DE19844901C1 - Method for metering liquid polynitro-aromatic compounds into hydrogenation reactors - Google Patents

Method for metering liquid polynitro-aromatic compounds into hydrogenation reactors

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Publication number
DE19844901C1
DE19844901C1 DE1998144901 DE19844901A DE19844901C1 DE 19844901 C1 DE19844901 C1 DE 19844901C1 DE 1998144901 DE1998144901 DE 1998144901 DE 19844901 A DE19844901 A DE 19844901A DE 19844901 C1 DE19844901 C1 DE 19844901C1
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Prior art keywords
reactor
polynitro
hydrogenation
metering liquid
lines
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DE1998144901
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German (de)
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Reinhard Langer
Gerd Fengler
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Bayer AG
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Bayer AG
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C209/00—Preparation of compounds containing amino groups bound to a carbon skeleton
    • C07C209/30—Preparation of compounds containing amino groups bound to a carbon skeleton by reduction of nitrogen-to-oxygen or nitrogen-to-nitrogen bonds
    • C07C209/32—Preparation of compounds containing amino groups bound to a carbon skeleton by reduction of nitrogen-to-oxygen or nitrogen-to-nitrogen bonds by reduction of nitro groups
    • C07C209/36—Preparation of compounds containing amino groups bound to a carbon skeleton by reduction of nitrogen-to-oxygen or nitrogen-to-nitrogen bonds by reduction of nitro groups by reduction of nitro groups bound to carbon atoms of six-membered aromatic rings in presence of hydrogen-containing gases and a catalyst
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1836—Heating and cooling the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
    • B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
    • B01J8/222—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid in the presence of a rotating device only
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
    • B01J2208/00141—Coils

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

A method for metering liquid polynitro-aromatics into hydrogenation reactors comprises pumping the nitroaromatic round one or more pipelines in the form of closed loops passing entirely or partly through the reactor and provided with outlets inside the reactor.

Description

Die vorliegende Erfindung betrifft ein Verfahren zur sicheren und schonenden Dosierung von flüssigen Nitroaromaten mit mehr als einer Nitrogruppe, speziell von Dinitrotoluolen in Reaktoren zur Hydrierung, speziell zur Sumpfphasen-Hydrierung.The present invention relates to a method for safe and gentle Dosing of liquid nitro aromatics with more than one nitro group, especially from Dinitrotoluenes in reactors for hydrogenation, especially for the bottom phase hydrogenation.

Nitroaromaten mit mehr als einer Nitrogruppe können in der flüssigen Phase an grobteiligen festen Katalysatorschüttungen, wie z. B. in WO 97/2080 beschrieben, oder mittels aufgeschlämmten feinteiligen Katalysatoren in der sogenannten Sumpf­ phase, wie in WO 96/11052 beschrieben, hydriert werden. Dabei dient das Reak­ tionsgemisch selber, gegebenenfalls unter Zusatz eines weiteren Lösungsmittels als Reaktionsmedium. Als Katalysatoren kommen im wesentlichen Edelmetall-Träger- Katalysatoren oder Raney-Nickel zum Einsatz.Nitro aromatics with more than one nitro group can be in the liquid phase coarse-particle solid catalyst beds, such as. B. described in WO 97/2080, or by means of slurried fine-particle catalysts in the so-called sump phase, as described in WO 96/11052, are hydrogenated. The reak is used here tion mixture itself, optionally with the addition of another solvent as Reaction medium. The catalysts used are essentially noble metal supports Catalysts or Raney nickel are used.

Stand der Technik ist die Dosierung von Nitroaromaten in einen Katalysatorslurry über ein Einleitungsrohr an einer Stelle mit guter Durchmischung, wie es z. B. in WO 96/11052 beschrieben ist.State of the art is the metering of nitro aromatics into a catalyst slurry via an inlet pipe at a point with good mixing, as z. B. in WO 96/11052.

Die Aufgabe der vorliegenden Erfindung besteht darin, ein sicheres Dosierverfahren zur Verfügung zu stellen, welches zudem Katalysatordesaktivierung und Neben­ produktbildung vermeidet.The object of the present invention is a safe dosing method to provide, which also catalyst deactivation and side avoids product formation.

Gegenstand der vorliegenden Erfindung ist ein Verfahren zur Dosierung von flüssigen Nitroaromaten mit mehr als einer Nitrogruppe in Reaktoren zur Hydrie­ rung, bevorzugt zur Sumpfphasen-Hydrierung, dadurch gekennzeichnet, daß a) der zu dosierende Nitroaromat in einer oder mehreren Ringleitungen im Kreis gepumpt wird, b) diese Ringleitungen ganz oder teilweise im Hydrierreaktor verlaufen, c) die Ringleitungen im Reaktorinneren mit Austrittsöffnungen zum Reaktorinneren ver­ sehen sind. The present invention relates to a method for metering liquid nitro aromatics with more than one nitro group in reactors for hydration tion, preferably for the bottom phase hydrogenation, characterized in that a) the Nitroaromat to be dosed pumped in one or more ring lines in a circle is b) all or part of these ring lines run in the hydrogenation reactor, c) the Ver ring lines in the interior of the reactor with outlet openings to the interior of the reactor are seen.  

Das Verfahren besteht im wesentlichen darin, daß man den zu dosierenden Nitro­ aromaten in einer oder mehreren Leitungen im Kreis pumpt, diese Leitungen ganz oder teilweise im Hydrierreaktor verlaufen und im Reaktorinneren mit Austritts­ öffnungen zum Reaktorinneren versehen sind und der zu dosierende Nitroaromat ge­ gebenenfalls zusammen mit Verdünnungsmittel in diese Kreisstromleitung dosiert wird. Die dadurch entstehende Druckdifferenz zwischen Reaktorinneren und Kreis­ stromleitung bewirkt, daß der zu dosierende Nitroaromat durch die Austritts­ öffnungen in das Reaktorinnere gedrückt wird. Der zu dosierende Nitroaromat wird bevorzugt über eine Dosierpumpe in die Ringleitung dosiert.The process consists essentially in that the nitro to be dosed aromatics pumps in one or more lines in a circle, these lines completely or partially run in the hydrogenation reactor and inside the reactor with outlet openings to the inside of the reactor are provided and the nitroaromatic to be metered if necessary, metered together with diluent into this circular flow line becomes. The resulting pressure difference between the inside of the reactor and the circuit power line causes the nitroaromatic to be dosed through the outlet openings are pressed into the interior of the reactor. The nitroaromatic to be dosed will preferably metered into the ring line via a metering pump.

Als geeignete Nitroaromaten für das erfindungsgemäße Verfahren sind z. B. zu nennen, Dinitrobenzol, Trinitrobenzol, Tetranitrobenzol, die isomeren Dinitrotoluole, wie 2,4-, 2,6-, 3,4-, 2,3- und 2,5-Dinitrotoluol und deren Gemische, bevorzugt Gemische mit 2,4- und 2,6-Dinitrotoluol als Hauptkomponenten (z. B. 70 bis 85 Gew.-% 2,4-Dinitrotoluol und 10 bis 25 Gew.-% 2,6-Dinitrotoluol und 3,4-, 2,3- und 2,5-Dinitrotoluol jeweils < 4 Gew.-%), die isomeren Trinitrotoluole, die isomeren Dinitrochlorbenzole, die isomeren Trinitrochlorbenzole, die isomeren Dinitrodichlor­ benzole, die isomeren Dinitronaphthaline, die Isomeren Trinitronaphthaline und die Isomeren Di- und Trinitroanthracene und -phenanthrene, bevorzugt werden die isomeren Dinitrotoluole einzeln oder als Mischung eingesetzt.Suitable nitroaromatics for the process according to the invention are, for. B. too name dinitrobenzene, trinitrobenzene, tetranitrobenzene, the isomeric dinitrotoluenes, such as 2,4-, 2,6-, 3,4-, 2,3- and 2,5-dinitrotoluene and mixtures thereof Mixtures with 2,4- and 2,6-dinitrotoluene as main components (e.g. 70 to 85 % By weight 2,4-dinitrotoluene and 10 to 25% by weight 2,6-dinitrotoluene and 3,4-, 2,3- and 2,5-dinitrotoluene each <4 wt .-%), the isomeric trinitrotoluenes, the isomeric Dinitrochlorobenzenes, the isomeric trinitrochlorobenzenes, the isomeric dinitrodichlor benzenes, the isomeric dinitronaphthalenes, the isomers trinitronaphthalenes and the Isomers di- and trinitroanthracenes and -phenanthrenes, the preferred isomeric dinitrotoluenes used individually or as a mixture.

Geeignete Verdünnungsmittel sind z. B. das bei der Hydrierung entstehende Amin- Wassergemisch, kurzkettige aliphatische Alkohole wie Isopropanol und aromatische Kohlenwasserstoffe wie Benzol und Toluol, bevorzugt werden kurzkettige aliphatische Alkohole gegebenenfalls zusammen mit Teilen des entstehenden Amin- Wassergemisches, besonders bevorzugt wird ausschließlich das Amin-Wasser­ gemisch verwendet. Dieses wird bevorzugt aus dem Hydrierreaktor ausgeschleust und dann mit dem zu dosierenden Nitroaromaten vermischt. Suitable diluents are e.g. B. the amine formed during the hydrogenation Water mixture, short-chain aliphatic alcohols such as isopropanol and aromatic Hydrocarbons such as benzene and toluene, short-chain are preferred aliphatic alcohols optionally together with parts of the amine Water mixture, particularly preferred is the amine water mix used. This is preferably discharged from the hydrogenation reactor and then mixed with the nitroaromatic to be dosed.  

Geeignete Reaktoren für das erfindungsgemäße Verfahren sind diskontinuierlich oder kontinuierlich betriebene Rührkessel-Reaktoren, wie sie z. B. in WO 96/11052 und EP 263 935 beschrieben sind, ebenso geeignet sind Kreisstrom- bzw. Loop-Reak­ toren die Stand der Technik sind, auch Blasensäulen können mit dem erfindungs­ gemäßen Verfahren betrieben werden. Bevorzugt werden für das erfindungsgemäße Verfahren Rührkessel-Reaktoren, wie sie z. B. in WO 96/11052 beschrieben sind.Suitable reactors for the process according to the invention are batchwise or continuously operated stirred tank reactors, such as those used for. B. in WO 96/11052 and EP 263 935 are described, circular current or loop reac are also suitable gates that are state of the art, also bubble columns can with the invention operated in accordance with the procedure. Are preferred for the invention Process stirred tank reactors, such as those used for. B. are described in WO 96/11052.

Das in dem erfindungsgemäßen Verfahren verwendete Dosiersystem besteht minde­ stens aus einer und höchstens aus 100, bevorzugt aus einer und höchstens 10, be­ sonders bevorzugt aus einer und höchstens zwei Ringleitungen mit je einer Pumpe pro Ringleitung zum Umpumpen des Leitungsinhaltes. Diese Ringleitungen können hinter der Pumpe auf 1 bis 100 Leitungen aufgeteilt werden, die vor der Pumpe wieder zusammengeführt werden, bevorzugt wird auf eine Aufteilung auf mehrere Leitungen verzichtet. Der Durchmesser der Ringleitungen liegt zwischen 0,5 und 50 cm, bevorzugt zwischen 1 und 10 cm. Jede Ringleitung hat eine separate Zu­ leitung über die der Nitroaromat gegebenenfalls zusammen mit Verdünnungsmittel in die Ringleitung eindosiert wird.The dosing system used in the method according to the invention is at least at least from one and at most from 100, preferably from one and at most 10, be particularly preferably from one and at most two ring lines, each with a pump per ring line for pumping around the contents of the line. These ring lines can behind the pump to be divided into 1 to 100 lines, which are in front of the pump be merged again, preference is given to splitting into several Lines waived. The diameter of the ring lines is between 0.5 and 50 cm, preferably between 1 and 10 cm. Each ring line has a separate door Line through which the nitroaromatic may be used together with the diluent is metered into the ring line.

Die Ringleitungen besitzen im Inneren des Reaktors zwischen 2 und 200.000, bevor­ zugt zwischen 4 und 40.000, besonders bevorzugt zwischen 8 und 8000, ganz be­ sonders bevorzugt zwischen 16 und 1600, speziell zwischen 32 und 320 Austritts­ öffnungen zur Verteilung des zu dosierenden Nitroaromaten.The loop lines inside the reactor have between 2 and 200,000 before moves between 4 and 40,000, particularly preferably between 8 and 8,000, entirely particularly preferred between 16 and 1600, especially between 32 and 320 outlet openings for the distribution of the nitroaromatic to be dosed.

Die Austrittsöffnungen sind so gestaltet, daß eine möglichst gleichmäßige Nitro­ aromatenverteilung in den Reaktor erreicht wird. Der Durchmesser der Austrittsöff­ nungen liegt zwischen 0,001 und 10 mm, bevorzugt zwischen 0,01 und 1 mm, beson­ ders bevorzugt zwischen 0,1 und 0,5 mm.The outlet openings are designed so that the nitro is as uniform as possible aromatics distribution is achieved in the reactor. The diameter of the outlet opening is between 0.001 and 10 mm, preferably between 0.01 and 1 mm, in particular more preferably between 0.1 and 0.5 mm.

Das in dem erfindungsgemäßen Verfahren verwendete Dosiersystem wird bevorzugt derart gestaltet, daß der Inhalt der Kreisstromleitung durch einen Wärmetauscher ge­ pumpt wird, der die Temperatur des im Kreis gepumpten Eduktes zwischen 10 und 120°C, bevorzugt zwischen 30 und 100°C, besonders bevorzugt zwischen 50 und 80°C hält.The dosing system used in the method according to the invention is preferred designed so that the contents of the circuit flow line ge through a heat exchanger  is pumped, the temperature of the educt pumped in a circuit between 10 and 120 ° C, preferably between 30 and 100 ° C, particularly preferably between 50 and Holds at 80 ° C.

Wärmetauscher zur Kühlung von Ringleitungen befinden sich bevorzugt außerhalb des Reaktors.Heat exchangers for cooling ring lines are preferably located outside of the reactor.

In den erfindungsgemäßen Verfahren wird bevorzugt Dinitrotoluol zu Toluylen­ diamin hydriert. Dabei wird eine besonders geringe Nebenproduktbildung und Katalysatordesaktivierung beobachtet.Dinitrotoluene is preferred to tolylene in the process according to the invention diamine hydrogenated. A particularly low by-product formation and Catalyst deactivation observed.

Reaktoren können in dem erfindungsgemäßen Verfahren unter Normaldruck und unter Druck betrieben werden, bevorzugt werden die Reaktoren im Druckbereich zwischen 1 und 100 bar, besonders bevorzugt zwischen 3 und 30 bar betrieben.Reactors can in the process according to the invention under normal pressure and operated under pressure, the reactors in the pressure range are preferred operated between 1 and 100 bar, particularly preferably between 3 and 30 bar.

Das erfindungsgemäße Verfahren kann zur vorteilhaften Durchführung von Hydrierungen insbesondere von Sumpfphasenhydrierungen eingesetzt werden, wie sie beispielsweise in WO 96/11052 beschrieben werden.The method according to the invention can be used to advantageously carry out Hydrogenations are used, in particular by phase-phase hydrogenations, such as they are described, for example, in WO 96/11052.

Die Vorteile des erfindungsgemäßen Verfahrens zur Dosierung von Nitroaromaten sind Vermeidung von Katalysatordesaktivierung, Nebenproduktbildung und Über­ temperaturen, Vermeidung von Bereichen in denen Nitroaromaten bei hohen Tempe­ raturen in größeren Mengen längere Verweilzeiten haben und damit zu gefährlichen Zersetzungen neigen.The advantages of the process according to the invention for metering nitroaromatics are avoiding catalyst deactivation, by-product formation and over temperatures, avoiding areas in which nitroaromatics at high temperatures fittings in larger quantities have longer dwell times and are therefore dangerous Decomposition tend.

Das in dem erfindungsgemäßen Verfahren verwendete Dosiersystem kann besonders gut auf die Bildung von Verstopfungen überwacht werden. So zeigt eine Differenz­ druckmessung an einer Kreislaufpumpe eine beginnende Verstopfung des bevorzugt gekühlten Umpumpkreislaufes an, während eine Differenzdruckmessung zwischen Zufuhrleitung und Reaktorinnenraum eine beginnende Verstopfung der Austrittsöff­ nungen anzeigt.The dosing system used in the method according to the invention can be special be well monitored for the formation of constipation. So shows a difference pressure measurement on a circulatory pump an early blockage of the preferred cooled pump circuit during a differential pressure measurement between  Feed line and reactor interior a starting blockage of the outlet opening displays.

Das erfindungsgemäße Verfahren zeichnet sich durch eine große Betriebssicherheit aus, da der Nitroaromat im Inneren des heißen Reaktors gekühlt zugespeist werden kann und erst im Reaktor auf die Reaktionstemperatur erwärmt wird.The method according to the invention is characterized by great operational reliability off, since the nitroaromatic is fed in cooled inside the hot reactor can and is only heated to the reaction temperature in the reactor.

Fig. 1 zeigt ein Beispiel für das in dem erfindungsgemäßem Verfahren eingesetzte Dosiersystem am Beispiel eines Rührkessels. In Fig. 1 bezeichnet 1 die Reak­ torwand, 2 einen Begasungsrührer, 3 die Dosierpumpe, 4 die Kreislaufpumpe, 5 den Wärmetauscher zur Kühlung des Nitroaromaten und 6 die im Inneren des Reaktors mit Austrittsöffnungen versehene Ringleitung. Fig. 1 shows an example of the process of the invention used in the dosing system using the example of a stirred tank. In Fig. 1 1 2 denotes the reac goal wall, a gassing stirrer, 3, the dosing pump, the circulation pump 4, 5 is the heat exchanger for cooling of the nitroaromatic and 6 provided in the interior of the reactor with outlet openings ring line.

Claims (4)

1. Verfahren zur Dosierung von flüssigen Nitroaromaten mit mehr als einer Nitrogruppe, in Reaktoren zur Hydrierung, dadurch gekennzeichnet, daß a) der zu dosierende Nitroaromat in einer oder mehreren Ringleitungen im Kreis gepumpt wird, b) diese Ringleitungen ganz oder teilweise im Hydrierreaktor verlaufen, c) die Ringleitungen im Reaktorinneren mit Austrittsöffnungen zum Reaktorinneren versehen sind.1. A process for metering liquid nitroaromatics with more than one nitro group in reactors for hydrogenation, characterized in that a) the nitroaromatic to be metered is pumped in a circle in one or more ring lines, b) these ring lines run wholly or partly in the hydrogenation reactor, c) the ring lines in the interior of the reactor are provided with outlet openings to the interior of the reactor. 2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die Kreisstrom­ leitungen zwischen 2 und 200.000, bevorzugt zwischen 4 und 40.000, beson­ ders bevorzugt zwischen 8 und 8000, ganz besonders bevorzugt zwischen 16 und 1600, speziell zwischen 32 und 320 Ausstrittsöffnungen besitzen.2. The method according to claim 1, characterized in that the circulating current lines between 2 and 200,000, preferably between 4 and 40,000, especially more preferably between 8 and 8000, very particularly preferably between 16 and 1600, especially between 32 and 320 outlet openings. 3. Verfahren nach Anspruch 1 und 2, dadurch gekennzeichnet, daß der Inhalt der Kreisstromleitung durch einen Wärmetauscher gepumpt wird, der die Tempe­ ratur des im Kreis gepumpten Eduktes zwischen 10 und 120°C, bevorzugt zwischen 30 und 100°C, besonders bevorzugt zwischen 50 und 80°C hält.3. The method according to claim 1 and 2, characterized in that the content of the Circulating power line is pumped through a heat exchanger which is the tempe rature of the educt pumped in a circle between 10 and 120 ° C, preferred between 30 and 100 ° C, particularly preferably between 50 and 80 ° C. 4. Verfahren nach Anspruch 1 bis 3, dadurch gekennzeichnet, daß Dinitrotoluole zu Toluylendiaminen hydriert werden.4. The method according to claim 1 to 3, characterized in that dinitrotoluenes are hydrogenated to toluenediamines.
DE1998144901 1998-09-30 1998-09-30 Method for metering liquid polynitro-aromatic compounds into hydrogenation reactors Expired - Fee Related DE19844901C1 (en)

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Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2003068724A1 (en) * 2002-02-15 2003-08-21 Basf Aktiengesellschaft Method for the production of amines
US7595029B2 (en) 2001-08-30 2009-09-29 Air Products And Chemicals, Inc. Monolith catalytic reactor coupled to static mixer
WO2011086050A2 (en) 2010-01-14 2011-07-21 Bayer Materialscience Ag Method for producing aromatic amines in the liquid phase
WO2011144481A1 (en) 2010-05-17 2011-11-24 Basf Se Process for preparing tolylenediamine by hydrogenation of dinitrotoluene
WO2012123469A1 (en) 2011-03-16 2012-09-20 Basf Se Optimized metering of reactants for a process for preparing aromatic amines by hydrogenation of nitroaromatics
US8609899B2 (en) 2010-05-17 2013-12-17 Basf Se Process for preparing toluenediamine by hydrogenation of dinitrotoluene
US8835688B2 (en) 2011-03-16 2014-09-16 Basf Se Optimized introduction of the starting materials for a process for preparing aromatic amines by hydrogenation of nitroaromatics

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0263935A2 (en) * 1986-10-16 1988-04-20 Bayer Ag Process for cooling exothermal reactions and a reactor, particularly a stirrer reactor, for carrying out exothermal reactions
WO1996011052A1 (en) * 1994-10-07 1996-04-18 Bayer Aktiengesellschaft Sludge phase reactor and its use

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0263935A2 (en) * 1986-10-16 1988-04-20 Bayer Ag Process for cooling exothermal reactions and a reactor, particularly a stirrer reactor, for carrying out exothermal reactions
WO1996011052A1 (en) * 1994-10-07 1996-04-18 Bayer Aktiengesellschaft Sludge phase reactor and its use

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7595029B2 (en) 2001-08-30 2009-09-29 Air Products And Chemicals, Inc. Monolith catalytic reactor coupled to static mixer
WO2003068724A1 (en) * 2002-02-15 2003-08-21 Basf Aktiengesellschaft Method for the production of amines
KR100909409B1 (en) * 2002-02-15 2009-07-24 바스프 에스이 Method of Making Amines
WO2011086050A2 (en) 2010-01-14 2011-07-21 Bayer Materialscience Ag Method for producing aromatic amines in the liquid phase
US9150493B2 (en) 2010-01-14 2015-10-06 Bayer Intellectual Property Gmbh Method for producing aromatic amines in the liquid phase
WO2011144481A1 (en) 2010-05-17 2011-11-24 Basf Se Process for preparing tolylenediamine by hydrogenation of dinitrotoluene
US8609899B2 (en) 2010-05-17 2013-12-17 Basf Se Process for preparing toluenediamine by hydrogenation of dinitrotoluene
WO2012123469A1 (en) 2011-03-16 2012-09-20 Basf Se Optimized metering of reactants for a process for preparing aromatic amines by hydrogenation of nitroaromatics
US8835688B2 (en) 2011-03-16 2014-09-16 Basf Se Optimized introduction of the starting materials for a process for preparing aromatic amines by hydrogenation of nitroaromatics
US9308515B2 (en) 2011-03-16 2016-04-12 Basf Se Optimized introduction of the starting materials for a process for preparing aromatic amines by hydrogenation of nitroaromatics

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