27 | 2020-11-17 | Cleancarbonconversion Patents Ag | Process reacting organic materials to give hydrogen gas |
Family Cites Families (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2357621A (en) * | 1941-07-30 | 1944-09-05 | Max B Miller & Co Inc | Apparatus for coking petroleum residues |
| US3316183A (en) * | 1963-12-12 | 1967-04-25 | Exxon Research Engineering Co | Shaped carbon articles and method of making |
| DE1796129A1 (en) * | 1968-09-05 | 1972-03-02 | Metallgesellschaft Ag | Process for the continuous production of metallurgical shaped coke |
| US3756791A (en) * | 1971-06-09 | 1973-09-04 | Bethlehem Steel Corp | Al and or coal derivatives method for simultaneously calcining and desulfurizing agglomerates co |
| US4053365A (en) * | 1975-12-02 | 1977-10-11 | Great Lakes Carbon Corporation | Rotary calciner |
| DE2627479C2 (en) * | 1976-06-18 | 1983-09-22 | Bergwerksverband Gmbh, 4300 Essen | Use of a molded coke as an adsorbent for sulfur oxides from exhaust gases |
| FR2385786A1 (en) * | 1977-03-28 | 1978-10-27 | Nord Pas Calais Houilleres | PROCESS FOR OBTAINING MOLD COKE FROM NON-COKEFIABLE COALS |
| US4218288A (en) * | 1979-02-12 | 1980-08-19 | Continental Oil Company | Apparatus and method for compacting, degassing and carbonizing carbonaceous agglomerates |
| DE2925202A1 (en) * | 1979-06-22 | 1981-01-15 | Rupert Hoell | Plastic waste pyrolysis - by counterflow in inclined cylinder externally heated to high discharge temp. |
| US4303477A (en) * | 1979-06-25 | 1981-12-01 | Babcock Krauss-Maffei Industrieanlagen Gmbh | Process for the pyrolysis of waste materials |
| CH645401A5 (en) * | 1980-08-21 | 1984-09-28 | Alusuisse | METHOD FOR PRODUCING DESULFURED COOKED FOR ANODES USED IN ALUMINUM ELECTROLYSIS. |
| US4369171A (en) * | 1981-03-06 | 1983-01-18 | Great Lakes Carbon Corporation | Production of pitch and coke from raw petroleum coke |
| DE3125609A1 (en) * | 1981-06-30 | 1983-01-13 | Rütgerswerke AG, 6000 Frankfurt | METHOD FOR PRODUCING CARBON MOLDED BODIES |
| CA1260868A (en) * | 1984-04-11 | 1989-09-26 | Izaak Lindhout | Process for calcining green coke |
-
1986
- 1986-03-20 DE DE19863609348 patent/DE3609348A1/en not_active Withdrawn
-
1987
- 1987-01-12 EP EP87100270A patent/EP0237702B1/en not_active Expired
- 1987-01-12 DE DE8787100270T patent/DE3760453D1/en not_active Expired
- 1987-01-12 ES ES87100270T patent/ES2000091B3/en not_active Expired
- 1987-01-12 AT AT87100270T patent/ATE45587T1/en active
- 1987-01-29 ZA ZA870673A patent/ZA87673B/en unknown
- 1987-02-02 CA CA000528742A patent/CA1268438A/en not_active Expired - Fee Related
- 1987-03-06 US US07/023,052 patent/US4764318A/en not_active Expired - Fee Related
- 1987-03-17 JP JP62060246A patent/JPS62227991A/en active Pending
- 1987-03-19 CS CS186187A patent/CS274289B2/en unknown
- 1987-03-19 PL PL1987264723A patent/PL151853B1/en unknown
- 1987-03-20 AU AU70434/87A patent/AU585436B2/en not_active Ceased
Also Published As
| Publication number | Publication date |
|---|---|
| JPS62227991A (en) | 1987-10-06 |
| ES2000091B3 (en) | 1989-10-16 |
| DE3760453D1 (en) | 1989-09-21 |
| CS186187A2 (en) | 1990-09-12 |
| AU7043487A (en) | 1987-09-24 |
| PL264723A1 (en) | 1988-05-12 |
| CA1268438A (en) | 1990-05-01 |
| US4764318A (en) | 1988-08-16 |
| ATE45587T1 (en) | 1989-09-15 |
| AU585436B2 (en) | 1989-06-15 |
| EP0237702A2 (en) | 1987-09-23 |
| EP0237702A3 (en) | 1988-02-10 |
| ES2000091A4 (en) | 1987-12-01 |
| PL151853B1 (en) | 1990-10-31 |
| DE3609348A1 (en) | 1987-09-24 |
| ZA87673B (en) | 1987-09-16 |
| CS274289B2 (en) | 1991-04-11 |
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