DE19718871A1 - Process for oxychlorination of ethylene in a fluidized bed catalyst bed - Google Patents
Process for oxychlorination of ethylene in a fluidized bed catalyst bedInfo
- Publication number
- DE19718871A1 DE19718871A1 DE1997118871 DE19718871A DE19718871A1 DE 19718871 A1 DE19718871 A1 DE 19718871A1 DE 1997118871 DE1997118871 DE 1997118871 DE 19718871 A DE19718871 A DE 19718871A DE 19718871 A1 DE19718871 A1 DE 19718871A1
- Authority
- DE
- Germany
- Prior art keywords
- catalyst
- fluidized bed
- ethylene
- oxychlorination
- bed
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Ceased
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/093—Preparation of halogenated hydrocarbons by replacement by halogens
- C07C17/15—Preparation of halogenated hydrocarbons by replacement by halogens with oxygen as auxiliary reagent, e.g. oxychlorination
- C07C17/152—Preparation of halogenated hydrocarbons by replacement by halogens with oxygen as auxiliary reagent, e.g. oxychlorination of hydrocarbons
- C07C17/156—Preparation of halogenated hydrocarbons by replacement by halogens with oxygen as auxiliary reagent, e.g. oxychlorination of hydrocarbons of unsaturated hydrocarbons
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
Description
Die Erfindung richtet sich auf ein Verfahren zur Oxichlorie rung von Ethylen in einem wirbelschichtmäßig ausgebildeten Katalysatorbett.The invention is directed to a process for oxychlorine tion of ethylene in a fluidized bed Catalyst bed.
Ein Problem bei exothermen, aber auch endothermen katalyti schen Vorgängen besteht darin, daß zu Beginn des Katalysator bettes der Hauptteil der Reaktion und (beispielsweise bei exo thermen Vorgängen) der Hauptanfall der Wärme stattfindet, die dann nach außen abgeführt werden muß, während über den Rest der Betthöhe die Restumsetzung erfolgt mit deutlich geringerem Wärmeanfall. Danach müssen die Wärmetauscherrohre, aber auch die Höhe der Katalysatorschicht entsprechend ausgelegt werden. Da die Länge der Verdampferrohre von der gesamten Wirbel schicht umspült werden muß, um eine genügende Wärmeabfuhr zu ermöglichen, wird eine große Menge an Katalysator benötigt, was mit entsprechend hohen Kosten verbunden ist.A problem with exothermic, but also endothermic catalyti processes is that at the beginning of the catalyst the main part of the reaction and (for example in exo thermal processes) the main amount of heat that takes place then must be discharged to the outside while over the rest the bed height the remaining conversion takes place with significantly less Heat accumulation. After that, the heat exchanger tubes, too the height of the catalyst layer can be designed accordingly. Because the length of the evaporator tubes from the entire vortex layer must be washed to ensure sufficient heat dissipation a large amount of catalyst is required which is associated with correspondingly high costs.
Um eine Vergleichmäßigung der Temperatur zwischen Fuß und Kopf der Wirbelschicht zu erreichen, ist schon vorgeschlagen wor den, Glas, Tonerde oder Kieselsäure bzw. Quarz zur Stabilisie rung der Korngrößenverteilung des Katalysators einzusetzen (DE-24 42 182-C3).To even out the temperature between the foot and head Reaching the fluidized bed has already been suggested glass, alumina or silica or quartz for stabilization tion of the particle size distribution of the catalyst (DE-24 42 182-C3).
Hier setzt die Erfindung an, die sich zur Aufgabe gestellt hat, insbesondere den Aufwand und die Kosten bei heterogenen, katalytischen Gasphasenreaktionen im Wirbelschichtreaktor, nämlich bei der Oxichlorierung von Ethylen, zu verringern. Dieses Ziel wird durch die Maßnahme des Anspruches 1 gelöst.This is where the invention comes in, which set itself the task has, in particular the effort and costs for heterogeneous, catalytic gas phase reactions in a fluidized bed reactor, namely in the oxychlorination of ethylene. This goal is solved by the measure of claim 1.
Das hier eingesetzte, daß den Katalysatorträger bildende Mate rial hat besondere Vorteile, da es von den physikalischen Pa rametern dem Katalysator sehr ähnlich ist. Damit lassen sich die Parameter, wie Korngröße, Abriebfestigkeit u. dgl., in einfacher Weise so anpassen, daß sich z. B. die Abriebverluste minimieren lassen.The mate used here that forms the catalyst support rial has special advantages because it depends on the physical Pa rametern is very similar to the catalyst. With that you can the parameters such as grain size, abrasion resistance and. Like., in adjust easily so that z. B. the abrasion losses minimize.
Allgemein ist zu sagen, daß die Erzeugung von 1,2 Dichlorethan
(1,2-EDC) durch Oxichlorierung von Ethylen verläuft an einem
kupferhaltigen Katalysator (Träger: Aluminiumoxid) nach der
Bruttogleichung:
In general, it can be said that the production of 1,2 dichloroethane (1,2-EDC) by oxychlorination of ethylene takes place on a copper-containing catalyst (carrier: aluminum oxide) according to the gross equation:
C2H4 + 2 HCl + 1/2 O2 → C2H4Cl2 + H2O + Δ H
C 2 H 4 + 2 HCl + 1/2 O 2 → C 2 H 4 Cl 2 + H 2 O + Δ H
wobei hier die Reaktion in einem Wirbelschichtreaktor mit Wär
meabfuhr durch ein vertikales Verdampferrohrbündel durchge
führt wird. Als Beispiel seien einige Daten genannt:
Betthöhe: ca. 14 m
Mittlerer Katalysatorkorndurchmesser: ca. 51 µm
Kupfergehalt des Katalysators: ca. 4%
Reaktionstemperatur: 220°C
Reaktionsdruck: 4,55 bar
Gasgeschwindigkeit bei Minimalfluidierung: ca. 0,002 m/s
Leerrohrgasgeschwindigkeit im Reaktor: 0,21-0,42 m/s
Weitere Ausgestaltungen ergeben sich aus den Unteransprüchen.where the reaction is carried out in a fluidized bed reactor with heat dissipation through a vertical evaporator tube bundle. Some data may be mentioned as an example:
Bed height: approx. 14 m
Average catalyst grain diameter: approx. 51 µm
Copper content of the catalyst: approx. 4%
Reaction temperature: 220 ° C
Reaction pressure: 4.55 bar
Gas velocity with minimal fluidization: approx. 0.002 m / s
Empty tube gas velocity in the reactor: 0.21-0.42 m / s
Further refinements result from the subclaims.
Besonders vorteilhaft ist, wie oben schon ausgeführt, wenn als Verdünnungsmaterial der inerte Katalysator, nämlich γ-Alumini umoxid, eingesetzt wird.As already stated above, it is particularly advantageous if as Dilution material of the inert catalyst, namely γ-aluminum umoxid, is used.
Auch ist es zweckmäßig, die Form der Teilchen, z. B. die Sphä rizität (Abweichung der Katalysator-Teilchen von einer idealen Kugelform) so zu wählen, wie dies bei den Katalysator-Teilchen selbst der Fall ist, wobei hier zweckmäßig ein Katalysator und ein entsprechendes Verdünnungsmaterial mit einer Sphärizität von 0,99 eingesetzt wird (fast ideale Kugelform). Derartig runde Teilchen vermindern idealerweise unerwünschten Abrieb.It is also appropriate to change the shape of the particles, e.g. B. the sphere Ricity (deviation of the catalyst particles from an ideal Spherical shape) to be chosen, as is the case with the catalyst particles itself is the case, in which case a catalyst and an appropriate diluent with a sphericity of 0.99 is used (almost ideal spherical shape). Such round particles ideally reduce unwanted abrasion.
Auch wird erfindungsgemäß beim Verdünnungsmaterial eine Korn größenverteilung gewählt, die derjenigen des Katalysatormate riales selbst entspricht, auch dies fördert die Verringerung des Abriebverhaltens, so daß die ausgetragene Feinstaubmenge gegenüber herkömmlich betriebenen Systemen nicht geändert wird.According to the invention, a grain is also used in the dilution material size distribution chosen that of the catalyst mate riales itself, this also promotes reduction the abrasion behavior, so that the amount of fine dust discharged not changed compared to conventionally operated systems becomes.
Eine zweckmäßige Variante der Erfindung besteht darin, daß Verdünnungsmaterial aus Keramik hoher Wärmeleitfähigkeit ein gesetzt wird. Hierbei kann es sich beispielsweise um Silicium carbit handeln.An expedient variant of the invention is that Thinner material made of ceramic with high thermal conductivity is set. This can be silicon, for example trade carbit.
Allgemein sei angemerkt, daß das Verfahren auch bei anderen Wirbelschichtprozessen anwendbar ist, es muß nicht zwingend zur Oxichlorierung von Ethylen eingesetzt werden, obgleich es hier von besonderem Wert ist. Die Wärmeleitfähigkeit des ein gesetzten Inertmateriales hat wesentlichen Einfluß auf die mantelseitigen Wärmeübergangszahlen. Hier können in besonderer Weise keramische Werkstoffe eingesetzt werden, wodurch sich die Effizienz des Katalysator-Verdünnungsverfahrens nochmals steigern läßt.In general, it should be noted that the method also applies to others Fluid bed processes is applicable, it doesn't have to be mandatory be used for the oxychlorination of ethylene, although it is of particular value here. The thermal conductivity of the one set inert material has a significant influence on the jacket-side heat transfer coefficients. Here in particular Way ceramic materials are used, which makes the efficiency of the catalyst dilution process again can increase.
Neben der besonders vorteilhaften Mengenangabe von bis zu 50% γ-Aluminiumoxid als Verdünnungsmaterial sei angemerkt, daß hier auch andere Mischungsverhältnisse in Betracht kommen. Je nach Einsatzgebiet kann auch ein höherer Anteil des Verdün nungsmateriales vorgesehen sein.In addition to the particularly advantageous quantity of up to 50% γ-alumina as a dilution material should be noted that other mixing ratios can also be considered here. Each depending on the application, a higher proportion of the dilution be provided.
Claims (5)
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE1997118871 DE19718871A1 (en) | 1997-05-03 | 1997-05-03 | Process for oxychlorination of ethylene in a fluidized bed catalyst bed |
PCT/EP1998/002087 WO1998050328A1 (en) | 1997-05-03 | 1998-04-09 | Method for oxichlorination of ethylene in a fluidized bed-catalyst bed |
AU76424/98A AU7642498A (en) | 1997-05-03 | 1998-04-09 | Method for oxichlorination of ethylene in a fluidized bed-catalyst bed |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE1997118871 DE19718871A1 (en) | 1997-05-03 | 1997-05-03 | Process for oxychlorination of ethylene in a fluidized bed catalyst bed |
Publications (1)
Publication Number | Publication Date |
---|---|
DE19718871A1 true DE19718871A1 (en) | 1998-11-12 |
Family
ID=7828625
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
DE1997118871 Ceased DE19718871A1 (en) | 1997-05-03 | 1997-05-03 | Process for oxychlorination of ethylene in a fluidized bed catalyst bed |
Country Status (3)
Country | Link |
---|---|
AU (1) | AU7642498A (en) |
DE (1) | DE19718871A1 (en) |
WO (1) | WO1998050328A1 (en) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP1020222A2 (en) * | 1999-01-08 | 2000-07-19 | Süd Chemie Mt S.R.L. | Catalytic composition for controlling exothermic reactions on a fixed bed |
DE102008048526A1 (en) | 2008-09-23 | 2010-04-01 | Uhde Gmbh | Process for the use of the heat of reaction in the production process of 1,2-dichloroethane from ethylene in a fluidized bed reactor |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
TWI341218B (en) | 2005-11-14 | 2011-05-01 | Oxy Vinyls Lp | Catalyst compositions and process for oxychlorination |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DD86387A (en) * | ||||
US4446249A (en) * | 1979-11-05 | 1984-05-01 | The B. F. Goodrich Company | Copper catalyst compositions for fluid-bed oxyhydrochlorination of ethylene |
US5202511A (en) * | 1989-08-16 | 1993-04-13 | The Dow Chemical Company | Catalyst diluent for oxychlorination process |
DE4131446A1 (en) * | 1991-09-21 | 1993-06-09 | Basf Ag, 6700 Ludwigshafen, De | REACTOR AND METHOD FOR CARRYING OUT HETEROGENIC CATALYTIC GAS PHASE REACTIONS |
DE4305001A1 (en) * | 1993-02-18 | 1994-08-25 | Hoechst Ag | Oxychlorination device |
Family Cites Families (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4339620A (en) * | 1979-11-05 | 1982-07-13 | The B. F. Goodrich Company | Copper-catalyzed fluid-bed ethylene oxhydrochlorination process |
-
1997
- 1997-05-03 DE DE1997118871 patent/DE19718871A1/en not_active Ceased
-
1998
- 1998-04-09 WO PCT/EP1998/002087 patent/WO1998050328A1/en active Application Filing
- 1998-04-09 AU AU76424/98A patent/AU7642498A/en not_active Abandoned
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DD86387A (en) * | ||||
US4446249A (en) * | 1979-11-05 | 1984-05-01 | The B. F. Goodrich Company | Copper catalyst compositions for fluid-bed oxyhydrochlorination of ethylene |
US5202511A (en) * | 1989-08-16 | 1993-04-13 | The Dow Chemical Company | Catalyst diluent for oxychlorination process |
DE4131446A1 (en) * | 1991-09-21 | 1993-06-09 | Basf Ag, 6700 Ludwigshafen, De | REACTOR AND METHOD FOR CARRYING OUT HETEROGENIC CATALYTIC GAS PHASE REACTIONS |
DE4305001A1 (en) * | 1993-02-18 | 1994-08-25 | Hoechst Ag | Oxychlorination device |
Cited By (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP1020222A2 (en) * | 1999-01-08 | 2000-07-19 | Süd Chemie Mt S.R.L. | Catalytic composition for controlling exothermic reactions on a fixed bed |
EP1020222A3 (en) * | 1999-01-08 | 2001-11-21 | Süd Chemie Mt S.R.L. | Catalytic composition for controlling exothermic reactions on a fixed bed |
US6593269B1 (en) | 1999-01-08 | 2003-07-15 | Sud Chemie Mt S.R.L. | Catalysts for exothermic reactions on a fixed bed |
DE102008048526A1 (en) | 2008-09-23 | 2010-04-01 | Uhde Gmbh | Process for the use of the heat of reaction in the production process of 1,2-dichloroethane from ethylene in a fluidized bed reactor |
WO2010034392A1 (en) * | 2008-09-23 | 2010-04-01 | Uhde Gmbh | Method for using the reaction heat developing during the production process of 1,2-dichloroethane from ethylene in a fluidized bed reactor |
RU2481320C2 (en) * | 2008-09-23 | 2013-05-10 | Тиссенкрупп Уде Гмбх | Method of using reaction heat obtained during production of 1,2-dichloroethane from ethylene in fluidised bed reactor |
US8552229B2 (en) | 2008-09-23 | 2013-10-08 | Thyssenkrupp Uhde Gmbh | Method for utilization of the reaction heat that occurs in the production process of 1,2-dichloroethane from ethylene in a fluidized bed reactor |
Also Published As
Publication number | Publication date |
---|---|
AU7642498A (en) | 1998-11-27 |
WO1998050328A1 (en) | 1998-11-12 |
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Legal Events
Date | Code | Title | Description |
---|---|---|---|
OP8 | Request for examination as to paragraph 44 patent law | ||
8131 | Rejection |