EP2627744A1

EP2627744A1 - Method for removing compounds containing phosphorus from compositions containing triglyceride

Info

Publication number: EP2627744A1
Application number: EP11779117.8A
Authority: EP
Inventors: Ulrich Sohling; Friedrich Ruf; Andrea Stege
Original assignee: Sued Chemie IP GmbH and Co KG
Current assignee: Sued Chemie IP GmbH and Co KG
Priority date: 2010-10-13
Filing date: 2011-10-13
Publication date: 2013-08-21
Also published as: US8987487B2; DE102010048367A1; US20140012025A1; WO2012049232A1

Abstract

The invention relates to a method for removing compounds containing phosphorus from compositions containing triglyceride.

Description

Process for removing phosphorus-containing compounds from triglyceride-containing compositions

The present invention relates to a method for

Removal of phosphorus-containing compounds from triglyceride-containing compositions.

With the degumming or the degumming of vegetable oil is called the process, the phosphorus-containing

Remove compounds from the vegetable oil. If the vegetable oil used as a food, it is appropriate to the

Lower phosphorus content, as it increases the shelf life

is improved. In recent years, but also increasingly vegetable oil as a raw material for the chemical

Industry and used for the production of biodiesel. This trend goes hand in hand with the end of oil and gas supplies. Often, for the use of vegetable oil for the production of biodiesel or other chemical raw materials even sharper specifications in terms of

Final phosphorus value required. For example, the European standard limits the phosphorus content in biodiesel to 4 ppm, and it is likely that this value will be lowered further down to 1 ppm or even lower in the future.

In a process of the prior art for the production of biofuels, the vegetable oil with the aid of a

heterogeneous catalyst hydrogenated with hydrogen to paraffin. One example of such a process is the so-called Nex BTL process from Neste in Finland. Since phosphorus-containing compounds can poison heterogeneous catalysts, a particularly low phosphorus content in the vegetable oil must be set for this process. In addition to the examples given, there are a variety of other processes in which vegetable oil in chemical

Raw materials is used and due to the

Final specification or the use of heterogeneous

Catalysts require a particularly low phosphorus content in vegetable oil.

Hvolby [Hvolby A., JAOCS 48: 503 (1971)]

degummed soybean oil with a large amount of EDTA solution to remove calcium and phospholipids from the oil and to facilitate degumming (8 parts 10% EDTA solution to 1 part oil). Likewise, he treated crude soybean oil with the same volume ratio with a saturated one

Sodium pyrophosphate solution and obtained a 90% removal of non-hydratable phospholipids.

In DE 10257215 B4 Lurgi AG is a method

presented how the shelf life of biodiesel can be improved. For this purpose, in an intermediate step, the

Crude ester phase, inter alia, with a mixture of an acid and a complexing agent, such as EDTA, added and prepared at 50 ° C a fine emulsion. This emulsion breaks after about 30 minutes and the ester phase is then washed with water. The purified biodiesel thus obtained is virtually free of all condensation and crystallization germs as well as mucilages and iron compounds. In US 20090306419 Cargill describes a process in which an influx of vegetable crude oil is mixed with water with ultrahigh shear forces. Depending on the phosphorus content in the oil, the water may contain a complexing carboxylic acid such as citric acid and / or phosphoric acid and / or salts thereof be added. Subsequently, the resulting mucus is separated in a retention tank and fed the degummed oil of bleaching and deodorization.

In SU 1731793 Al is described as with a 0.1 to 0.5% aqueous solution of hydroxyethylenediphosphonic acid, nitrilotrimethylphosphonic acid or their K salts as

Complexing agent for degumming with citric acid

pretreated oils is worked.

The company Grace GmbH & CO. KG describes in WO 2009/068274 (EP 2008/010044) the use of liquid adsorbent solutions for the further purification of already pre-degummed vegetable oils or fatty acid methyl esters. As liquid adsorbents are here successively or in mixtures aqueous solutions of citric acid, caustic soda and

Suspensions of colloidal silica in water

used.

Oil Dri Corporation America explains in WO 9633621 AI a Vorreinigungsverfahren for vegetable oils, in which a clay with an organic acid is pulverized together. With this mixture, a pre-cleaning is done, to which a bleaching with bleaching earth is connected.

In a published research study Alfa-Laval AB describes, based on the RD 203006 a method in which shortly before the separation of the phospholipids after a

Treatment with a weak organic acid Water with a low content of a water-soluble polymeric substance is added. This would significantly reduce the proportion of non-hydratable phospholipids. As polymeric Substances are listed here anionic, cationic and nonionic polymers, such as starch, milk powder, casein, methyl cellulose and gum arabic.

In EP 269277 Bl the Cambrian Engineering Group Ltd. Degumming at below 40 ° C is preferred. The vegetable oil is washed with a weak organic acid, e.g. a 50% citric acid solution, a certain amount

Added water and degummed at below 40 ° C with stirring. The precipitated mucilages are separated by centrifugation and the oil with a further bleaching with

fed to conventional bleaching earth. Other possible organic acids include maleic acid, acetic anhydride, lactic acid and oxalic acid in aqueous saturated solution.

Oilseeds Biorefinery Corporation George Town (EP 02053118 Al) describes the removal of phospholipids

Fats / oils by enzymatic pretreatment and subsequent washing with an aqueous solution of a

Complexing agent from the group of ethylenediaminetetraacetic acid, β-alaninediacetic acid, nitrilotriacetic acid,

Diethylenetriaminepentaacetic acid, hydroxyethylethylenediaminetriacetic acid, iminodiacetate or an aqueous solution of an acid such as citric acid, lactic acid, fumaric acid, tartaric acid or phosphoric acid or both.

In AU 728062 B2, the oil is first treated with an organic acid from the group citric acid, malic acid,

Ethylenediaminetetraacetic acid, treated tartaric acid, oxalic acid, maleic acid ^¬ or an inorganic acid such as phosphoric acid, salt ^¬ acid or sulfuric acid. After sufficient An aqueous solution of a carboxylic acid having at least 3 carboxyl groups in the acid form or as a salt with a monovalent ion as the electrolyte or complexing agent is added, in which case the sodium salt of EDTA is preferably used. The non-hydratable phospholipids are thereby converted into a hydratable form and can be removed with the aqueous phase. Before separation of the oil phase, a surfactant (Na lauryl sulfate) may be added.

The same is also described in CA 2164840. Here is an organic acid such as citric acid, phosphoric acid,

Oxalic, tartaric, aminocarboxylic,

Polyhydroxycarboxylic acids, polycarboxylic acids, their salts, their mixtures with one another and a surfactant of the anionic, cationic, zwitterionic or nonionic added or formed in situ, used for degumming. Also preferred here with trisodium citrate or

Sodium salt of EDTA with sodium lauryl sulfate as a surfactant at 60 - 90 ° C worked.

The use of citric acid for degumming

Vegetable oils are treated in many other publications (eg DE 2609705 C3, DD 284043 A5, CA 2434499 C, CA 2351338 C, GB 01510056 A, Smiles et al.), wherein the acid in aqueous solution in different concentrations at different temperatures for different Long

Times with the oil comes into contact. Nash et al. (1984)

combine citric acid in high concentrations with

Surfactants, such as oxazoline, polymeric sulfonates or alkyl sulfates or with crude lecithin, which although to a

Reduction of phosphorus content leads, but the final content still very high precipitates. United Oilseeds Products Ltd. in patent CA 1157883 of 1983 describes the use of citric acid for the

Degumming at preferably temperatures between 40 and 75 ° C.

Choukri et al. describes the use of EDTA in the

Degumming of crude oil or water pre-degummed oil. Here, 5% of an aqueous EDTA solution is optimally added to the oil at> 65 ° C, a surfactant (sodium lauryl sulfate) was added and mixed for 20 min.

0. Zufarov et al. (Eur. J. Lipid Sci. Technol. 2009, 111, 0000-0000) deals with water-degummed rapeseed oil and

Sunflower oil at room temperature by adding

Ethanolamine at room temperature.

Another method, in which the oil is degummed with a liquid phase, is described in WO 2009/068274 of

Grace / Desmet has been described.

Due to the increasing use of vegetable oils for

Production of raw materials for the chemical industry and the resulting demands for a low

Phosphorus content and a low phosphorus content of these oils, there is a growing demand for even more efficient method for phosphorus removal from crude oils. However, the prior art methods show that the effect of these methods is limited. Thus, in some cases, despite upstream Wasserentschleimung only achieved a reduction to more than 10 ppm of phosphorus in the oil. A big

Dependence also depends on the type of oil. It should also be remembered that crude oils of the same kind Diverge greatly with regard to the phosphorus content, depending on the plant variety, the growing conditions, the harvest and storage conditions and the type of oil production.

There has therefore been a need for a method of reducing the phosphorus content in triglyceride-containing compositions, particularly crude vegetable oils, which can easily achieve a very large reduction in phosphorus content and, moreover, can be used on a large scale.

The inventors of the present application have therefore set themselves the task of developing such a method, which also has a reduction of the phosphorus content also of

Crude oils with a very high phosphorus content (for example

Waste oils and pomace oils) in a simple manner, so that these without further processing for

Biodiesel production can be used. Furthermore, the inventors of the present application, the task of providing a method that is not only suitable for the preparation of crude vegetable oils, but can also be applied to other phosphorus-containing triglyceride compositions, in particular raw biodiesel.

To solve this problem, the inventors of

present application, a method for the removal of

Phosphorus-containing compounds from triglyceride-containing

Compositions comprising the following steps: a) contacting the triglyceride-containing

Composition comprising at least one substance selected from organic acids, phosphoric acid, Ethanolamine and solid adsorbents based on clay minerals, bleaching earths, aluminosilicates or

silicates; b) adding H20 to the composition according to step a); c) separating the aqueous phase from the triglyceride-containing composition;

Contacting the triglyceride-containing composition of step c) with at least one substance selected from organic acids, phosphoric acid, ethanolamine and solid adsorbents based on clay minerals, bleaching earths, aluminosilicates or silicates; e) addition of H 2 O to the composition according to step d); f) separating the aqueous phase from the triglyceride-containing composition;

By the method according to the invention, the phosphorus content of crude vegetable oils and other triglyceride-containing

Not only can compositions be reduced to meet the current 4 ppm upper limit required by EU standard EN 14214; By the method according to the invention much lower residual contents of phosphorus can be achieved, so that even with a further reduction of the

Phosphorus content in biodiesel these values can still be met. The term "phosphorus-containing compound" is understood in the context of any compound which contains at least one phosphorus atom, in particular hydratable and non-hydratable phospholipids and phosphoglycosides.

For the purposes of the present invention, the term "triglyceride-containing composition" means any composition which comprises at least one triglyceride (according to IUPAC:

triacylglycerol; the terms "triglyceride" and

"Triacylglycerol" are used interchangeably in the context of the present application) contains in particular biodiesel

Vegetable oil base and its precursors.

The term "biodiesel precursor" as used in the context of

The present invention refers to any mixtures comprising mono and / or di-glycerides of fatty acids. For example, such mixtures can one

Content of at least 30 wt .-%, preferably of at least 60 wt .-%, preferably of at least 85 wt .-%, in particular of at least 90 wt .-% of mono- or di-glycerides, each based on the total weight of the organic Have components of the mixture. Additionally, mixtures referred to as "biodiesel precursors" may optionally include fatty acid alkyl esters or fats. The term "fat" in the context of the present invention may refer to any mixture comprising triglycerides. As a fat, both mixtures with solid

Consistency, semi-solid consistency or liquid consistency at room temperature. In common usage, fats that are liquid at room temperature are often referred to as oils. It should be expressly understood that the term "fats" in the context of the present invention also includes any oils, such as the fats, which according to The general language traditions are referred to below as soybean oils, rapeseed oils, etc. The selection of a fat or a mixture of fats may be made in accordance with the general knowledge of one skilled in the art. Fats of different origin and composition are listed for example in the "textbook of food chemistry", Berlin, 2001, 5th edition, ISBN 3-540- 41096-1, by Belitz, Grosch, Schieberle.

Expressly mentioned is that as fat, however, too

Contaminated or waste products derived fats, such as frying oils, come into consideration. According to a preferred embodiment, the fat is a fat or oil having a lecithin content of less than 10% by weight, in particular less than 5% by weight, more preferably less than 10 ppm, in particular less than 5 ppm , According to one embodiment, degummed and / or deodorized fats or oils are also preferred

Biodiesel (precursors) having the above lecithin contents. In a further preferred embodiment, the oils and / or fats are considered to be difficult to degummable due to their high content of non-hydratable phospholipids. As an example, an oil is listed, which can still have a content of P up to 200 ppm after pre-degumming with water.

More preferably, the process according to the present invention is based on triglyceride-containing compositions

used, selected from the group consisting of soybean oil, rapeseed oil, sunflower oil, linseed oil, jatropha oil, canola oil,

Cottonseed oil, pumpkin seed oil, coconut oil, rice germ oil,

Peanut oil, corn oil, olive kernel oil, jojoba oil, almond oil,

Palm oil and its mixtures. Other oils used in the process can be used in the present invention are oils that can be obtained from algae.

Likewise preferred is the use of triglyceride-containing compositions, in particular oils, as above

which have already been subjected to pre-degumming (for example using citric acid, phosphoric acid or water).

In particular, the process according to the invention is generally particularly suitable for triglyceride-containing compositions having a very high phosphorus content, in particular vegetable oils having a phosphorus content of more than 450 ppm, more than 550 ppm and more than 650 ppm. Even with these oils is achieved by application of the method according to the invention a reduction of the phosphorus content below the limit according to the EU standard EN 14214.

The term "bringing into contact" means any kind of contacting which is known to the person skilled in the art as suitable for the purpose according to the invention Preferably, the triglyceride-containing composition is mixed with the substance by stirring In the embodiment, the mixture is stirred for a period of 1 minute to 24 hours, more preferably 5 minutes to 12 hours, more preferably 15 minutes to 5 hours, and most preferably 30 minutes to 2 hours

Water bath kept at a certain constant temperature. For details of the large-scale implementation of a degumming process, see "Practical Guide to

Vegetable Oil Processing ", Chapter 3 - Crude Oil De-gum and Acid Pre-treatment, AOCS Press, pp 33 (2008). The addition of H 2 O according to steps b) and e) can be carried out in any manner known to the person skilled in the art as suitable for the purpose according to the invention. In a preferred

In the embodiment according to steps a) and d) H20 is added in an amount of from 0.1 to 15% by weight (based on the amount of the triglyceride-containing composition), preferably from 0.5 to 10% by weight. %, more preferably from 1 to 7 wt%, and most preferably from 2 to 5 wt%. During the addition, the composition is in a

preferred execution form continuously stirred. In a preferred embodiment, the H20 added remains in the composition for a period of from 1 minute to 12 hours, preferably from 5 minutes to 5 hours, more preferably from 10 minutes to 2 hours, and most preferably from 30 minutes to 1 hour. In a particularly preferred

In the embodiment, the composition is stirred continuously.

The separation of the aqueous phase from the composition according to steps c) and f) can be carried out in any manner known to those skilled in the art as suitable for the purpose according to the invention. Preferably, the separation of the aqueous phase by centrifugation is preferably carried out at 1000 to 5000 rpm, more preferably at 3000 to 4500 rpm and most preferably from 3500 to 4000 rpm, preferably for a period of 1 minute to 30 minutes preferably from 5 minutes to 15 minutes.

In a particularly preferred embodiment, contacting according to steps a) and / or d) is carried out at a temperature of from 10 to 85 ° C., more preferably from 15 to 75 ° C., particularly preferably from 20 to 60 ° C, especially

preferably from 25 to 50 ° C and most preferably from 35 to 45 ° C performed. In a further particularly preferred embodiment, the addition of H 2 O in accordance with

Steps b) and / or e) at a temperature of 10 to 85 ° C, more preferably from 15 to 75 ° C, particularly preferably from 20 to 60 ° C, more preferably from 25 to 50 ° C and most preferably from 35 up to 45 ° C performed. In a likewise preferred embodiment, the process according to the present invention according to steps a) to f) at a temperature of 10 to 85 ° C, more preferably from 15 to 75 ° C, particularly preferably from 20 to 60 ° C, more preferably from 25 to 50 ° C, and most preferably from 35 to 45 ° C.

The temperature is preferably carried out in a water bath.

Also preferably, the addition of H 2 O according to steps b) and e) is already at a temperature of 10 to 85 ° C, more preferably 15 to 75 ° C, particularly preferably 20 to 60 ° C, particularly preferably 25 to 50 ° C, and most preferably preheated from 35 to 45 ° C. Furthermore, it is possible in the context of the present invention that all steps a) to f) at different

Temperatures are carried out.

In a further preferred embodiment of the present invention, the organic acid is selected from the group consisting of malic acid, tartaric acid, citric acid,

Lactic acid, formic acid, oxalic acid, malonic acid and mixtures thereof. Also preferred is the use of

Phosphoric acid and mixtures of all the above

Acids. Preferred concentrations of the organic and / or phosphoric acid are from 0.01 to 5% by weight (based on the weight of the triglyceride-containing composition), preferably from 0.05% to 5%, more preferably from 0.1% to 3%, and most preferably from 0.2% to 2%, by weight.

In a further preferred embodiment of the present invention, the solid adsorbent is selected from the group consisting of aluminosilicates, aluminum oxides,

Alumina hydrates, silica gels, clay minerals, bleaching earths and mixtures thereof.

In the context of the method according to the invention can

Combination with the extractant Adsorbents are used on the basis of silica gels, as they are

for example, by the company Grace in Worms under the

Trade name Trisyl® are sold. These can be one

Have water content of up to 60%. The use and production of such adsorbents are described in the patent EP 0185182 Bl.

As solid adsorbents but can also natural

Clay minerals are used. It can be about

Attapulgites, sepiolites or smectite clays, such as

Montmorillonite, beidellite, hectorite and saponite act. In addition, kerolithaltige clays can be used. Substituting the previously mentioned clays without additional

Treatment with acid only in a dried and ground state, so it is often called by so-called

Natural bleaching earth. A special case of such natural bleaching earths are porous clays consisting of mixtures of smectite clays and silica gel. Such mixtures come

of course, and their use for oil treatment is, for example, in the patent 'Oberflächenreiche Rohtone zur Preparation of bleaching earths and activation processes of these clays', WO 2006/131136, K. Schurz, Süd-Chemie AG.

However, the preceding clays are commonly used for oil treatment in the form of so-called bleaching earth, d. H. These clays can be loaded with acids, which is then referred to as a so-called 'Surface Modified Bleaching Earth' (SMBE). In addition, it is possible to cook according to the prior art, such clays with acid and, for example, from montmorillonite a high-digestion bleaching earth

manufacture. The manufacture and use of such

Bleaching earths are described, for example, in the following references: Practical Guide to Vegetable Oil Processing, M.K. Gupta, Chapter 5 Bleaching, pp 101, AOCS Press (2008);

Bleaching of fats and oils, Introduction, W. Zschau, pp 505, European Journal of Lipid Science and Technology (2001);

Bleaching of fats and oils, Chemical and physical base of whitening, W. Zschau, pp 509, European Journal of Lipid

Science and Technology (2001); What is bleaching earth ?, W. Zschau, pp 506, Fette Seifen Anstrichmittel (1985). In the process according to the invention can be used as adsorbents and aluminum-oxygen compounds, such as

Alumina hydrate, boehmite and different

Aluminum oxides, such as. B., ß and γ-alumina,

be used. The composition comprises an aluminosilicate having a

Weight fraction S1O ₂ of greater than 0.3, preferably greater than 0.35, particularly preferably greater than 0.4, based on the sum of the weight fractions of Si0 ₂ and A1 ₂ 0 ₃ on. The aluminosilicate preferably has, moreover, a S1O ₂ - weight content of less than 0.8, preferably less than 0.7, more preferably less than 0, 65, based on the total weight percent of Si0 ₂ and A1 ₂ 0 _3. For the purposes of the present invention, the aluminosilicate has a specific surface area of more than 350 m ² / g, preferably more than 400 m ² / g, particularly preferably more than 450 m ² / g. Particular preference is given to aluminosilicates having a specific surface area of from 355 m ² / g to 650 m ² / g, more preferably from 365 m ² / g to 600 m ² / g, more preferably from 400 m ² / g to 575 m ² / g, more preferably from 455 m ² / g to 550 m ² / g. The specific surface area is determined by the BET method.

According to another preferred embodiment, the aluminosilicate preferably has a pore volume of from 0.5 ml / g to 1.4 ml / g, preferably a pore volume of from 0.55 ml / g to 1.3 ml / g, more preferably 0, 6 ml / g to 1.2 ml / g, more preferably from 0.6 ml / g to 0.99 ml / g, further more preferably from 0.6 ml / g to 0.95 ml / g, and most preferably from 0.6 ml / g to 0.90 ml / g. The pore volume is calculated as the cumulative pore volume according to BJH (I.P. Barret, L.G.

Joiner, P.P. Haienda, J. Am. Chem. Soc. 73, 1991, 373) for pores having a diameter of 1.7 to 300 nm.

On the one hand, the high specific surface area and the high pore volume make it possible to achieve a high adsorption capacity for the triglyceride-containing composition

contained impurities such as phospholipids and metal ions and a rapid kinetics of adsorption, so that the method is particularly suitable for industrial application.

According to a preferred embodiment, the form comprises

Alumosilicate a proportion of other metals of less than 5 wt .-%, preferably less than 2 wt .-%, more preferably less than 1 wt .-%, particularly preferably less than 0.5 wt .-%. It is particularly preferred that the at least one aluminosilicate has a content of Fe ₂ O 3 of at most 0.2% by weight, more preferably of at most 0.1% by weight, more preferably of at most 0.05% by weight and on most preferably of at most 0.02% by weight. Further, it is particularly preferred that the at least one aluminosilicate has a content of Na ₂ O of at most 0.05 wt .-%, more preferably of at most 0.01 wt .-%, more preferably of at most 0.008 wt .-% and most preferably of at most 0.005 wt .-% has.

Finally, it is preferable that the aluminosilicate has a content of C of at most 0.5% by weight, more preferably

at most 0.4 wt%, more preferably at most 0.3 wt%, and most preferably at most 0.2 wt%. According to another preferred embodiment, this is

Aluminosilicate a synthetic aluminosilicate.

In the context of the present invention, it is possible that all of the embodiments described in more detail above are also combined with one another and it is also possible within the meaning of the present invention that in the case of several in the aluminosilicate-containing

Alumosilicates contained in this composition are of the same or different kind and are, for example, in their weight ratio of S1O ₂ : Al ₂ O ₃ , the specific surface BET and / or the cumulative pore volume to BJH and / or other parameters differ as long as at least one of the aluminosilicates contained a weight fraction of S1O ₂ of greater than 0.3 on the sum of

Parts by weight of S1O ₂ and AI ₂ O ₃ has.

Particularly preferred aluminosilicate-containing compositions comprise at least one aluminosilicate having a weight fraction of SiO ₂ of greater than 0.3 based on the sum of

Parts by weight of S1O ₂ and Al ₂ O ₃ , a specific

BET surface area of more than 350 m ² / g and a

cumulative pore volume after BJH of more than 0.7 ml / g for pores between 1.7 and 300 nm, preferably greater than 0.8 ml / g, particularly preferably greater than 0.9 ml / g. Particularly preferred aluminosilicate-containing compositions comprise at least one aluminosilicate having a weight fraction of SiO ₂ of greater than 0.3 based on the sum of

Parts by weight of S1O ₂ and Al ₂ O ₃ , a water content of 5, 0 to 8.0 wt .-%, a BET surface area of 350 to 600 m ² / g, a cumulative pore volume to BJH of 0.6 to 1, 0 cm ³ / g for pores having a diameter of 1.7 to 300 nm and an average pore diameter of 6.0 to 10.5 nm, and a C content of 0.1 to 0.3 wt .-%, a Fe20 ₃ content of 0.05 to 0.01 wt .-% and a Na ₂ 0 content of 0.01 to 0.001 wt .-%. Particularly preferred are aluminosilicate-containing

Compositions comprising at least one aluminosilicate having a weight fraction of S1O ₂ of greater than 0.3 based on the sum of the proportions by weight of S1O ₂ and Al ₂ O ₃ , a

Water content of 6.0 to 8.0 wt .-%, a BET surface area of 450 to 570 m ² / g, a cumulative pore volume to BJH of 0.75 to 0.95 cm ³ / g for pores having a diameter of 1.7 to 300 nm and an average pore diameter of 7.2 to 7.9 nm, and a C content of 0.1 to 0.3 wt .-%, a Fe ₂ Ü ₃ content of 0.05 to 0.01 wt .-% and a Na ₂ 0 content of 0.01 to 0.001 wt .-%.

The aluminosilicate according to the present invention can be prepared, for example, by using organic

Aluminum compounds hydrolyzed under acidic conditions and then together with silica or

Silica compounds are aged under hydrothermal conditions. Suitable aluminum compounds are

for example, aluminum alcoholates,

Aluminum hydroxyalcoholates, aluminum acetylacetonates,

Aluminum alkyl chlorides or aluminum carboxylates. A suitable method is described for example in DE 03839580 and US 6,245,310 Bl. This procedure is

particularly favorable, because this can achieve very high specific surface areas and porosities.

In order to obtain particularly pure aluminosilicates, hydrolyzable ones can also be used instead of silica

Organosilicon compounds are used, wherein the

Hydrolysis of organosilicon compounds and the

hydrolyzable aluminum compounds is carried out together. Such a method is described for example in EP 0 931 017 Bl.

Particular preference is given to using aluminosilicates which contain only S1O ₂ and Al ₂ O ₃ as constituents. In this case, those are preferred which have a weight ratio of Al ₂ O ₃ to S1O _{2 of} at least 0.3 and at most 0.7, preferably at least 0.35 and a maximum of 0.65. The proportion of further metals, calculated as the most stable oxide, is preferably less than 5% by weight, more preferably less than 3% by weight, more preferably less than 2% by weight and most preferably less than 1% by weight. selected.

As adsorbents, which are used in combination with the complexing agents according to the inventive method, any mixtures of the previously mentioned

Adsorbents are used. The adsorbents used in the invention can be provided for example in the form of a powder. A composition in the form of a powder is suitable, for example, when the adsorbent is stirred into the vegetable oil, that is in the form of a suspension. The particle size of the powder is adjusted in the sense of the invention such that the adsorbent is purified from the purified material within a suitable period of time without difficulty by a suitable method, such as filtration

Separate vegetable oil. If a powder is used, which is suspended in the crude vegetable oil, the

Dry sieve residue of the adsorbent on a sieve with a mesh size of 63 μπι preferably more than 25 wt .-% and is preferably in a range of 30 to 50 wt .-%. The Trockensiebrückstand on a sieve with a mesh size of 25 μπι is preferably more than 80 wt .-% and is preferably in a range of 85 to 88 wt .-%. Furthermore, the dry residue on a sieve with a mesh size of 45 μπι preferably more than 35 wt .-%, more preferably more than 45 wt .-%. In particular, for an application of the adsorbent in the form of a column packing but also larger particle sizes are suitable. For this purpose, the adsorbent is preferably used in the form of granules. For the preparation of column packings, a granulate is preferably used which has a particle size of more than 0.1 mm. Preferably, the granules have a particle size in the range of 0.2 to 5 mm, particularly preferably 0.3 to 2 mm. The grain size can be adjusted, for example, by sieving.

The granules can be prepared by conventional methods, for example, by applying a finely ground adsorbent with a granulating agent, for example water, and then granulated in a conventional granulating in a mechanically generated fluidized bed. However, other methods can be used to control the granules

manufacture. Thus, the powdered adsorbent

be formed for example by compaction to a granulate.

Preferred concentrations of the adsorbent are from 0.05 to 6 wt .-% (based on the weight of the triglyceride-containing

Composition), preferably 0.1 to 5 wt .-%, more preferably from 0.15 to 3 wt .-% and most preferably from 0.2 to 2 wt. -%.

In a further preferred embodiment of the present invention, ethanolamine is selected from the group consisting of monoethanolamine, diethanolamine, triethanolamine and mixtures thereof, with monoethanolamine being particularly preferred. Preferred concentrations of the ethanolamine are from 0.001 to 5% by weight (based on the weight of the triglycerides-containing Composition), preferably 0.005 to 5 wt .-%, further

preferably from 0.01 to 3% by weight, and most preferably from 0.1 to 2% by weight.

In a further preferred embodiment of the invention

The process of the invention, the step a) and / or d) is carried out at atmospheric pressure or under vacuum. Likewise preferred is that step b) and / or e) in

Atmospheric pressure or under vacuum is performed.

Finally, it is possible that all steps a) to f) are carried out at atmospheric pressure or under vacuum.

Furthermore, it is within the scope of the present invention possible to repeat steps d) to f), i. re-contacting the triglyceride-containing ones

Composition comprising at least one substance selected from organic acids, phosphoric acid, ethanolamine and solid adsorbents based on clay minerals, bleaching earths, aluminosilicates or silicates or mixtures thereof

and subsequent addition of H 2 O to the composition followed by separation of the aqueous phase from the triglyceride-containing composition.

In the context of the present invention, all

Embodiments, as described here, freely combined with each other. Especially preferred

For example, embodiments according to the present invention

A) a process for the removal of phosphorus-containing

Compounds of triglyceride-containing compositions comprising the following steps Contacting the triglyceride-containing composition with at least one ethanolamine, preferably monoethanolamine;

Adding H 2 O to the composition according to step a);

Separating the aqueous phase from the triglyceride-containing composition; d) contacting the triglyceride-containing

Composition of step c) with at least one organic acid, preferably citric acid; e) addition of H 2 O to the composition according to step d); f) separating the aqueous phase from the triglyceride-containing composition.

In addition, particularly preferred is when the process is carried out at a temperature of 35 to 45 ° C, preferably at 40 ° C. Furthermore, it is preferred if the organic acid is used in a concentration of 0.1 to 0.5 wt .-%, preferably 0.2 wt .-%, and it is particularly preferably a 20% citric acid. Also preferred, when the ethanolamine is added in the form of monoethanolamine, preferably in a concentration of 0.1 to 1 wt .-%, particularly preferably 0.5 wt .-%. B) a process for the removal of phosphorus-containing

Compounds of triglyceride-containing compositions comprising the following steps: a) contacting the triglyceride-containing

Composition of step c) with at least one organic acid, preferably citric acid; b) adding H20 to the composition according to step a); c) separating the aqueous phase from the triglyceride-containing composition; d) contacting the triglyceride-containing

Composition with at least one ethanolamine, preferably monoethanolamine; e) addition of H 2 O to the composition according to step d); f) separating the aqueous phase from the triglyceride-containing composition.

In addition, particularly preferred is when the process is carried out at a temperature of 35 to 45 ° C, preferably at 40 ° C. Furthermore, it is preferred if the organic acid in an absolute concentration of 0.1 to 2 wt .-%, preferably 1 wt .-% is used and especially here

preferably a 50% strength citric acid solution is used. Also preferred, when the ethanolamine is added in the form of monoethanolamine, preferably in one Concentration of 0.1 to 1 wt .-%, particularly preferably 0.5 wt. -%.

C) a process for the removal of phosphorus-containing

Composition with at least one ethanolamine, preferably monoethanolamine; b) adding H20 to the composition according to step a); c) separating the aqueous phase from the triglyceride-containing composition; d) contacting the triglyceride-containing

Composition from step c) with at least one adsorbent, preferably an aluminosilicate; e) addition of H 2 O to the composition according to step d); f) separating the aqueous phase from the triglyceride-containing composition.

In addition, particularly preferred is when the process is carried out at a temperature of 35 to 45 ° C, preferably at 40 ° C. In addition, it is preferred if the ethanolamine is added in the form of monoethanolamine, preferably in a concentration of 0.1 to 1 wt .-%, particularly preferably 0.5 Wt .-%. Also preferred is when the adsorbent in a concentration of 0.1 to 2 wt .-%, preferably 1 wt .-%

is added.

D) a process for the removal of phosphorus-containing

Composition from step c) with at least one adsorbent, preferably an aluminosilicate; b) adding H20 to the composition according to step a); c) separating the aqueous phase from the triglyceride-containing composition; d) contacting the triglyceride-containing

Composition according to step c) with at least one ethanolamine, preferably monoethanolamine; e) addition of H 2 O to the composition according to step d); f) separating the aqueous phase from the triglyceride-containing composition.

In addition, it is particularly preferable that the process is carried out at a temperature of from 35 to 45 ° C, preferably at 40 ° C. In addition, it is preferable if the

Ethanolamine in the form of monoethanolamine is added, preferably in a concentration of 0.1 to 1 wt .-%, more preferably 0.5% by weight. It is likewise preferred if the adsorbent is added in a concentration of 0.1 to 2% by weight, preferably 1% by weight.

Measurement methods and procedures Pre-degumming a) Pre-degumming with water

The crude oil is heated to 40 ° C. with stirring. Under

Maintaining this temperature, calculated on the amount of crude oil, 5% (w / w) dist. Water was added dropwise and stirred for 1 h. Subsequently, the resulting precipitate at room temperature at 4000 rev / min for 15 min

centrifuged. The supernatant oil is the pre-degummed oil for subsequent investigations. b) pre-degumming with citric acid

The crude oil is heated to 40 ° C. with stirring. Under

Maintaining this temperature, calculated on the amount of crude oil, 5% (w / w) of 10% aqueous citric acid solution was added dropwise and stirred for 1 h. Subsequently, the

centrifuged at room temperature at 4000 rev / min for 15 min. The supernatant oil is the citric acid pre-degummed oil for subsequent tests. Degumming with organic acids, phosphoric acid, solid adsorbent or ethanolamine

1. Degumming stage

20 g of the pre-degummed oil (pre-degumming a or b) are placed in a small beaker with the appropriate amount of organic acid, phosphoric acid, solid adsorbent or Ethanolamine added. The mixture is stirred in a 40 ° C tempered water bath. After 60 minutes, this mixture 2% dist. Water (based on the amount pre-degummed oils) is added dropwise and stirred for a further 30 min in a water bath at 40 ° C. Subsequently, the oil is separated from the precipitate and the water phase by centrifuging at 4000 rpm for a period of 15 minutes. The thus purified oil is fed to the metal and P-analysis or can be subjected to a second degumming stage.

2. Degumming stage

The oil obtained from the 1st degumming stage is reused and carried out analogously to the 1st stage

subjected.

methods

The physical properties of the adsorbents were determined by the following methods:

BET surface area / pore volume after BJH and BET:

The surface and the pore volume were combined with a

fully automatic nitrogen porosimeter of the company

Micromeritics type ASAP 2010 determined.

The sample is cooled in a high vacuum to the temperature of liquid nitrogen. Subsequently, it becomes continuous

Nitrogen dosed into the sample chambers. By detecting the adsorbed amount of gas as a function of pressure, an adsorption isotherm is determined at a constant temperature. In a pressure equalization, the analysis gas is gradually

removed and recorded a desorption isotherm.

To determine the specific surface area and the porosity according to the BET theory, the data according to DIN 66131

evaluated.

The pore volume is also determined from the measurement data using the BJH method (I.P. Barret, L.G. Joiner, P.P.

Haienda, J. Am. Chem. Soc. 73, 1991, 373). This procedure also takes into account effects of capillary condensation. Pore volumes of certain volume size ranges are determined by summing up incremental pore volumes obtained from the evaluation of the BJH adsorption isotherm. The total pore volume by BJH method refers to pores with a diameter of 1.7 to 300 nm.

Water content:

The water content of the products at 105 ° C is determined using the method DIN / ISO-787/2.

Loss on ignition:

In a heat-treated weighed porcelain crucible with lid approx. 1 g of dried sample is weighed to the nearest 0.1 mg and annealed for 2 hours at 1000 ° C in a muffle furnace. Thereafter, the crucible is cooled in a desiccator and weighed.

Determination of dry residue

About 50 g of the air-dry clay material to be examined are placed on a sieve of the corresponding mesh size weighed. The sieve is connected to a vacuum cleaner, which passes through a sieve which circulates under the sieve bottom all portions which are finer than the sieve

sucks. The strainer is covered with a plastic lid and the vacuum cleaner is switched on. After 5 minutes, the vacuum cleaner is switched off and the amount of remaining on the screen, coarser portions by differential weighing

determined.

Determination of the bulk density A measuring cylinder cut off at the 100 ml mark is weighed. Then, the sample to be examined is filled by means of a Pulvertrichters so in a train in the measuring cylinder that above the conclusion of the

Measuring cylinder forms a Schüttkegel. The pouring cone is made with the help of a ruler, which over the opening of the

Measuring cylinder is guided, stripped and ge filled

Weigh the measuring cylinder again. The difference corresponds to the bulk density.

Description of Adsorbents In the following tables are the chemical

Compositions and physical properties of

Adsorbents listed, which are used in the following examples. Trisyl® 300 is a commercially available silica gel from Grace in Worms. Table la: Chemical composition of the adsorbents Adsorbent aluminosilicate 1

AI2O3 + Si0 ₂ -

75

Content (% by weight)

LOI (wt%) 25

AI2O3: Si0 ₂

60: 40

(Wt .-%)

C (wt%) 0.2

Fe ₂ 0 ₃ (wt%) 0, 02

Na ₂ O (wt%) 0, 005

Adsorbent bleaching earth 1

Si0 ₂ (%) 70, 1

AI2O3 (%) 10, 0

Fe ₂ 0 ₃ (%) 3, 0

CaO (%) 1.5

MgO (%) 4.3

Na ₂ O (%) 0.3

K ₂ 0 (%) 1.4

Loss on ignition (%) 8, 6

Table lb Physical properties of the adsorbents

TriSyl®

BleichAlumo-

adsorbent

earth 1 silicate 1

300

Bulk weight (g / 1) 350 250-450 354

Mean particle size (d50)

n. d. 50 15

[Μπι]

Dry sieve residue at 45 μπι

49 n. d. n. d.

(%)

Dry sieve residue to 63 μπι

35 n. d. n. d.

(%)

Water content (wt .-%) Max. 15 7.8 57

BET surface area (m ² / g) 225 512 669

Cumulative pore volume (BJH)

for pore diameters 1.7-300 0, 825 0, 97 n. d. nm (cm ³ / g)

average

16, 4, 7.2 n. d. Pore diameter (BJH) (nm) Examples and figures

It is pointed out that in the following

Examples and figures have a purely illustrative character and only the clarification of

method of the invention, but in no way limit the present invention.

Show it

Fig. 1: The concentrations of Ca, Mg and P after

Implementation of the method according to Example 1 on the basis of pre-degummed soybean oil

(Pre-degumming with water and citric acid)

Fig. 2: The concentrations of Ca, Mg and P after

Implementation of the method according to Example 2 on the basis of pre-degummed soybean oil (water pre-degumming) and after carrying out in each case only one treatment step (here only P content)

example 1

Comparison of the Ca, Mg and P final contents in pre-degumming with water or citric acid and different order of after-treatment with citric acid and ethanolamine.

Example 1.1

It is a raw soybean oil pre-degummed with water. This pre-degummed oil (SO 1.1a) is treated with 0.5% ethanolamine (SO 1.1b) with 0.5% ethanolamine in the 1st stage (corresponds to step a) of the process according to the invention) and treated with 2% aqueous citric acid (50%) in the 2nd stage (corresponding to step b) of the process according to the invention) (SO 1.1 c). treated with 2% aqueous citric acid (50%) in the 1st stage and treated with 0.5% ethanolamine in the 2nd stage SO 1. ld). treated with 2% aqueous citric acid (50%) (SOI.le). Example 1.2

The raw soybean oil from Example 1.1a is pre-degummed with citric acid (SO 1.2a). This pre-degummed oil is treated with 0.5% ethanolamine (SO 1.2b) or with 2% 50% citric acid (SO 1.2c)

Stolmär Scheele & Partner - 37/45 - 13th October 2011

34973-SOUTH P-WO

Results for Example 1

Table 1

These results show that a combination of ethanolamine with citric acid provides a significant improvement in results. Ethanolamine can be in very low

Dosage can be used. A sole degumming with citric acid or ethanolamine is not enough.

Example 2

Combination of ethanolamine with adsorbents Example 2.1

A raw soybean oil is pre-degummed with water. This pre-degummed oil is treated with 0.5% ethanolamine as the first step. The oil obtained from this is further treated in a second stage with 1% adsorbent. The adsorbents used are a bleaching earth, an aluminosilicate and a silica gel (see description of the adsorbents). The silica gel is the product Trisyl® 300 from Grace, Worms.

Example 2.2

The experiment is carried out analogously to Example 2.1, only the order of degumming steps is exchanged, ie 1st stage 1% adsorbent, 2nd stage 0.5% ethanolamine. Table 2:

A combination of aluminosilicate 1 with ethanolamine removes Ca, Mg and P almost completely, whereas the

Single uses have a significantly higher final content of P. Although this is an additional step performed, but this can significantly reduce the dosages used. This is also evident in the combination of ethanolamine with other adsorbents. Used

Ethanolamine in the first step, the final results are even more advantageous. For comparison, if the soybean oil is treated conventionally, i. e.g. a pre-degumming with 10% water at 80 ° C for 20 min, after separation of the oil phase, an addition of 0.2% of a 20% citric acid and reaction time of 20 min at 80 ° C. In this approach, the conventional

Adsorbent (eg bleaching earth 1, Trisyl® 300) supplied and treated at 110 ° C for 30 min and 30 mbar. Even with a 2% Adsorbensdosage used here was still a P content of 38 ppm, Ca content of 18 ppm and Mg content of 12 ppm for Trisyl ^® 300 and 66 ppm (P), 34 ppm (Ca), 23 ppm (Mg) for bleaching earth 1 was obtained. The necessary specification of below 4 ppm P and below 10 ppm Ca and Mg could not be achieved in this way.

In contrast, with the method according to the invention, these values can be achieved with significantly lower dosages of adsorbents or

Complexing agents can be achieved.

Claims

claims

1. Process for the removal of phosphorus-containing

Composition comprising at least one substance selected from organic acids, phosphoric acid, ethanolamine and solid adsorbents based on clay minerals, bleaching earths, aluminosilicates, silica gels,

Precipitated silicas or silicates; b) adding H20 to the composition according to step a); c) separating the aqueous phase from the triglyceride-containing composition; d) contacting the triglyceride-containing

Composition from step c) with at least one substance selected from organic acids,

Phosphoric acid, ethanolamine and solid adsorbents based on clay minerals, bleaching earths, aluminosilicates, silica gels, precipitated silicas or silicates; e) addition of H 2 O to the composition according to step d); f) separating the aqueous phase from the triglyceride-containing composition.

2. The method according to claim 1, wherein the step a) and / or d) is carried out at a temperature of 20 to 60 ° C.

3. The method according to claim 2, wherein the step a) and / or d) is carried out at a temperature of 25 to 50 ° C.

4. The method according to any one of the preceding claims wherein the triglyceride-containing composition soybean oil, rapeseed oil,

Sunflower oil, palm oil; Jatropha oil, linseed oil, canola oil,

Cottonseed oil, pumpkin seed oil, coconut oil, rice germ oil,

Peanut oil, corn oil, olive kernel oil, jojoba oil, almond oil and / or algae oil.

5. The method according to any one of the preceding claims, wherein the organic acid is selected from the group consisting of malic acid, tartaric acid, citric acid, lactic acid,

Formic acid, oxalic acid, malonic acid and mixtures thereof.

6. The method according to any one of claims 1 to 4, wherein the solid adsorbent is selected from the group consisting of aluminosilicates, alumina, alumina hydrates,

Silica gel-based compositions, bleaching earths and mixtures thereof.

7. The method according to any one of claims 1 to 4, wherein

Ethanolamine is selected from the group consisting of monoethanolamine, diethanolamine, triethanolamine and their

Mixtures.

A process according to any one of claims 1 to 5, wherein the concentration of the organic acid or phosphoric acid is selected in the range of 0.01 to 5% by weight (based on the weight of the triglyceride-containing composition).

9. The method according to any one of claims 1 to 4 or 6, wherein the concentration of the adsorbent in the range of 0.1 to 5 wt. % (based on the weight of the triglyceride composition) is selected.

A process according to any one of claims 1 to 4 or 7, wherein the concentration of the ethanolamine is selected in the range of 0.01 to 3.0% by weight (based on the weight of the triglyceride composition).

11. The method according to any one of the preceding claims, wherein the step a) and / or d) is carried out at atmospheric pressure or under vacuum.

12. The method according to any one of the preceding claims, wherein the bringing into contact of the triglyceride-containing

Composition according to step a) is carried out with ethanolamine.

13. The method according to any one of the preceding claims, wherein the bringing into contact of the triglyceride-containing

Composition according to step d) is carried out with an organic acid, phosphoric acid or a solid adsorbent.