EP0341547A1 - Process for catalytic hydrogenation of lanolin to lanolin alcohol - Google Patents

Process for catalytic hydrogenation of lanolin to lanolin alcohol Download PDF

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Publication number
EP0341547A1
EP0341547A1 EP89107908A EP89107908A EP0341547A1 EP 0341547 A1 EP0341547 A1 EP 0341547A1 EP 89107908 A EP89107908 A EP 89107908A EP 89107908 A EP89107908 A EP 89107908A EP 0341547 A1 EP0341547 A1 EP 0341547A1
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Prior art keywords
catalyst
lanolin
weight
hydrogen
percent
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EP89107908A
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German (de)
French (fr)
Inventor
Theo Dr. Fleckenstein
Joachim Dr. Pohl
Gerd Dr Göbel
Franz-Josef Dr. Carduck
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Henkel AG and Co KGaA
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Henkel AG and Co KGaA
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Publication of EP0341547A1 publication Critical patent/EP0341547A1/en
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    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
    • C11B11/00—Recovery or refining of other fatty substances, e.g. lanolin or waxes
    • C11B11/005—Lanolin; Woolfat

Definitions

  • the invention relates to a process for the catalytic hydrogenation of lanolin to wool wax alcohol or lanolin alcohol.
  • Lanolin is understood here to mean anhydrous, purified lanolin of standard quality.
  • Lanolin or wool wax is the sheep's sebum secretion.
  • the wool wax is obtained from the raw wool by machine washing with soapy water in an emulsified form.
  • Rohlanolin is obtained from this emulsion. This Rohlanolin is a greasy, viscous, brown-yellow to brown-black, greasy mass with a penetrating, goat-like smell.
  • Bleaching with hydrogen peroxide with the addition of phosphoric acid gives the so-called neutral wool wax from the rohlanolin.
  • Neutral wool wax is yellow to light brown in color and has a softened odor. Will it be e.g. Treated with adsorbents such as bleaching earth or activated carbon, you get Adeps lanae, which is a light yellow, almost odorless substance.
  • One refining process is to hydrogenate lanolin. It is catalytically hydrogenated in the bottom phase (suspension hydrogenation) at a pressure of 250 bar in five stages in a temperature range between 250 ° C and 310 ° C.
  • lanolin Since lanolin still contains catalyst poisons despite the cleaning mentioned, it must be detoxified before hydrogenation. The prehydrogenation and the subsequent main hydrogenation then take place. Despite the detoxification, a large amount of catalyst, namely 3 to 5 kg of catalyst mass per 100 kg of lanolin is consumed. Another disadvantage of the known method is that side reactions with undesirable reaction products occur due to the relatively high temperatures. These reaction products deteriorate the quality of the lanolin alcohol.
  • the object of the invention is to achieve a better quality of the end product with a lower catalyst consumption in a continuous process for the catalytic hydrogenation of lanolin.
  • This object is achieved by reacting lanolin together with hydrogen at pressures from 20 bar to 300 bar, temperatures from 225 ° C. to 260 ° C. and with weight ratios of hydrogen: lanolin from 1: 1 to 10: 1 over catalysts which 30 to 40% by weight of copper, 23 to 30% by weight of chromium, 1 to 10% by weight of manganese, 1 to 10% by weight of silicon and 1 to 7% by weight of barium and, if desired, further transition metals in the form contain their oxides and after calcining the components forming the catalyst with 1 to 10 wt .-%, based on the oxidic catalyst, of at least one binder converted into lumpy and / or granular moldings and activated with hydrogen or a mixture containing hydrogen.
  • the process product can be used in dermatics and cosmetic preparations.
  • the catalyst based on the oxidic catalyst mass, contains 32 to 38% by weight of copper.
  • the catalyst preferably contains 1.5 to 3% by weight of barium, based on the oxidic catalyst mass.
  • a process is also preferred in which the catalyst, based on the oxidic catalyst mass, is 32 to 38% by weight of copper, 26 to 29% by weight of chromium, 1.5 to 3% by weight of barium and 0.5 to 2 % By weight of silicon and additionally 1 to 5, preferably 2 to 3 each % By weight, based on the oxidic catalyst mass, contains manganese.
  • the catalyst has a particle size in the range from 0.2 to 6 mm, preferably from 0.5 to 4 mm.
  • a catalyst which has a specific surface area in the range from 20 to 40 m 2 / g, preferably from 25 to 30 m 2 / g. It is also advantageous if the catalyst has a pore volume in the range from 0.1 to 1.0 cm3 / g.
  • reaction pressure is 230 to 270 bar. It is also advantageous if the lanolin flows with hydrogen through a trickle bed containing the catalyst.
  • the catalyst is charged with 0.1 to 2 l of lanolin per liter of catalyst per hour, in particular 0.25 to 0.5 h -1.
  • the process is particularly effective when a granular form of the catalyst is used.
  • the granules do not clog the reactor, as is to be feared in similar processes.
  • the irregular shape of the granules and the resulting increased surface area make the catalyst more effective.
  • the invention is not limited to catalysts in granular form, since both lumpy and granular catalysts can be used.
  • the starting product is purified, anhydrous lanolin originating in Australia and with less than 1% acids.
  • the lanolin is free of oxidized fatty acids.
  • the sulfur content before the hydrogenation was 40 ppm, the chlorine content 16 ppm.
  • the catalyst specified in DE-OS 36 24 812 in Example 2 was used.

Abstract

To obtain an end product of a higher quality, the lanolin is reacted with hydrogen, at a pressure comprised between 20 and 300 bars, at a temperature comprised between 225 and 260 DEG C and in hydrogen to lanolin weight proportions comprised between 1 to 1 and 1 to 10, by means of catalysts which contain between 30 and 40 percent by weight of copper, between 23 and 30 percent by weight of chromium, between 1 and 10 percent by weight of manganese, between 1 and 10 percent by weight of silicon and between 1 and 7 percent by weight of barium, as well as, optionally, other transition metals in the form of their oxides, and which, after the components constituting them have been calcinated, have been transformed into lumps and/or grains of an aggregate with between 1 and 10 percent by weight, relative to the oxidation catalyst, of at least one binder and activated with hydrogen or a mixture containing hydrogen.

Description

Die Erfindung betrifft ein Verfahren zum katalytischen Hydrieren von Lanolin zu Wollwachsalkohol oder Lanolinalkohol. Unter Lanolin wird hier wasserfreies, gereinigtes Lanolin von Standardqualität verstanden.The invention relates to a process for the catalytic hydrogenation of lanolin to wool wax alcohol or lanolin alcohol. Lanolin is understood here to mean anhydrous, purified lanolin of standard quality.

Lanolin oder Wollwachs ist das Talgdrüsensekret der Schafe. Aus der Rohwolle wird das Wollwachs durch maschinelles Waschen mit Seifenlauge in emulgierter Form gewonnen. Aus dieser Emulsion wird Rohlanolin gewonnen. Dieses Rohlanolin ist eine schmierig zähe, braungelbe bis braunschwarze, fettartige Masse von penetrantem, bockartigem Geruch. Durch bestimmte Reinigungsschritte, z.B. Blei­chen mit Wasserstoffperoxid unter Zusatz von Phosphorsäure erhält man aus dem Rohlanolin das sogenannte Neutralwollwachs. Neutral­wollwachs ist von gelber bis hellbrauner Farbe und gemildertem Geruch. Wird es noch z.B. mit Adsorbtionsmitteln wie Bleicherde oder Aktivkohle nachbehandelt, so erhält man Adeps lanae, welches eine hellgelbe, fast geruchsfreie Substanz ist.Lanolin or wool wax is the sheep's sebum secretion. The wool wax is obtained from the raw wool by machine washing with soapy water in an emulsified form. Rohlanolin is obtained from this emulsion. This Rohlanolin is a greasy, viscous, brown-yellow to brown-black, greasy mass with a penetrating, goat-like smell. Through certain cleaning steps, e.g. Bleaching with hydrogen peroxide with the addition of phosphoric acid gives the so-called neutral wool wax from the rohlanolin. Neutral wool wax is yellow to light brown in color and has a softened odor. Will it be e.g. Treated with adsorbents such as bleaching earth or activated carbon, you get Adeps lanae, which is a light yellow, almost odorless substance.

Ein Veredlungsverfahren besteht darin, Lanolin zu hydrieren. Dabei wird in der Sumpfphase (Suspensionshydrierung) bei einem Druck von 250 bar in fünf Stufen in einem Temperaturbereich zweichen 250°C und 310°C katalytisch hydriert.One refining process is to hydrogenate lanolin. It is catalytically hydrogenated in the bottom phase (suspension hydrogenation) at a pressure of 250 bar in five stages in a temperature range between 250 ° C and 310 ° C.

Da Lanolin trotz der erwähnten Reinigung noch Katalysatorgifte enthält, muß es vor dem Hydrieren entgiftet werden. Danach findet die Vorhydrierung und die anschließende Haupthydrierung statt. Trotz der Entgiftung wird eine große Menge an Katalysator, nämlich 3 bis 5 kg an Katalysatormasse pro 100 kg Lanolin verbraucht. Ein weiterer Nachteil des bekannten Verfahrens besteht darin, daß in­folge der relativ hohen Temperaturen Nebenreaktionen mit uner­wünschten Reaktionsprodukten auftreten. Diese Reaktionsprodukte verschlechtern die Qualität des Lanolinalkohols.Since lanolin still contains catalyst poisons despite the cleaning mentioned, it must be detoxified before hydrogenation. The prehydrogenation and the subsequent main hydrogenation then take place. Despite the detoxification, a large amount of catalyst, namely 3 to 5 kg of catalyst mass per 100 kg of lanolin is consumed. Another disadvantage of the known method is that side reactions with undesirable reaction products occur due to the relatively high temperatures. These reaction products deteriorate the quality of the lanolin alcohol.

Der Erfindung liegt die Aufgabe zugrunde, in einem insbesondere kontinuierlichen Verfahren zum katalytischen Hydrieren von Lanolin eine bessere Qualität des Endproduktes bei geringerem Katalysa­torverbrauch zu erreichen.The object of the invention is to achieve a better quality of the end product with a lower catalyst consumption in a continuous process for the catalytic hydrogenation of lanolin.

Diese Aufgabe wird dadurch gelöst, daß man Lanolin zusammen mit Wasserstof bei Drücken von 20 bar bis 300 bar, Temperaturen von 225°C bis 260°C und bei Gewichtsverhältnissen von Wasserstoff : Lanolin von 1:1 bis 10:1 über Katalysatoren umsetzt, die 30 bis 40 Gew.-% Kupfer, 23 bis 30 Gew.-% Chrom, 1 bis 10 Gew.-% Mangan, 1 bis 10 Gew.-% Silicium und 1 bis 7 Gew.-% Barium sowie gewünsch­tenfalls weitere Übergangsmetalle in Form ihrer Oxide enthalten und nach dem Calcinieren der den Katalysator bildenden Komponenten mit 1 bis 10 Gew.-%, bezogen auf des oxidischen Katalysator, we­nigstens eines Binders zu stückigen und/oder gekörnten Formlingen umgewandelt und mit Wasserstoff oder einem Wasserstoff enthalten­den Gemisch aktiviert worden sind.This object is achieved by reacting lanolin together with hydrogen at pressures from 20 bar to 300 bar, temperatures from 225 ° C. to 260 ° C. and with weight ratios of hydrogen: lanolin from 1: 1 to 10: 1 over catalysts which 30 to 40% by weight of copper, 23 to 30% by weight of chromium, 1 to 10% by weight of manganese, 1 to 10% by weight of silicon and 1 to 7% by weight of barium and, if desired, further transition metals in the form contain their oxides and after calcining the components forming the catalyst with 1 to 10 wt .-%, based on the oxidic catalyst, of at least one binder converted into lumpy and / or granular moldings and activated with hydrogen or a mixture containing hydrogen.

Mit Hilfe dieses neuen Verfahrens konnte bei überraschend niedri­gen Temperaturen hydriert werden, die entsprechend weniger uner­wünschte Nebenprodukte zur Folge hatten. Dabei verringerte sich der Katalysatorverbrauch auf weniger als 1/9 des Wertes bei dem bekannten Verfahren. Anstelle der vorher benötigten fünf Verfahrensstufen ist in dem erfindungs­gemäßen Verfahren nur ein einziger Verfahrensschritt erforder­lich.With the help of this new process it was possible to hydrogenate at surprisingly low temperatures, which resulted in fewer undesirable by-products. The catalyst consumption was reduced to less than 1/9 of the value in the known method. Instead of Five process steps previously required are only required for a single process step in the process according to the invention.

Bein Hydrieren des natürlichen Wollwachses, welches keine Tri­glyceride, also Fette, enthält, sondern ein echtes Wachs ist, wird die Esterzahl von etwa 100 auf maximal 5 gesenkt und die Hydro­xylzahl entsprechend erhöht. Das bräunlich bis dunkel gefärbte Ausgangsmaterial mit unangenehmen Geruch wird farblos bis leicht gelb mit fruchtigem Geruch. Bei der Hydrierung werden die Fett­säuren und Hydroxyfettsäuren zu den entsprechenden Fett- bzw. Wachsalkoholen reduziert und vorhandene olefinische Doppelbin­dungen abgesättigt. Die Reaktionsvorgänge bei der Hydrierung sind jedoch schon deshalb im einzelnen noch unbekannt, weil Lanolin aus einem komplizierten, in seiner Zusammensetzung noch nicht völlig aufgeklärten Estergemisch besteht.When hydrogenating natural wool wax, which does not contain triglycerides, i.e. fats, but is a real wax, the ester number is reduced from about 100 to a maximum of 5 and the hydroxyl number is increased accordingly. The brownish to dark colored starting material with an unpleasant smell turns colorless to slightly yellow with a fruity smell. During the hydrogenation, the fatty acids and hydroxy fatty acids are reduced to the corresponding fatty or wax alcohols and existing olefinic double bonds are saturated. However, the reaction processes in the hydrogenation are still unknown in detail because lanolin consists of a complicated ester mixture which has not yet been fully elucidated in its composition.

Das Verfahrensprodukt kann in Dermatika und kosmetischen Zube­reitungen verwendet werden.The process product can be used in dermatics and cosmetic preparations.

Besonders vorteilhaft ist es, wenn die Umsetzung kontinuierlich erfolgt.It is particularly advantageous if the implementation takes place continuously.

Vorteilhaft ist, wenn der Katalysator, bezogen auf die oxidische Katalysatormasse, 32 bis 38 Gew.-% Kupfer enthält.It is advantageous if the catalyst, based on the oxidic catalyst mass, contains 32 to 38% by weight of copper.

Vorzugsweise enthält der Katalysator, bezogen auf die oxidische Katalysatormasse, 1,5 bis 3 Gew.-% Barium.The catalyst preferably contains 1.5 to 3% by weight of barium, based on the oxidic catalyst mass.

Bevorzugt ist auch ein Verfahren, wobei der Katalysator, bezogen auf die oxidische Katalysatormasse, 32 bis 38 Gew.-% Kupfer, 26 bis 29 Gew.-% Chrom, 1,5 bis 3 Gew.-% Barium und 0,5 bis 2 Gew.-% Silizium und zusätzlich je 1 bis 5, bevorzugt 2 bis 3 Gew.-%, bezogen auf die oxidische Katalysatormasse, Mangan ent­hält.A process is also preferred in which the catalyst, based on the oxidic catalyst mass, is 32 to 38% by weight of copper, 26 to 29% by weight of chromium, 1.5 to 3% by weight of barium and 0.5 to 2 % By weight of silicon and additionally 1 to 5, preferably 2 to 3 each % By weight, based on the oxidic catalyst mass, contains manganese.

Ferner ist es vorteilhaft, wenn der Katalysator eine Korngröße im Bereich von 0,2 bis 6 mm, bevorzugt von 0,5 bis 4 mm aufweist.It is also advantageous if the catalyst has a particle size in the range from 0.2 to 6 mm, preferably from 0.5 to 4 mm.

Weiterhin wird ein Katalysator bevorzugt, der eine spezifische Oberfläche im Bereich von 20 bis 40 m²/g, bevorzugt von 25 bis 30 m²/g aufweist. Vorteilhaft ist ebenfalls, wenn der Katalysator ein Porenvolumen im Bereich von 0,1 bis 1,0 cm³/g aufweist.Furthermore, a catalyst is preferred which has a specific surface area in the range from 20 to 40 m 2 / g, preferably from 25 to 30 m 2 / g. It is also advantageous if the catalyst has a pore volume in the range from 0.1 to 1.0 cm³ / g.

Bei einer weiteren vorteilhaften Ausführung des Verfahrens be­trägt der Reaktionsdruck 230 bis 270 bar. Vorteilhaft ist auch, wenn das Lanolin mit Wasserstoff durch ein den Katalysator ent­haltendes Rieselbett strömt.In a further advantageous embodiment of the method, the reaction pressure is 230 to 270 bar. It is also advantageous if the lanolin flows with hydrogen through a trickle bed containing the catalyst.

Die Vorteile dieses Verfahrens treten auch auf, wenn Neutral­lanolin anstelle von Rohlanolin verwendet wird.The advantages of this process also occur if neutral ethanol is used instead of crude alcohol.

In einer anderen bevorzugten Ausführungsform wird der Kataly­sator mit 0,1 bis 2 l Lanolin pro Liter Katalysator und Stunde, insbesondere 0,25 bis 0,5 h⁻¹, belastet.In another preferred embodiment, the catalyst is charged with 0.1 to 2 l of lanolin per liter of catalyst per hour, in particular 0.25 to 0.5 h -1.

Das Verfahren ist besonders effektiv, wenn eine Granulatform des Katalysators verwendet wird. Das Granulat führt in diesem Fall nicht, wie bei ähnlichen Verfahren zu befürchten ist, zu einem Verstopfen des Reaktors. Die unregelmäßige Form des Granulats und die dadurch vergrößerte Oberfläche führt zu der größeren Wirksamkeit des Katalysators. Die Erfindung ist jedoch nicht auf Katalysatoren in Granulatform beschränkt, denn es können sowohl stückige als auch gekörnte Katalysatoren verwendet werden.The process is particularly effective when a granular form of the catalyst is used. In this case, the granules do not clog the reactor, as is to be feared in similar processes. The irregular shape of the granules and the resulting increased surface area make the catalyst more effective. However, the invention is not limited to catalysts in granular form, since both lumpy and granular catalysts can be used.

Im folgenden wird die Erfindung anhand zweier Ausführungsbei­spiele näher beschrieben.The invention is described in more detail below with reference to two exemplary embodiments.

In beiden Fällen ist das Ausgangsprodukt gereinigtes, wasser­freies Lanolin mit dem Ursprungsland Australien und mit weniger als 1% Säuren. Das Lanolin ist frei von oxidierten Fettsäuren. Der Schwefelgehalt betrug vor dem Hydrieren 40 ppm, der Chlorgehalt 16 ppm. In beiden Fällen wurde der in der DE-OS 36 24 812 in Beispiel 2 angegebene Katalysator verwendet.In both cases, the starting product is purified, anhydrous lanolin originating in Australia and with less than 1% acids. The lanolin is free of oxidized fatty acids. The sulfur content before the hydrogenation was 40 ppm, the chlorine content 16 ppm. In both cases, the catalyst specified in DE-OS 36 24 812 in Example 2 was used.

Beispiel 1example 1

0,5 Liter Kupferchromit-Katalysator, Granulat der Korngröße 1,6 mm bis 2,0 mm wurden in einem Rohrreaktor mit dem Durchmesser 25 mm nach der Aktivierung mit 0,25 l Lanolin (roh) pro Stunde (Spezifikation: Säurezahl SZ kleiner 1, Verseifungszahl VZ = 90 bis 100; Schwefelgehalt = 33 ppm) und 10 Nm³/h Wasserstoff (99%) in Kontakt gebracht. Lanolin und Wasserstoff strömten gleichsin­nig im Rieselbett von oben nach unten. Der Reaktionsdruck be­trug 250 bar, die reaktionstemperatur 230°C bis 260°C.0.5 liters of copper chromite catalyst, granules with a grain size of 1.6 mm to 2.0 mm were in a tubular reactor with a diameter of 25 mm after activation with 0.25 l of lanolin (raw) per hour (specification: acid number SZ less than 1 , Saponification number VZ = 90 to 100; sulfur content = 33 ppm) and 10 Nm³ / h hydrogen (99%). Lanolin and hydrogen flowed in the same direction in the trickle bed from top to bottom. The reaction pressure was 250 bar, the reaction temperature 230 ° C to 260 ° C.

Das Hydrierprodukt besaß folgende Kennzahlen:
VZ kleiner 5,0; Hydroxylzahl OHZ = 175; Kohlenwasserstoff-Ge­halt: 6,4 Gew.-%; Schwefelgehalt: 8 ppm ; Farbzahl (Hazen) : 3.The hydrogenation product had the following key figures:
VZ less than 5.0; Hydroxyl number OHZ = 175; Hydrocarbon content: 6.4% by weight; Sulfur content: 8 ppm; Color number (Hazen): 3.

Beispiel 2Example 2

32 Liter des in Beispiel 1 verwendeten Katalysators in Form von zylindrischen Tabletten der Größe 6 x 3 mm wurden in einem Rohrreaktor des Durchmessers 113 mm mit 6 l/h Lanolin (roh) und 375 Nm³/h Wasserstoff in Kontakt gebracht. Der Reaktionsdruck betrag 250 bar, die Reaktionstemperatur lag zwischen 225°C und 250°C.32 liters of the catalyst used in Example 1 in the form of cylindrical tablets of size 6 × 3 mm were brought into contact in a tubular reactor with a diameter of 113 mm with 6 l / h lanolin (crude) and 375 Nm 3 / h hydrogen. The reaction pressure was 250 bar, the reaction temperature was between 225 ° C and 250 ° C.

Das Hydrierprodukt besaß folgende Kennzahlen:
VZ kleiner 6,0; OHZ = 170; Kohlenwasserstoffgehalt: 9,0 Gew.-%; Farbzahl (Hazen): 50.The hydrogenation product had the following key figures:
VZ less than 6.0; OHZ = 170; Hydrocarbon content: 9.0% by weight; Color number (Hazen): 50.

Claims (13)

1. Verfahren zum katalytischen Hydrieren von Lanolin zu Lanolinal­kohol,
dadurch gekennzeichnet,
daß man Lanolin zusammen mit Wasserstof bei Drücken von 20 bar bis 300 bar, Temperaturen von 225°C bis 260°C und bei Gewichts­verhältnissen von Wasserstoff : Lanolin von 1:1 bis 10:1 über Katalysatoren umsetzt, die 30 bis 40 Gew.-% Kupfer, 23 bis 30 Gew.-% Chrom, 1 bis 10 Gew.-% Mangan, 1 bis 10 Gew.-% Silicium und 1 bis 7 Gew.-% Barium sowie gewünschtenfalls weitere Über­gangsmetalle in Form ihrere oxide enthalten und nach dem Calci­nieren der den Katalysator bildenden komponenten mit 1 bis 10 Gew.-%, bezogen auf den oxidischen Katalysator, wenigstens ei­nes Binders zu stückigen und/oder gekörnten Formlingen umge­wandelt und mit Wasserstoff oder einem Wasserstoff enthaltendem Gemisch aktiviert worden sind.1. Process for the catalytic hydrogenation of lanolin to lanolin alcohol,
characterized,
that lanolin is reacted together with hydrogen at pressures from 20 bar to 300 bar, temperatures from 225 ° C. to 260 ° C. and with weight ratios of hydrogen: lanolin from 1: 1 to 10: 1 over catalysts which contain 30 to 40% by weight. % Copper, 23 to 30% by weight chromium, 1 to 10% by weight manganese, 1 to 10% by weight silicon and 1 to 7% by weight barium and, if desired, further transition metals in the form of their oxides and after Calcining the components forming the catalyst with 1 to 10 wt .-%, based on the oxidic catalyst, of at least one binder converted into lumpy and / or granular moldings and activated with hydrogen or a mixture containing hydrogen. 2. Verfahren nach Anspruch 1,
dadurch gekennzeichnet,
daß die Umsetzung kontinuierlich erfolgt.2. The method according to claim 1,
characterized,
that the implementation takes place continuously. 3. Verfahren nach Anspruch 1 oder 2,
dadurch gekennzeichnet, daß der Katalysator, bezogen auf die Oxidische Katalysatormasse, 32 bis 38 Gew.-% Kupfer enthält.3. The method according to claim 1 or 2,
characterized in that the catalyst, based on the oxide catalyst mass, contains 32 to 38% by weight of copper. 4. Verfahren nach einem der Ansprüche 1 bis 3,
dadurch gekennzeichnet,
daß der Katalysator, bezogen auf die oxidische Katalysatormas­se, 1,5 bis 3 Gew.-% Barium enthält.4. The method according to any one of claims 1 to 3,
characterized,
that the catalyst, based on the oxidic catalyst mass, contains 1.5 to 3 wt .-% barium. 5. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß der Katalysator, bezogen auf die oxidische Katalysator­masse, 32 bis 38 Gew.-% Kupfer, 26 bis 29 Gew.-% Chrom, 1,5 bis 3 Gew.-% Barium und 0,5 bis 2 Gew.-% Silicium und zusätzlich je 1 bis 5, bevorzugt 2 bis 3 Gew.-%, bezogen auf die oxidische Katalysatormasse, Mangan enthält.5. The method according to claim 1 or 2, characterized in that the catalyst, based on the oxidic catalyst mass, 32 to 38 wt .-% copper, 26 to 29 wt .-% chromium, 1.5 to 3 wt .-% barium and 0.5 to 2 wt .-% silicon and additionally 1 to 5, preferably 2 to 3 wt .-%, based on the oxidic catalyst mass, contains manganese. 6. Verfahren nach einem der Ansprüche 1 bis 5, dadurch ge­kennzeichnet, daß der Katalysator eine Korngröße im Bereich von 0,2 bis 6 mm, bevorzugt von 0,5 bis 4 mm, aufweist.6. The method according to any one of claims 1 to 5, characterized in that the catalyst has a grain size in the range from 0.2 to 6 mm, preferably from 0.5 to 4 mm. 7. Verfahren nach einem der Ansprüche 1 bis 6, dadurch ge­kennzeichnet, daß der Katalysator eine spezifische Ober­fläche im Bereich von 20 bis 40 m²/g, bevorzugt von 25 bis 30 m²/g aufweist.7. The method according to any one of claims 1 to 6, characterized in that the catalyst has a specific surface area in the range from 20 to 40 m² / g, preferably from 25 to 30 m² / g. 8. Verfahren nach einem der Ansprüche 1 bis 7, dadurch ge­kennzeichnet, daß der Katalysator ein Porenvolumen im Be­reich von 0,1 bis 1,0 cm³/g aufweist.8. The method according to any one of claims 1 to 7, characterized in that the catalyst has a pore volume in the range of 0.1 to 1.0 cm³ / g. 9. Verfahren nach einem der Ansprüche 1 bis 8, dadurch ge­kennzeichnet, daß der Reaktionsdruck 230 bis 270 bar be­trägt.9. The method according to any one of claims 1 to 8, characterized in that the reaction pressure is 230 to 270 bar. 10. Verfahren nach einem der Ansprüche 1 bis 9, dadurch ge­kennzeichnet, daß das Lanolin mit Wasserstoff durch ein den Katalysator enthaltendes Rieselbett strömt.10. The method according to any one of claims 1 to 9, characterized in that the lanolin flows with hydrogen through a trickle bed containing the catalyst. 11. Verfahren nach einem der Ansprüche 1 bis 10, dadurch ge­kennzeichnet, daß das Lanolin Neutrallanolin verwendet wird.11. The method according to any one of claims 1 to 10, characterized in that the lanolin neutral alcohol is used. 12. Verfahren nach einem der Ansprüche 1 bis 11, dadurch gekennzeichnet, daß der Katalysator mit 0,1 bis 2 l Lanolin pro l Katalysator und Stunde, insbesondere 0,25 bis 0,5 h⁻¹, belastet wird.12. The method according to any one of claims 1 to 11, characterized characterized in that the catalyst is charged with 0.1 to 2 l lanolin per l catalyst and hour, in particular 0.25 to 0.5 h⁻¹. 13. Verfahren nach einem der Ansprüche 1 bis 12, dadurch ge­kennzeichnet, daß eine Granulatform des Katalysators ver­wendet wird.13. The method according to any one of claims 1 to 12, characterized in that a granular form of the catalyst is used.
EP89107908A 1988-05-09 1989-05-02 Process for catalytic hydrogenation of lanolin to lanolin alcohol Withdrawn EP0341547A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19883815755 DE3815755A1 (en) 1988-05-09 1988-05-09 METHOD FOR CATALYTIC HYDRATING LANOLIN
DE3815755 1988-05-09

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EP0341547A1 true EP0341547A1 (en) 1989-11-15

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EP19890905656 Withdrawn EP0426684A1 (en) 1988-05-09 1989-05-02 Process for producing lanolin-alcohol from lanolin by catalytic hydrogenation
EP89107908A Withdrawn EP0341547A1 (en) 1988-05-09 1989-05-02 Process for catalytic hydrogenation of lanolin to lanolin alcohol

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EP19890905656 Withdrawn EP0426684A1 (en) 1988-05-09 1989-05-02 Process for producing lanolin-alcohol from lanolin by catalytic hydrogenation

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CN (1) CN1039439A (en)
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WO2004011581A1 (en) * 2002-07-26 2004-02-05 Croda International Plc Compositions formed from the reduction of lanolin

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CN100438976C (en) * 2005-12-07 2008-12-03 南化集团研究院 Catalyst for alduronic gas-phase hydrogenation to prepare alditol and preparing method
CN100398633C (en) * 2006-05-19 2008-07-02 浙江大学 Method for non-catalytic lanolin hydrolyzed preparation of lanolin acid and lanolin alcohol using in near critical water medium
AT514649B1 (en) 2013-08-14 2016-02-15 Geoplast Kunststofftechnik Ges M B H Method and device for monitoring the transport of solid free-flowing heating material, such as wood chips or pellets

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EP0254189A2 (en) * 1986-07-23 1988-01-27 Henkel Kommanditgesellschaft auf Aktien Process for direct hydrogenation of glyceric oils

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EP0254189A2 (en) * 1986-07-23 1988-01-27 Henkel Kommanditgesellschaft auf Aktien Process for direct hydrogenation of glyceric oils

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Cited By (2)

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Publication number Priority date Publication date Assignee Title
WO2004011581A1 (en) * 2002-07-26 2004-02-05 Croda International Plc Compositions formed from the reduction of lanolin
GB2391808B (en) * 2002-07-26 2004-12-29 Croda Int Plc Lanolin hydrocarbon containing compositions from the reduction of lanolin or lanolin-derived feedstock

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DE3815755A1 (en) 1989-11-23
CN1039439A (en) 1990-02-07
WO1989010952A1 (en) 1989-11-16
EP0426684A1 (en) 1991-05-15

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