Esterification of carboxylic acids with olefins using a zeolitic material having a BEA-type frame- work structure

TECHNICAL FIELD

The present invention relates to a catalytic process for the preparation of an ester starting from a carboxylic acid and an alkene using a zeolitic material having a BEA-type framework structure as the catalyst.

INTRODUCTION

The synthesis of esters, such as fatty esters in the prior art is commonly carried out via the con- densation of fatty acids with alcohols in a homogeneously catalyzed process. For instance, a state of the art process for fatty esters involves direct esterification of fatty acids (C12 and C14) with alcohol/ trans-esterification of methyl esters with alcohol in a semi-batch process, the reac- tion being homogeneously catalyzed in the presence of acidic catalysts such as sulfuric acid. The disadvantages of said prior art process includes:

- Thermodynamic limitations since the reaction is equilibrium limited, hence high conversions can only be achieved by removing one of the products (either the ester or the water).

- Semi-batch process is necessary, since H ₂ 0 removal makes a continuous process difficult.

- Alcohols are expensive, having a relatively high price compared to olefins

- Feedstock (alcohol) loss since alcohols can form azeotropes with water being produced in the reaction, leading to loss of feedstock and expensive separation.

- Catalyst separation issues, due to the removal of the homogenous catalyst being challenging.

There is therefore the need for an improved process for the production of esters which over- comes the limitations of the prior art.

US 5,189,201 describes the preparation of a lower fatty acid ester such as ethyl acetate or ethyl acrylate by a process in which a lower fatty acid (i.e. having up to four carbon atoms) such as acetic acid or acrylic acid is reacted with a lower olefin such as ethylene by using as solid cata- lyst a heteropoly-acid or its salt (for instance Cesium phosphotungstate).

WO 2010/146156 A1 relates to an organotemplate-free synthetic process for the production of a zeolitic material (zeolite beta) having a BEA framework structure comprising Y0 ₂ and optionally comprising X ₂ 0 ₃ , wherein Y is a tetravalent element, and X is a trivalent element. WO

2010/146156 A1 further relates to the use of said zeolitic material in exhaust gas treatment, preferably in the treatment of industrial or automotive exhaust gas.

Olefins (alkenes) have lower prices than the corresponding alcohol, hence give access to a more cost effective process for the production of an ester. Furthermore, by employing a hetero- geneous catalyst in place of a homogeneous catalyst enables a simplified process avoiding the disadvantages of semi-batch processing. Nevertheless, there remains the need for the provision of an improved process, in particular with regard to the selectivity towards and the yield of the ester product. Furthermore, there remains a need for a process which may be run for prolonged periods, in particular in a continuous mode, while sustaining a high selectivity towards and achieving a high yield of the ester product.

DETAILED DESCRIPTION

It was therefore an object of the present invention to provide a process for the production of an ester which is economically advantageous and can be carried out with high yield and selectivity, particularly over extended reaction times. Thus, it has surprisingly been found that the esterifi- cation of carboxylic acids with alkenes can advantageously be carried out with a zeolitic materi- al having a BEA-framework structure as obtained from organotemplate-free synthesis as the catalyst.

Therefore, the present invention relates to a process for production of an ester comprising: (1) preparing a mixture (M1 ) comprising a carboxylic acid of formula (I) and an alkene of formula (II)

(2) feeding the mixture (M1) into a reactor containing a catalyst, said catalyst comprising a zeolitic material having a BEA-type framework structure;

(3) contacting the mixture (M1 ) with the catalyst in the reactor for reacting at least a portion of the mixture (M1 ) to an ester of formula (III)

(4) collecting a reacted mixture (M2) containing the ester of formula (III) from the reactor; wherein R and R’ are alkyl groups;

wherein R” is hydrogen or an alkyl group; wherein the zeolitic material having a BEA-type framework structure displays an X-ray diffrac tion pattern comprising at least the following reflections:

wherein 100% relates to the intensity of the maximum peak in the 20-45° 20 range of the X-ray powder diffraction pattern, and

wherein the BEA-type framework structure comprises YO ₂ and X ₂ O ₃ , wherein Y is a tetravalent element, and X is a trivalent element.

According to the zeolitic material having a BEA-type framework structure used in the inventive process, no particular restrictions apply relative to the method according to which the X-ray dif fraction is obtained for determining the diffraction angles and intensities of the reflections, pro- vided that the Cu K(alpha 1) radiation is used to this effect. According to the inventive process it is however preferred that the X-ray diffraction pattern is obtained as described in the experi- mental section for determining the diffraction angles and intensities of the reflections displayed by the zeolitic material having a BEA-type framework structure used in the inventive process

Preferably, R is an optionally branched and/or optionally substituted and/or optionally unsatu- rated alkyl group selected from the group consisting of optionally branched and/or optionally substituted and/or optionally unsaturated C1-C24 alkyl groups, more preferably C2-C22 alkyl groups, more preferably C4-C20 alkyl groups, more preferably C6-C18 alkyl groups, more pref- erably C8-C18 alkyl groups, more preferably C10-C16 alkyl groups, more preferably C12-C16 alkyl groups, more preferably C12-C14 alkyl groups, more preferably C12 or C14 alkyl groups, and more preferably C14 alkyl groups, wherein more preferably R is selected from the group consisting of optionally substituted methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, undecyl, dodecyl, tridecyl, tetradecyl, pentadecyl, and hexadecyl, more preferably from the group consisting of optionally substituted dodecyl, tridecyl, tetradecyl, pentadecyl, and hex- adecyl, more preferably from the group consisting of optionally substituted dodecyl, tetradecyl, and hexadecyl, wherein more preferably R is optionally substituted dodecyl or tetradecyl, pref- erably dodecyl or tetradecyl, and more preferably tetradecyl. The term“C ₁ -C ₂₄ alkyl” as used in the context of the present invention refers to an alkyl residue having from 1 to 24 carbon atoms in the chain. The alkyl residue may have, for example, 1 , 2, 3, 4, 5, or 6 carbon atoms in the chain (C ₁ -C ₆ alkyl) or 1 , 2, 3, or 4 carbon atoms in the chain (C ₁ -C ₄ alkyl).

The term "optionally substituted" as used in the context of the present invention is to be under- stood to include any suitable substituent conceivable for the skilled person to be comprised in the carboxylic acid of formula (I) and/or alkene of formula (II) which does not prevent the for- mation of the ester of formula (III) according to the present process.

Preferably, R’ is an optionally branched and/or optionally substituted and/or optionally unsatu- rated alkyl group selected from the group consisting of optionally branched and/or optionally substituted and/or optionally unsaturated C1-C6 alkyl groups, more preferably C1-C5 alkyl groups, more preferably C1-C4 alkyl groups, more preferably C1-C3 alkyl groups, more prefer- ably C1-C2 alkyl groups, and more preferably C1 alkyl groups, wherein more preferably R is selected from the group consisting of optionally substituted methyl, ethyl, propyl, butyl, pentyl, and hexyl, more preferably from the group consisting of optionally substituted methyl, ethyl, propyl, butyl, and pentyl, more preferably from the group consisting of optionally substituted methyl, ethyl, propyl, and butyl, more preferably from the group consisting of optionally substi- tuted methyl, ethyl, and propyl, wherein more preferably R is optionally substituted methyl or ethyl, preferably methyl.

Preferably, R” is hydrogen or an optionally branched and/or optionally substituted and/or op- tionally unsaturated alkyl group selected from the group consisting of optionally branched and/or optionally substituted and/or optionally unsaturated C1-C6 alkyl groups, more preferably C1-C5 alkyl groups, more preferably C1-C4 alkyl groups, more preferably C1-C3 alkyl groups, more preferably C1-C2 alkyl groups, and more preferably C1 alkyl groups, wherein more preferably R is hydrogen or an alkyl group selected from the group consisting of optionally substituted me- thyl, ethyl, propyl, butyl, pentyl, and hexyl, more preferably from the group consisting of option- ally substituted methyl, ethyl, propyl, butyl, and pentyl, more preferably from the group consist- ing of optionally substituted methyl, ethyl, propyl, and butyl, more preferably from the group consisting of optionally substituted methyl, ethyl, and propyl, wherein more preferably R is hy- drogen or optionally substituted methyl or ethyl, wherein more preferably R is hydrogen, methyl, or ethyl, wherein more preferably R is hydrogen.

As to the carboxylic acid of formula (I), it is preferred that the carboxylic acid of formula (I) is selected from the group consisting of optionally substituted formic acid, acetic acid, propionic acid, valeric acid, acrylic acid, methacrylic acid, and crotonic acid, wherein preferably the car- boxylic acid of formula (I) is optionally substituted acetic acid or acrylic acid.

As to the alkene of formula (II), it is preferred that the alkene of formula (II) is selected from the group consisting of optionally substituted ethylene, propylene, 1-butene, 2-butene, and isobu- tene, wherein more preferably the alkene of formula (II) is optionally substituted ethylene or propylene, preferably ethylene or propylene, and more preferably propylene. Preferably, the carboxylic acid of formula (I) is myristic acid and the alkene of formula (II) is propylene. It is alternatively preferred that the carboxylic acid of formula (I) is lauric acid and the alkene of formula (II) is propylene. It is alternatively preferred that the carboxylic acid of formula (I) is acetic acid and the alkene of formula (II) is ethylene. Alternatively, it is preferred that the carboxylic acid of formula (I) is acrylic acid and the alkene of formula (II) is ethylene.

While there are no specific restrictions, it is preferred that the alkene : carboxylic acid molar ratio of the alkene of formula (II) to the carboxylic acid of formula (I) in the mixture (M1 ) prepared in (1) and reacted in (3) is in the range of from 0.1 : 1 to 1 : 0.1 , preferably from 0.3 : 1 to 1 : 0.3, more preferably from 0.5 : 1 to 1 : 0.5, more preferably from 0.7 : 1 to 1 : 0.7, more preferably from 0.8 : 1 to 1 : 0.8, more preferably from 0.85 : 1 to 1 : 0.85, more preferably from 0.9 : 1 to 1 : 0.9, and more preferably from 0.95 : 1 to 1 : 0.95.

Preferably, the mixture (M1 ) prepared in (1 ) and reacted in (3) contains 50 wt.-% or less of wa- ter based on 100 wt.-% of the carboxylic acid of formula (I), preferably 20 wt.-% or less, more preferably 10 wt.-% or less, more preferably 5 wt.-% or less, more preferably 1 wt.-% or less, more preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more preferably 0.01 wt.-% or less, more preferably 0.005 wt.-% or less, more prefera- bly 0.001 wt.-% or less, more preferably 0.0005 wt.-% or less, and more preferably 0.0001 wt- % or less of water based on 100 wt.-% of the carboxylic acid of formula (I). Preferably, the mix- ture (M1) prepared in (1) and reacted in (3) comprises 50 mol% or less of an alcohol of formula

(IV)

based on 100 mol% of the carboxylic acid of formula (I), preferably 20 mol% or less, more pref- erably 10 mol% or less, more preferably 5 mol% or less, more preferably 1 mol% or less, more preferably 0.5 mol% or less, more preferably 0.1 mol% or less, more preferably 0.05 mol% or less, more preferably 0.01 mol% or less, more preferably 0.005 mol% or less, more preferably 0.001 mol% or less, more preferably 0.0005 mol% or less, and more preferably 0.0001 mol% or less of an alcohol of the formula (IV) based on 100 mol% of the carboxylic acid of formula (I). The mixture (M1) prepared in (1 ) and reacted in (3) preferably contains 50 wt.% or less of ele- ments and/or compounds other than the carboxylic acid of formula (I) and the alkene of formula (II) based on 100 wt.-% of the carboxylic acid of formula (I), preferably 20 wt.-% or less, more preferably 10 wt.-% or less, more preferably 5 wt.-% or less, more preferably 1 wt.-% or less, more preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more preferably 0.01 wt.-% or less, more preferably 0.005 wt.-% or less, more prefera- bly 0.001 wt.-% or less, more preferably 0.0005 wt.-% or less, and more preferably 0.0001 wt- % or less of elements and/or compounds other than the carboxylic acid of formula (I) and the alkene of formula (II) based on 100 wt.-% of the carboxylic acid of formula (I). Preferably, the mixture (M1 ) prepared in (1 ) and reacted in (3) consists of a mixture of the carboxylic acid of formula (I) and the alkene of formula (II).

As to steps (2) and (3) and the catalyst in (2) and (3), the catalyst in the reactor preferably con- tains 200 wt.% or less of elements and/or compounds other than the zeolitic material having a BEA-type framework structure based on 100 wt.-% of the zeolitic material having a BEA-type framework structure, preferably 100 wt.-% or less, more preferably 50 wt.-% or less, more pref- erably 20 wt.-% or less, more preferably 10 wt.-% or less, more preferably 5 wt.-% or less, more preferably 1 wt.-% or less, more preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more preferably 0.01 wt.-% or less, more preferably 0.005 wt.-% or less, more preferably 0.001 wt.-% or less, more preferably 0.0005 wt.-% or less, and more preferably 0.0001 wt.-% or less of elements and/or compounds other than the zeolitic ma- terial having a BEA-type framework structure based on 100 wt.-% of the zeolitic material having a BEA-type framework structure. Preferably, in (2) and (3) the zeolitic material having a BEA- type framework structure comprised in the catalyst is in the H-form.

Preferably, in (2) and (3) the zeolitic material having a BEA-type framework structure comprised in the catalyst contains 5 wt.-% or less of a metal AM calculated as the element and based on 100 wt.-% of YO ₂ contained in the framework structure of the zeolitic material having a BEA- type framework structure, preferably 1 wt.-% or less, more preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more preferably 0.01 wt.-% or less, more preferably 0.005 wt.-% or less, more preferably 0.001 wt.-% or less, more preferably 0.0005 wt.-% or less, and more preferably 0.0001 wt.-% or less of a metal AM calculated as the element and based on 100 wt.-% of YO ₂ contained in the framework structure of the zeolitic material having a BEA-type framework structure,

wherein the metal AM stands for Na, preferably for Na and K, more preferably for alkali metals, and more preferably for alkali and alkaline earth metals.

Preferably, in (2) and (3) the zeolitic material having a BEA-type framework structure comprised in the catalyst contains 5 wt.-% or less of a metal TM calculated as the element and based on 100 wt.-% of YO ₂ contained in the framework structure of the zeolitic material having a BEA- type framework structure, preferably 1 wt.-% or less, more preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more preferably 0.01 wt.-% or less, more preferably 0.005 wt.-% or less, more preferably 0.001 wt.-% or less, more preferably 0.0005 wt.-% or less, and more preferably 0.0001 wt.-% or less of a metal TM calculated as the element and based on 100 wt.-% of YO ₂ contained in the framework structure of the zeolitic material having a BEA-type framework structure,

wherein the metal TM stands for Pt, Pd, Rh, and Ir, and preferably stands for transition metal elements of groups 3-12.

In (2) and (3) the catalyst in the reactor preferably contains 5 wt.-% or less of a metal AM calcu- lated as the element and based on 100 wt.-% of the catalyst, preferably 1 wt.-% or less, more preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more preferably 0.01 wt.-% or less, more preferably 0.005 wt.-% or less, more preferably 0.001 wt.-% or less, more preferably 0.0005 wt.-% or less, and more preferably 0.0001 wt.-% or less of a metal AM calculated as the element and based on 100 wt.-% of the catalyst, wherein the metal AM stands for Na, preferably for Na and K, more preferably for alkali metals, and more preferably for alkali and alkaline earth metals. Preferably, in (2) and (3) the catalyst contained in the reactor contains 5 wt.-% or less of a metal TM calculated as the element and based on 100 wt.-% of the catalyst, preferably 1 wt.-% or less, more preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more preferably 0.01 wt.-% or less, more preferably 0.005 wt.-% or less, more preferably 0.001 wt.-% or less, more preferably 0.0005 wt.-% or less, and more preferably 0.0001 wt.-% or less of a metal TM calculated as the element and based on 100 wt.-% of the catalyst,

wherein the metal TM stands for Pt, Pd, Rh, and Ir, and preferably stands for transition metal elements of groups 3-12. Preferably, in (2) and (3) the zeolitic material having a BEA-type framework structure comprised in the catalyst contains 5 wt.% or less of phosphorous calculat- ed as the element and based on 100 wt.-% of Y0 ₂ contained in the framework structure of the zeolitic material having a BEA-type framework structure, preferably 1 wt.-% or less, more pref- erably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more preferably 0.01 wt.-% or less, more preferably 0.005 wt.-% or less, more preferably 0.001 wt.-% or less, more preferably 0.0005 wt.-% or less, and more preferably 0.0001 wt.-% or less of phosphorous calculated as the element and based on 100 wt.-% of YO ₂ contained in the framework structure of the zeolitic material having a BEA-type framework structure. In (2) and (3) the catalyst preferably contains 5 wt.% or less of phosphorous calculated as the element and based on 100 wt.-% of the catalyst, preferably 1 wt.-% or less, more preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more preferably 0.01 wt.-% or less, more preferably 0.005 wt.-% or less, more preferably 0.001 wt.-% or less, more preferably 0.0005 wt.-% or less, and more preferably 0.0001 wt.-% or less of a metal AM calculated as the element and based on 100 wt.-% of the catalyst.

While there are no specific restrictions, it is preferred that the contacting of the mixture (M1) with the catalyst in (3) is conducted at a temperature in the range of from 80 to 250°C, preferably from 85 to 220°C, more preferably from 90 to 200°C, more preferably from 95 to 180°C, more preferably from 100 to 170°C, more preferably from 105 to 160°C, more preferably from 1 10 to 150°C, more preferably from 115 to 145°C, more preferably from 120 to 140°C, and more pref- erably in the range of from 125 to 135°C. Preferably, the contacting of the mixture (M1 ) with the catalyst in (3) is conducted at a pressure in the range of from 2 to 50 bar, preferably from 3 to 30 bar, more preferably from 4 to 25 bar, more preferably from 5 to 20 bar, more preferably from 6 to 17 bar, more preferably from 7 to 15 bar, more preferably from 7.5 to 13 bar, more prefera- bly from 8 to 12 bar, more preferably from 8.5 to 1 1.5 bar, more preferably from 9 to 1 1 bar, and more preferably in the range of from 9.5 to 10.5 bar. Preferably, the duration of the contacting of the mixture (M1 ) with the catalyst in (3) is in the range of from 0.05 to 12 h, preferably from 0.1 to 9 h, more preferably from 0.25 to 8 h, more preferably from 0.5 to 7.5 h, more preferably from 1 to 7 h, more preferably from 1.5 to 6.5 h, more preferably from 2 to 6 h, more preferably from 2.5 to 5.5 h, more preferably from 3 to 5 h, more preferably from 3.5 to 4.5 h, and more prefera- bly in the range of from 3.75 to 4.25 h. While there are no specific restrictions, it is preferred that the contacting of the mixture (M1) with the catalyst in (3) and the collecting of the reacted mixture (M2) in (4) is conducted in a continu- ous mode and/or in a batch mode, preferably in a continuous mode.

Preferably, the process is conducted in a continuous mode and/or in a batch mode, more pref- erably in a continuous mode. Preferably, the process is conducted in a continuous mode at a weight hourly space velocity (WHSV) in the range of from 0.08 to 20 lv ¹ , preferably from 0.09 to 15 Ir ¹ , more preferably from 0.1 to 10 lv ¹ , more preferably from 0.12 to 8 lv ¹ , more preferably from 0.14 to 5 lv ¹ , more preferably from 0.16 to 3 lv ¹ , more preferably from 0.18 to 1 lv ¹ , more preferably from 0.2 to 0.5 Ir ¹ , more preferably from 0.22 to 0.3 Ir ¹ , and more preferably in the range of from 0.24 to 0.26 Ir ¹ .

In the context of the present invention, the process preferably further comprises:

(5) separating the ester of formula (III) from the reacted mixture (M2) for obtaining a mixture (M3) containing unreacted carboxylic acid of formula (I) and/or unreacted alkene of formula (II).

In the context of the present invention, the process preferably further comprises:

(6) recycling the mixture (M3) containing unreacted carboxylic acid of formula (I) and/or unre- acted alkene of formula (II) to (1).

In addition to the aforementioned, the present invention further relates to a process for produc- tion of an ester starting from a dicarboxylic acid comprising:

(1) preparing a mixture (M1 ) comprising a carboxylic acid of formula (I’)

la (II)

(2) feeding the mixture (M1) into a reactor containing a catalyst, said catalyst comprising a zeolitic material having a BEA-type framework structure;

(3) contacting the mixture (M1 ) with the catalyst in the reactor for reacting at least a portion of the mixture (M1 ) to an ester of formula (III’) and/or (III”) R' O O R'

^R 1 JL - ^R"

(4) collecting a reacted mixture (M2) containing the ester of formula (III’) and/or (III”) from the reactor;

wherein R’ is an alkyl group;

wherein R” is hydrogen or an alkyl group;

wherein R’” is an alkylene group;

wherein the zeolitic material having a BEA-type framework structure displays an X-ray diffrac tion pattern comprising at least the following reflections:

wherein 100% relates to the intensity of the maximum peak in the 20-45° 20 range of the X-ray powder diffraction pattern, and

wherein the BEA-type framework structure comprises YO ₂ and X ₂ O ₃ , wherein Y is a tetravalent element, and X is a trivalent element.

Preferably, R’” is a single bond or is is an optionally branched and/or optionally substituted and/or optionally unsaturated alkylene group selected from the group consisting of optionally branched and/or optionally substituted and/or optionally unsaturated C1-C16 alkylene groups, preferably C1-C14 alkylene groups, more preferably C1-C12 alkylene groups, more preferably C1-C10 alkylene groups, more preferably C2-C9 alkylene groups, more preferably C2-C8 al- kylene groups, more preferably C2-C7 alkylene groups, more preferably C3-C6 alkylene groups, more preferably C3-C5 alkylene groups, more preferably C3 or C4 alkylene groups, and more preferably C4 alkylene groups, wherein more preferably R’” is selected from the group consisting of optionally substituted methylene, ethylene, propylene, butylene, pentylene, hexylene, heptylene, octylene, nonylene, decylene, dodecylene, tetradecylene, and hexa- decylene, more preferably from the group consisting of optionally substituted methylene, eth- ylene, propylene, butylene, pentylene, hexylene, heptylene, and octylene, more preferably from the group consisting of optionally substituted propylene, butylene, pentylene, and hexylene, wherein more preferably R’” is optionally substituted butylene or pentylene, preferably butylene or pentylene, and more preferably butylene.

According to the embodiments of the present invention starting from a dicarboxylic acid, it is preferred that R’ is an optionally branched and/or optionally substituted and/or optionally un- saturated C1-C18 alkyl groups, preferably C2-C16 alkyl groups, more preferably C3-C14 alkyl groups, more preferably C4-C12 alkyl groups, more preferably C5-C10 alkyl groups, more pref- erably C6-C9 alkyl groups, more preferably C7 or C8 alkyl groups, and more preferably C8 alkyl groups, wherein more preferably R’ is selected from the group consisting of optionally substitut- ed methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, dodecyl, tetradecyl, and hexadecyl, more preferably from the group consisting of optionally substituted butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, dodecyl, more preferably from the group consisting of optional- ly substituted hexyl, heptyl, octyl, nonyl, decyl, wherein more preferably R’ is optionally substi- tuted heptyl or octyl, preferably heptyl or octyl, and more preferably octyl.

With respect to the embodiments of the present invention starting from a dicarboxylic acid, it is preferred that the alkene of formula (II) is selected from the group consisting of optionally substi- tuted C2-C18 alkene, preferably C3-C16 alkene, more preferably C4-C14 alkene, more prefera- bly C5-C12 alkene, more preferably C6-C10 alkene, more preferably C7-C9 alkene, more pref- erably C7 or C8 alkene, and more preferably C10 alkene, wherein more preferably the alkene of formula (II) is selected from the group consisting of optionally substituted ethylene, propylene, butene, pentene, hexene, heptene, octene, nonene, decene, undecene, dodecene, tridecene, tetradecene, pentadecene, and hexadecene, more preferably from the group consisting of op- tionally substituted 1-hexene, 1-heptene, 1-octene, 1-nonene, 1-decene, 1-undecene, 1- dodecene, 1-tridecene, 1 -tetradecene, 1- pentadecene, and 1-hexadecene, more preferably from the group consisting of optionally substituted 1-octene, 1-nonene, 1-decene, 1-undecene, and 1 -dodecene, wherein more preferably the alkene of formula (II) is optionally substituted 1- nonene or 1-decene, preferably 1-nonene or 1-decene, and more preferably 1-decene.

As to the carboxylic acid of formula (G), it is preferred that the carboxylic acid of formula (G) is selected from the group consisting of optionally substituted oxalic acid, malonic acid, succinic acid, glutaric acid, adipic acid, pimelic acid, suberic acid, azelaic acid, sebacic acid, undecane- dioic acid, and dodecanedioic acid, preferably from the group consisting of optionally substituted succinic acid, glutaric acid, adipic acid, pimelic acid, and suberic acid, wherein more preferably the carboxylic acid of formula (G) is optionally substituted glutaric or adipic acid, preferably glu taric or adipic acid, and more preferably adipic acid.

Concerning the embodiments of the present invention starting from a dicarboxylic acid, it is pre- ferred that the alkene : carboxylic acid molar ratio of the alkene of formula (II) to the carboxylic acid of formula (G) in the mixture (M1 ) prepared in (1 ) and reacted in (3) is in the range of from 0.1 : 1 to 20 : 1 , preferably from 0.5 : 1 to 15 : 1 , more preferably from 1 : 1 to 10 : 1 , more pref- erably from 1.3 : 1 to 5 : 1 , more preferably from 1.5 : 1 to 3 : 1 , more preferably from 1.7 : 1 to 2.5 : 1 , more preferably from 1.9 : 1 to 2.3 : 1 , and more preferably from 1.95 : 1 to 2.1 : 1. With regard to the embodiments of the present invention starting from a dicarboxylic acid, it is preferred that the mixture (M1 ) prepared in (1) and reacted in (3) contains 50 wt.-% or less of water based on 100 wt.-% of the carboxylic acid of formula (G), preferably 20 wt.-% or less, more preferably 10 wt.-% or less, more preferably 5 wt.-% or less, more preferably 1 wt.-% or less, more preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more preferably 0.01 wt.-% or less, more preferably 0.005 wt.-% or less, more preferably 0.001 wt.-% or less, more preferably 0.0005 wt.-% or less, and more preferably 0.0001 wt.-% or less of water based on 100 wt.-% of the carboxylic acid of formula (G).

According to the embodiments of the present invention starting from a dicarboxylic acid, it is preferred that the mixture (M1 ) prepared in (1) and reacted in (3) comprises 50 mol% or less of an alcohol of formula (IV)

based on 100 mol% of the carboxylic acid of formula (I’), preferably 20 mol% or less, more pref- erably 10 mol% or less, more preferably 5 mol% or less, more preferably 1 mol% or less, more preferably 0.5 mol% or less, more preferably 0.1 mol% or less, more preferably 0.05 mol% or less, more preferably 0.01 mol% or less, more preferably 0.005 mol% or less, more preferably 0.001 mol% or less, more preferably 0.0005 mol% or less, and more preferably 0.0001 mol% or less of an alcohol of the formula (IV) based on 100 mol% of the carboxylic acid of formula (G).

Regarding the embodiments of the present invention starting from a dicarboxylic acid, it is pre- ferred that the mixture (M1) prepared in (1 ) and reacted in (3) contains 50 wt.% or less of ele- ments and/or compounds other than the carboxylic acid of formula (G) and the alkene of formula (II) based on 100 wt.-% of the carboxylic acid of formula (G), preferably 20 wt.-% or less, more preferably 10 wt.-% or less, more preferably 5 wt.-% or less, more preferably 1 wt.-% or less, more preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more preferably 0.01 wt.-% or less, more preferably 0.005 wt.-% or less, more prefera- bly 0.001 wt.-% or less, more preferably 0.0005 wt.-% or less, and more preferably 0.0001 wt- % or less of elements and/or compounds other than the carboxylic acid of formula (G) and the alkene of formula (II) based on 100 wt.-% of the carboxylic acid of formula (G).

Concerning the embodiments of the present invention starting from a dicarboxylic acid, it is pre- ferred that the mixture (M1) prepared in (1 ) and reacted in (3) consists of a mixture of the car- boxylic acid of formula (G) and the alkene of formula (II).

With regard to the embodiments of the present invention starting from a dicarboxylic acid, it is preferred that the contacting of the mixture (M1 ) with the catalyst in (3) is conducted at a tem- perature in the range of from 80 to 250°C, preferably from 100 to 230°C, more preferably from 1 10 to 210°C, more preferably from 120 to 200°C, more preferably from 130 to 190°C, more preferably from 140 to 180°C, more preferably from 145 to 175°C, more preferably from 150 to 170°C, and more preferably in the range of from 155 to 165°C.

As concerns the embodiments of the present invention starting from a dicarboxylic acid, it is preferred that the process further comprises:

(5) separating the ester of formula (III’) and/or (III”) from the reacted mixture (M2) for obtain- ing a mixture (M3) containing unreacted carboxylic acid of formula (G) and/or unreacted alkene of formula (II).

Furthermore, it is preferred according to the embodiments of the present invention starting from a dicarboxylic acid that the process further comprises:

(6) recycling the mixture (M3) containing unreacted carboxylic acid of formula (G) and/or un- reacted alkene of formula (II) to (1 ).

While there are no specific restrictions, it is preferred that the zeolitic material having a BEA- type framework structure comprised in the catalyst, displays a YO ₂ : X ₂ O ₃ molar ratio in the range of from 2 to 300, preferably from 4 to 200, more preferably from 6 to 150, more preferably from 8 to 100, more preferably from 12 to 70, more preferably from 14 to 50, more preferably from 16 to 40, more preferably from 18 to 35, more preferably from 20 to 30, and more prefera- bly from 22 to 26.

In the context of the present invention Y may be any tetravalent element. Preferably, the tetra- valent element Y of the zeolitic material having a BEA-type framework structure comprised in the catalyst, is selected from the group consisting of Si, Sn, Ti, Zr, Ge, and a mixture of two or more thereof, Y more preferably being Si.

In the context of the present invention X may be any trivalent element. Preferably, the trivalent element X of the zeolitic material having a BEA-type framework structure comprised in the cata- lyst, is selected from the group consisting of Al, B, In, Ga, and a mixture of two or more thereof, X more preferably being Al.

Preferably, the zeolitic material having a BEA-type framework structure comprised in the cata- lyst, has a total amount of acid sites in the range of from 0.25 to 1.0 mmol/g, preferably from 0.15 to 0.8 mmol/g, more preferably from 0.2 to 0.7 mmol/g, more preferably from 0.25 to 0.6 mmol/g, more preferably from 0.3 to 0.55 mmol/g, more preferably from 0.35 to 0.5 mmol/g, more preferably from 0.38 to 0.45 mmol/g, and more preferably from 0.4 to 0.42 mmol/g, wherein the total amount of acid sites is defined as the total molar amount of desorbed ammo- nia per mass of the zeolitic material determined according to the temperature programmed de- sorption of ammonia (NH ₃ -TPD).

Preferably, the zeolitic material having a BEA-type framework structure comprised in the cata- lyst, has an amount of medium acid sites, wherein the amount of medium acid sites is defined as the amount of desorbed ammonia per mass of the zeolitic material determined according to the temperature programmed desorption of ammonia (NH ₃ -TPD) in the temperature range of from 250 to 500 °C, wherein the amount of medium acid sites is at least 40% of the total amount of acid sites, preferably from 42 to 90%, more preferably from 44 to 80%, more preferably from 46 to 75%, more preferably from 48 to 70%, more preferably from 50 to 65%, more preferably from 53 to 60%, and more preferably from 55 to 57% of the total amount of acid sites. Prefera- bly, the amount of medium acid sites is in the range of from 0.10 to 0.90 mmol/g, preferably from 0.12 to 0.7 mmol/g, more preferably from 0.14 to 0.5 mmol/g, more preferably from 0.16 to 0.4 mmol/g, more preferably from 0.18 to 0.3 mmol/g, more preferably from 0.2 to 0.26 mmol/g, and more preferably from 0.22 to 0.24 mmol/g.

Preferably, the zeolitic material having a BEA-type framework structure comprised in the cata- lyst, has an amount of strong acid sites, preferably the amount of strong acid sites of the zeolitic material having a BEA-type framework structure comprised in the catalyst, defined as the amount of desorbed ammonia per mass of the zeolitic material determined according to the temperature programmed desorption of ammonia (NH ₃ -TPD) in the temperature range above 500 °C, preferably in the range of from 0 to 0.10 mmol/g, preferably from 0.00 to 0.07 mmol/g, more preferably from 0.00 to 0.05 mmol/g, more preferably from 0.00 to 0.04 mmol/g, more preferably from 0.00 to 0.03 mmol/g, more preferably from 0.00 to 0.02 mmol/g, more preferably from 0.00 to 0.015 mmol/g, more preferably from 0.00 to 0.01 mmol/g, and more preferably from 0.00 to 0.005 mmol/g.

The total amount of acid sites as well as the amount of medium acid sites and the amount of strong acid sites as used herein may readily be measured by known methods, preferably by temperature-programmed desorption of ammonia (NH ₃ -TPD), preferably with an automated chemisorption analysis unit having a thermal conductivity detector, preferably by continuous analysis of the desorbed species by an online mass spectrometer, preferably the temperature being measured by a Ni/Cr/Ni thermocouple immediately above the sample in a quartz tube, more preferably wherein the online mass spectrometer monitors the desorption of ammonia by utilizing the molecular weight of ammonia of 16, wherein more preferably the automated chemi- sorption analysis unit is a Micromeritics AutoChem II 2920, wherein more preferably the online mass spectrometer is a OmniStar QMG200 from Pfeiffer Vacuum. Preferably said measurement comprises 1. a preparation step, 2. a saturation with NH ₃ step, 3. a step wherein excess ammo- nia is removed and 4. a NH ₃ -TPD step, more preferably wherein the 4. NH ₃ -TPD step for the total amount of acid sites comprises heating under a He flow to 600 °C, preferably at a heating rate of 10 K/min, preferably wherein the temperature of 600 °C is then held for 30 minutes. It is more preferred that for determining the amount of medium acid sites, said 4. NH ₃ -TPD step is carried out at the temperature range of from 250 to 500 °C. It is more preferred that for deter- mining the amount of strong acid sites, said 4. NH ₃ -TPD step is carried out in the temperature range above 500 °C. According to the present invention it is more preferred that the total amount of acid sites as well as the amount of medium acid sites and the amount of strong acid sites as used herein are determined according to the method described herein in the examples under“determination of the acid sites”.

While there are no specific restrictions, it is preferred that the ratio of the amount of medium acid sites relative to amount of strong acid sites is greater than 0, preferably 10 or greater, more preferably 50 or greater, more preferably 100, more preferably 10 ³ or greater, more preferably 10 ⁴ or greater, more preferably 10 ⁵ or greater, more preferably 10 ⁶ or greater, more preferably 10 ⁷ or greater, more preferably 10 ⁸ or greater, and more preferably 10 ⁹ or greater.

As to step (2), it is preferred that the zeolitic material having a BEA-type framework structure is obtainable and/or obtained according to an organotemplate-free synthetic process.

While there are no specific restrictions, it is preferred that the organotemplate-free synthetic process comprises

(A) preparing a mixture comprising one or more sources for YO ₂ , one or more sources for X ₂ O ₃ , and seed crystals, the seed crystals comprising one or more zeolitic materials having a BEA-type framework structure;

(B) crystallizing the mixture obtained in (A) for obtaining a zeolitic material having a BEA-type framework structure;

wherein Y is a tetravalent element, and X is a trivalent element, and

wherein the mixture prepared in (A) and crystallized in (B) does not contain an organotemplate as structure-directing agent.

Preferably, the mixture prepared in (A) and crystallized in (B) contains 5 wt.-% or less of carbon calculated as the element and based on 100 wt.-% of Y contained in the mixture, preferably 1 wt.-% or less, more preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less, more prefer- ably 0.05 wt.-% or less, more preferably 0.01 wt.-% or less, more preferably 0.005 wt.-% or less, more preferably 0.001 wt.-% or less, more preferably 0.0005 wt.-% or less, and more preferably 0.0001 wt.-% or less of carbon calculated as the element and based on 100 wt.-% of Y con- tained in the mixture. Preferably, the zeolitic material having a BEA-type framework structure obtained in (B) comprises one or more alkali metals M, wherein M is preferably selected from the group consisting of Li, Na, K, Cs, and combinations of two or more thereof, more preferably from the group consisting of Li, Na, K, and combinations of two or more thereof, wherein more preferably the alkali metal M is Na and/or K, more preferably Na.

While there are no specific restrictions, it is preferred that the molar ratio M : YO ₂ in the mixture prepared in (A) and crystallized in (B) is in the range of from 0.05 to 5, preferably from 0.1 to 2, more preferably from 0.3 to 1 , more preferably from 0.4 to 0.8, more preferably from 0.45 to 0.7, more preferably from 0.5 to 0.65, and more preferably from 0.55 to 0.6.

In the context of the present invention Y may be any tetravalent element. Preferably, Y is se- lected from the group consisting of Si, Sn, Ti, Zr, Ge, and a mixture of two or more thereof, Y more preferably being Si. Generally, according to (A), any suitable one or more sources of YO ₂ can be used. Preferably, the one or more sources for YO ₂ contained in the mixture prepared in (A) and crystallized in (B) comprises one or more silicates, more preferably one or more alkali metal silicates, wherein the alkali metal is preferably selected from the group consisting of Li,

Na, K, Rb, and Cs, wherein more preferably the alkali metal is Na and/or K, and wherein more preferably the alkali metal is Na, wherein more preferably the one or more sources for YO ₂ con- tained in the mixture prepared in (A) and crystallized in (B) comprises water glass, preferably sodium and/or potassium silicate, more preferably sodium silicate. Preferably, the one or more sources for YO ₂ contained in the mixture prepared in (A) and crystallized in (B) further compris- es one or more silicas, more preferably one or more silica hydrosols and/or one or more colloi dal silicas, and more preferably one or more colloidal silicas.

In the context of the present invention X may be any trivalent element. Preferably, X is selected from the group consisting of Al, B, In, Ga, and a mixture of two or more thereof, X more prefera- bly being Al. Generally, according to (A), any suitable one or more sources of X ₂ O ₃ can be used. Preferably, the one or more sources for X ₂ O ₃ contained in the mixture prepared in (A) and crys- tallized in (B) comprises one or more aluminate salts, preferably an aluminate of an alkali metal, wherein the alkali metal is preferably selected from the group consisting of Li, Na, K, Rb, and Cs, wherein more preferably the alkali metal is Na and/or K, and wherein more preferably the alkali metal is Na.

While there are no specific restrictions, it is preferred that the molar ratio YO ₂ : X ₂ O ₃ of the mix- ture prepared in (A) and crystallized in (B) is in the range of from 1 to 200, preferably from 5 to 100, more preferably from 10 to 50, more preferably from 15 to 40, more preferably from 20 to 30, more preferably from 23 to 25, and more preferably from 23.5 to 24.

As to the seed crystals comprising one or more zeolitic materials having a BEA-type framework structure, preferably the amount of seed crystals comprised in the mixture prepared in (A) and crystallized in (B) is in the range of from 0.1 to 30 wt.-% based on 100 wt.-% of the one or more sources of YO ₂ in the mixture, calculated as YO ₂ , preferably from 0.5 to 20 wt.-%, more prefera- bly from 1 to 10 wt.-%, more preferably from 1.5 to 5 wt.-%, more preferably from 2 to 4 wt.-%, and more preferably from 2.5 to 3.5 wt.-%.

Preferably, the mixture prepared in (A) and crystallized in (B) further comprises one or more solvents, wherein said one or more solvents preferably comprises water, more preferably deion- ized water, wherein more preferably water is employed as the solvent further comprised in the mixture prepared in (A) and crystallized in (B), preferably deionized water. While there are no specific restrictions, it is preferred that the molar ratio H ₂ 0 : YO ₂ of the mixture prepared in (A) and crystallized in (B) is in the range of from 5 to 100, preferably from 10 to 50, more preferably from 13 to 30, more preferably from 15 to 20, and more preferably from 17 to 18.

As to step B, it is preferred that the crystallization in (B) involves heating of the mixture, prefera- bly at a temperature in the range of from 80 to 200°C, more preferably from 90 to 180°C, more preferably from 100 to 160°C, more preferably from 1 10 to 140°C, and more preferably from 1 15 to 130°C. Preferably, the crystallization in (B) is conducted under autogenous pressure, preferably under solvothermal conditions, and more preferably under hydrothermal conditions.

In (B) the mixture is preferably heated for a period in the range of from 5 to 200 h, preferably from 20 to 160 h, more preferably from 60 to 140 h, and more preferably from 100 to 130 h.

In the context of the present invention, the organotemplate-free synthetic process for the prepa- ration of the zeolitic material having a BEA-type framework structure preferably further compris- es

(C) isolating the zeolitic material having a BEA-type framework structure obtained in (B), pref- erably by filtration; and

(D) optionally washing the zeolitic material having a BEA-type framework structure obtained in (B) or (C), preferably in (C); and/or,

(E) optionally drying the zeolitic material having a BEA-type framework structure obtained in (B), (C) or (D), preferably in (D);

wherein the steps (C) and/or (D) and/or (E) can be conducted in any order, and

wherein one or more of said steps is preferably repeated one or more times.

In the context of the present invention, the organotemplate-free synthetic process for the prepa- ration of the zeolitic material having a BEA-type framework structure preferably further compris- es

(F) exchanging one or more of the ionic non-framework elements contained in the zeolitic material having a BEA-type framework structure obtained in (C), (D), or (E), preferably in (E), against H ⁺ and/or NH ₄ ⁺ , preferably against NH ₄ ⁺ ; and/or, preferably and

(G) drying and/or calcining, preferably drying and calcining the zeolitic material having a BEA- type framework structure obtained in (C), (D), (E), or (F).

In the context of the present invention, the organotemplate-free synthetic process for the prepa- ration of the zeolitic material having a BEA-type framework structure preferably further compris- es

(H) treating the zeolitic material having a BEA-type framework structure obtained in (C), (D), (E), (F), or (G), preferably in (G), with an aqueous solution having a pH of at most 5; and

(I) isolating the zeolitic material having a BEA-type framework structure obtained in (H), pref- erably by filtration; and/or,

(J) optionally washing the zeolitic material having a BEA-type framework structure obtained in (H) or (I), preferably in (I); and/or

(K) optionally drying and/or calcining, preferably drying and calcining the zeolitic material hav- ing a BEA-type framework structure obtained in (H), (I), or (J), preferably in (J);

wherein the steps (I) and/or (J) and/or (K) can be conducted in any order, and

wherein one or more of said steps is preferably repeated one or more times.

As to step (H), preferably the pH of the aqueous solution used for treating the zeolitic material in (H) has a pH in the range of from -1 to 4.5, more preferably of from -0.5 to 4, more preferably of from -0.2 to 3.5, more preferably of from -0.15 to 3, more preferably of from -0.1 to 2.5, more preferably of from -0.05 to 2, more preferably of from 0 to 1.5, more preferably of from 0.05 to 1 , more preferably of from 0.1 to 0.5, and more preferably of from 0.15 to 0.25. Preferably, in (H) the zeolitic material is added to the aqueous solution, and the mixture is heated, preferably at a temperature in the range of from 30 to 100°C, more preferably from 35 to 90°C, more preferably from 40 to 80°C, more preferably from 45 to 75°C, more preferably from 50 to 70°C, and more preferably from 55 to 65°C. Preferably, in (H) the mixture is heated for a period in the range of from 0.1 to 10 h, preferably from 0.1 to 7 h, more preferably from 0.5 to 5 h, more preferably from 0.5 to 4.5 h, more preferably from 1 to 4 h, more preferably from 1 to 3.5 h, more prefera- bly from 1.5 to 3 h, and more preferably from 1.5 to 2.5 h.

In the context of the present invention, the organotemplate-free synthetic process for the prepa- ration of the zeolitic material having a BEA-type framework structure preferably further compris- es

(L) treating the zeolitic material obtained in (H), (I), (J), or (K), preferably in (K), with a liquid aqueous system having a pH in the range of from 5.5 to 8 and a temperature of at least 75 C; and/or,

(M) optionally washing the zeolitic material having a BEA-type framework structure obtained in (L); and/or,

(N) optionally drying the zeolitic material having a BEA-type framework structure obtained in (L) or (M), preferably in (M);

wherein the steps (M) and (N) can be conducted in any order, and

wherein one or more of said steps is preferably repeated one or more times.

As to step (L), it is preferred that the pH of the liquid aqueous system used for treating the zeo- litic material in (L) has a pH in the range of from 5.5 to 12, more preferably from 5.5 to 10, more preferably from 6 to 9, more preferably from 6 to 8.5, more preferably from 6.5 to 8, and more preferably from 6.5 to 7.5. Preferably, in (L) the zeolitic material is added to the liquid aqueous system, and the mixture is heated, more preferably at a temperature in the range of from 40 to 100°C, preferably of from 50 to 100°C, more preferably of from 60 to 100°C, more preferably of from 65 to 95°C, more preferably of from 70 to 95°C, more preferably of from 75 to 95°C, more preferably of from 80 to 90°C, and more preferably of from 85 to 90°C. Preferably, in (L) the mixture is heated for a period in the range of from 1 to 40 h, preferably from 3 to 30 h, more preferably from 5 to 25 h, more preferably from 6 to 20 h, more preferably from 7 to 15 h, more preferably from 7.5 to 12 h, more preferably from 8 to 10 h, and more preferably from 8.5 to 9.5 h. Preferably, in (L) the liquid aqueous system comprises water, preferably deionized water, wherein more preferably the liquid aqueous system is water, preferably deionized water.

Preferably (H) and (L), more preferably (H), (I), and (L), more preferably (H), (I), (K), and (L), and more preferably (H), (I), (J), (K), (L), (M), and (N) are repeated one or more times, prefera- bly one to five times, more preferably two to four times, and more preferably three times.

In the context of the present invention, the organotemplate-free synthetic process for the prepa- ration of the zeolitic material having a BEA-type framework structure preferably further compris- es

(O) treating the zeolitic material having a BEA-type framework structure obtained in (L), (M), or (N), preferably in (N), with an aqueous solution having a pH of at most 3; and

(P) isolating the zeolitic material having a BEA-type framework structure obtained in (O), pref- erably by filtration; and/or,

(Q) optionally washing the zeolitic material having a BEA-type framework structure obtained in (O) or (P), preferably in (P); and/or,

(R) optionally drying and/or calcining, preferably drying and calcining the zeolitic material hav- ing a BEA-type framework structure obtained in (O), (P), or (Q), preferably in (Q);

wherein the steps (P) and/or (Q) and/or (R) can be conducted in any order, and

wherein one or more of said steps is preferably repeated one or more times. As to step (O), it is preferred that the pH of the aqueous solution used for treating the zeolitic material in (O) has a pH in the range of from -2 to 2, more preferably from -1.5 to 1 , more pref- erably from -1 to 0, more preferably from -0.7 to -0.1 , more preferably from -0.5 to -0.3, and more preferably from -0.45 to -0.35. Preferably, in (O) the zeolitic material is added to the aque- ous solution, and the mixture is heated, preferably at a temperature in the range of from 30 to 100°C, more preferably from 35 to 90°C, more preferably from 40 to 80°C, more preferably from 45 to 75°C, more preferably from 50 to 70°C, and more preferably from 55 to 65°C. Preferbly, in (O) the mixture is heated for a period in the range of from 0.1 to 10 h, preferably from 0.1 to 7 h, more preferably from 0.5 to 5 h, more preferably from 0.5 to 4.5 h, more preferably from 1 to 4 h, more preferably from 1 to 3.5 h, more preferably from 1.5 to 3 h, and more preferably from 1.5 to 2.5 h.

Preferably, in (H) and/or (O), preferably in (H) and (O), the aqueous solution comprises a min- eral acid, preferably a mineral acid selected from the list consisting of HF, HCI, HBr, HNO ₃ , H3PO4, H2SO4, H3BO3, HCIO4, and mixtures of two or more thereof, more preferably from the list consisting of HCI, HBr, HNO ₃ , H ₂ SO ₄ , HCIO ₄ , and mixtures of two or more thereof, more prefer- ably from the list consisting of HCI, HNO ₃ , H ₂ SO ₄ , and mixtures of two or more thereof, wherein more preferably the aqueous solution comprises HCI and/or HNO ₃ , preferably HNO ₃ .

In the context of the present invention, preferably drying in (E) and/or (G) and/or (K) and/or (N) and/or (R), preferably in (E), (G), (K), (N), and (R) is conducted at a temperature in the range of from 80 to 200°C, more preferably from 90 to 180°C, more preferably from 100 to 160°C, more preferably from 1 10 to 140°C, and more preferably from 115 to 130°C. Preferably, drying in (E) and/or (G) and/or (K) and/or (N) and/or (R), preferably in (E), (G), (K), (N), and (R) is conducted for a period in the range of from 1 to 120 h, preferably from 5 to 96 h, more preferably from 8 to 72 h, more preferably from 10 to 60 h, more preferably from 12 to 48 h, more preferably from 14 to 42 h, more preferably from 16 to 36 h, more preferably from 18 to 30 h, more preferably from 20 to 24 h, and more preferably from 21 to 23 h.

In the context of the present invention, preferably calcining in (G) and/or (K) and/or (R), prefera- bly in (G), (K) and (R) is conducted at a temperature in the range of from 250 to 1 ,000°C, pref- erably from 300 to 900°C, more preferably from 350 to 850°C, more preferably from 400 to 800°C, more preferably from 450 to 750°C, more preferably from 500 to 700°C, and more pref- erably from 550 to 650°C. Preferably, calcining in (G) and/or (K) and/or (R), preferably in (G), (K) and (R) is conducted for a period in the range of from 0.5 to 36 h, more preferably from 1 to 24 h, more preferably from 1.5 to 18 h, more preferably from 2 to 12 h, more preferably from 2.5 to 9 h, more preferably from 3 to 7 h, more preferably from 3.5 to 6.5 h, more preferably from 4 to 6 h, and more preferably from 4.5 to 5.5 h.

In the context of the present invention, the zeolitic material having a BEA-type framework struc- ture formed in (B) preferably comprises zeolite beta. Furthermore, in the context of the present invention preferably the seed crystals contained in the mixture prepared in (A) and crystallized in (B) comprise a zeolitic material having a BEA- type framework structure, preferably zeolite beta, and more preferably a zeolitic material having a BEA-type framework structure as obtainable and/or obtained according to the organotem- plate-free synthetic process for the preparation of the zeolitic material having a BEA-type framework structure as defined in in the process defined herein above.

The present invention is further illustrated by the following set of embodiments and combina- tions of embodiments resulting from the dependencies and back-references as indicated. In particular, it is noted that in each instance where a range of embodiments is mentioned, for ex- ample in the context of a term such as "The process of any one of embodiments 1 to 4", every embodiment in this range is meant to be explicitly disclosed for the skilled person, i.e. the word- ing of this term is to be understood by the skilled person as being synonymous to "The process of any one of embodiments 1 , 2, 3, and 4".

1. A process for the production of an ester comprising:

(1) preparing a mixture (M1 ) comprising a carboxylic acid of formula (I)

and an alkene of formula (II)

(2) feeding the mixture (M1) into a reactor containing a catalyst, said catalyst compris- ing a zeolitic material having a BEA-type framework structure;

(3) contacting the mixture (M1 ) with the catalyst in the reactor for reacting at least a por- tion of the mixture (M1 ) to an ester of formula (III)

O R'

· (in);

(4) collecting a reacted mixture (M2) containing the ester of formula (III) from the reac- tor;

wherein R and R’ are alkyl groups;

wherein R” is hydrogen or an alkyl group;

wherein the zeolitic material having a BEA-type framework structure displays an X-ray dif fraction pattern comprising at least the following reflections: wherein 100% relates to the intensity of the maximum peak in the 20-45° 20 range of the X-ray powder diffraction pattern, and

wherein the BEA-type framework structure comprises YO ₂ and X ₂ O ₃ , wherein Y is a tetra- valent element, and X is a trivalent element.

2 The process of embodiment 1 , wherein R is an optionally branched and/or optionally sub- stituted and/or optionally unsaturated alkyl group selected from the group consisting of op- tionally branched and/or optionally substituted and/or optionally unsaturated C1-C24 alkyl groups, preferably C2-C22 alkyl groups, more preferably C4-C20 alkyl groups, more pref- erably C6-C18 alkyl groups, more preferably C8-C18 alkyl groups, more preferably C10- C16 alkyl groups, more preferably C12-C16 alkyl groups, more preferably C12-C14 alkyl groups, more preferably C12 or C14 alkyl groups, and more preferably C14 alkyl groups, wherein more preferably R is selected from the group consisting of optionally substituted methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, undecyl, dodecyl, tridecyl, tetradecyl, pentadecyl, and hexadecyl, more preferably from the group consisting of optionally substituted dodecyl, tridecyl, tetradecyl, pentadecyl, and hexadecyl, more preferably from the group consisting of optionally substituted dodecyl, tetradecyl, and hexadecyl, wherein more preferably R is optionally substituted dodecyl or tetradecyl, pref- erably dodecyl or tetradecyl, and more preferably tetradecyl. 3 The process of any of embodiments 1 or 2, wherein R’ is an optionally branched and/or optionally substituted and/or optionally unsaturated alkyl group selected from the group consisting of optionally branched and/or optionally substituted and/or optionally unsaturat- ed C1-C6 alkyl groups, preferably C1-C5 alkyl groups, more preferably C1-C4 alkyl groups, more preferably C1-C3 alkyl groups, more preferably C1-C2 alkyl groups, and more preferably C1 alkyl groups, wherein more preferably R’ is selected from the group consisting of optionally substituted methyl, ethyl, propyl, butyl, pentyl, and hexyl, more preferably from the group consisting of optionally substituted methyl, ethyl, propyl, butyl, and pentyl, more preferably from the group consisting of optionally substituted methyl, ethyl, propyl, and butyl, more preferably from the group consisting of optionally substituted methyl, ethyl, and propyl, wherein more preferably R’ is optionally substituted methyl or ethyl, preferably methyl.

4. The process of any of embodiments 1 to 3, wherein the alkene of formula (II) is selected from the group consisting of optionally substituted ethylene, propylene, 1 -butene, 2- butene, and isobutene, wherein preferably the alkene of formula (II) is optionally substitut- ed ethylene or propylene, preferably ethylene or propylene, and more preferably propyl- ene.

5. The process of any of embodiments 1 to 4, wherein the carboxylic acid of formula (I) is myristic acid and the alkene of formula (II) is propylene.

6. The process of any of embodiments 1 to 4, wherein the carboxylic acid of formula (I) is lauric acid and the alkene of formula (II) is propylene.

7. The process of any of embodiments 1 to 6, wherein the carboxylic acid of formula (I) is selected from the group consisting of optionally substituted formic acid, acetic acid, propi- onic acid, valeric acid, acrylic acid, methacrylic acid, and crotonic acid, wherein preferably the carboxylic acid of formula (I) is optionally substituted acetic acid or acrylic acid.

8. The process of any of embodiments 1 to 4 or embodiment 7, wherein the carboxylic acid of formula (I) is acetic acid and the alkene of formula (II) is ethylene.

9. The process of any of embodiments 1 to 4 or embodiment 7, wherein the carboxylic acid of formula (I) is acrylic acid and the alkene of formula (II) is ethylene.

10. The process of any of embodiments 1 to 9, wherein the alkene : carboxylic acid molar ratio of the alkene of formula (II) to the carboxylic acid of formula (I) in the mixture (M1) prepared in (1 ) and reacted in (3) is in the range of from 0.1 : 1 to 1 : 0.1 , preferably from 0.3 : 1 to 1 : 0.3, more preferably from 0.5 : 1 to 1 : 0.5, more preferably from 0.7 : 1 to 1 : 0.7, more preferably from 0.8 : 1 to 1 : 0.8, more preferably from 0.85 : 1 to 1 : 0.85, more preferably from 0.9 : 1 to 1 : 0.9, and more preferably from 0.95 : 1 to 1 : 0.95.

11. The process of any of embodiments 1 to 10, wherein the mixture (M1 ) prepared in (1 ) and reacted in (3) contains 50 wt.-% or less of water based on 100 wt.-% of the carboxylic acid of formula (I), preferably 20 wt.-% or less, more preferably 10 wt.-% or less, more prefera- bly 5 wt.-% or less, more preferably 1 wt.-% or less, more preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more preferably 0.01 wt.-% or less, more preferably 0.005 wt.-% or less, more preferably 0.001 wt.-% or less, more preferably 0.0005 wt.-% or less, and more preferably 0.0001 wt.-% or less of water based on 100 wt.-% of the carboxylic acid of formula (I).

12. The process of any of embodiments 1 to 1 1 , wherein the mixture (M1 ) prepared in (1 ) and reacted in (3) comprises 50 mol% or less of an alcohol of formula (IV)

based on 100 mol% of the carboxylic acid of formula (I), preferably 20 mol% or less, more preferably 10 mol% or less, more preferably 5 mol% or less, more preferably 1 mol% or less, more preferably 0.5 mol% or less, more preferably 0.1 mol% or less, more preferably 0.05 mol% or less, more preferably 0.01 mol% or less, more preferably 0.005 mol% or less, more preferably 0.001 mol% or less, more preferably 0.0005 mol% or less, and more preferably 0.0001 mol% or less of an alcohol of the formula (IV) based on 100 mol% of the carboxylic acid of formula (I).

13. The process of any of embodiments 1 to 12, wherein the mixture (M1 ) prepared in (1 ) and reacted in (3) contains 50 wt.% or less of elements and/or compounds other than the car- boxylic acid of formula (I) and the alkene of formula (II) based on 100 wt.-% of the carbox- ylic acid of formula (I), preferably 20 wt.-% or less, more preferably 10 wt.-% or less, more preferably 5 wt.-% or less, more preferably 1 wt.-% or less, more preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more prefera- bly 0.01 wt.-% or less, more preferably 0.005 wt.-% or less, more preferably 0.001 wt.-% or less, more preferably 0.0005 wt.-% or less, and more preferably 0.0001 wt.-% or less of elements and/or compounds other than the carboxylic acid of formula (I) and the alkene of formula (II) based on 100 wt.-% of the carboxylic acid of formula (I).

14. The process of any of embodiments 1 to 13, wherein the mixture (M1 ) prepared in (1 ) and reacted in (3) consists of a mixture of the carboxylic acid of formula (I) and the alkene of formula (II).

15. The process of any of embodiments 1 to 14, wherein the contacting of the mixture (M1) with the catalyst in (3) is conducted at a temperature in the range of from 80 to 250°C, preferably from 85 to 220°C, more preferably from 90 to 200°C, more preferably from 95 to 180°C, more preferably from 100 to 170°C, more preferably from 105 to 160°C, more preferably from 1 10 to 150°C, more preferably from 115 to 145°C, more preferably from 120 to 140°C, and more preferably in the range of from 125 to 135°C. 16. The process of any of embodiments 1 to 15, wherein the process further comprises:

(5) separating the ester of formula (III) from the reacted mixture (M2) for obtaining a mixture (M3) containing unreacted carboxylic acid of formula (I) and/or unreacted alkene of formula (II).

17. The process of embodiment 16, wherein the process further comprises:

(6) recycling the mixture (M3) containing unreacted carboxylic acid of formula (I) and/or unreacted alkene of formula (II) to (1).

18. A process for the production of an ester comprising:

(1) preparing a mixture (M1 ) comprising a carboxylic acid of formula (G)

la (II)

(2) feeding the mixture (M1) into a reactor containing a catalyst, said catalyst compris- ing a zeolitic material having a BEA-type framework structure;

(3) contacting the mixture (M1 ) with the catalyst in the reactor for reacting at least a por- tion of the mixture (M1 ) to an ester of formula (III’) and/or (III”)

(4) collecting a reacted mixture (M2) containing the ester of formula (IN’) and/or (III”) from the reactor;

wherein R’ is an alkyl group;

wherein R” is hydrogen or an alkyl group;

wherein R”’ is an alkylene group;

wherein the zeolitic material having a BEA-type framework structure displays an X-ray dif fraction pattern comprising at least the following reflections: wherein 100% relates to the intensity of the maximum peak in the 20-45° 20 range of the X-ray powder diffraction pattern, and

wherein the BEA-type framework structure comprises YO ₂ and X ₂ O ₃ , wherein Y is a tetra- valent element, and X is a trivalent element. The process of embodiment 18, wherein R’” is a single bond or is an optionally branched and/or optionally substituted and/or optionally unsaturated alkylene group selected from the group consisting of optionally branched and/or optionally substituted and/or optionally unsaturated C1-C16 alkylene groups, preferably C1-C14 alkylene groups, more preferably C1-C12 alkylene groups, more preferably C1-C10 alkylene groups, more preferably C2-

C9 alkylene groups, more preferably C2-C8 alkylene groups, more preferably C2-C7 al- kylene groups, more preferably C3-C6 alkylene groups, more preferably C3-C5 alkylene groups, more preferably C3 or C4 alkylene groups, and more preferably C4 alkylene groups, wherein more preferably R’” is selected from the group consisting of optionally substituted methylene, ethylene, propylene, butylene, pentylene, hexylene, heptylene, oc- tylene, nonylene, decylene, dodecylene, tetradecylene, and hexadecylene, more prefera- bly from the group consisting of optionally substituted methylene, ethylene, propylene, bu- tylene, pentylene, hexylene, heptylene, and octylene, more preferably from the group consisting of optionally substituted propylene, butylene, pentylene, and hexylene, wherein more preferably R’” is optionally substituted butylene or pentylene, preferably butylene or pentylene, and more preferably butylene. The process of any of embodiments 18 or 19, wherein R’ is an optionally branched and/or optionally substituted and/or optionally unsaturated C1-C18 alkyl groups, preferably C2- C16 alkyl groups, more preferably C3-C14 alkyl groups, more preferably C4-C12 alkyl groups, more preferably C5-C10 alkyl groups, more preferably C6-C9 alkyl groups, more preferably C7 or C8 alkyl groups, and more preferably C8 alkyl groups, wherein more preferably R’ is selected from the group consisting of optionally substituted methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, dodecyl, tetradecyl, and hexadecyl, more preferably from the group consisting of optionally substituted butyl, pentyl, hexyl, heptyl, octyl, nonyl, decyl, dodecyl, more preferably from the group consisting of optionally substituted hexyl, heptyl, octyl, nonyl, decyl, wherein more preferably R’ is optionally sub- stituted heptyl or octyl, preferably heptyl or octyl, and more preferably octyl.

21. The process of any of embodiments 18 to 20, wherein the alkene of formula (II) is select- ed from the group consisting of optionally substituted C2-C18 alkene, preferably C3-C16 alkene, more preferably C4-C14 alkene, more preferably C5-C12 alkene, more preferably C6-C10 alkene, more preferably C7-C9 alkene, more preferably C7 or C8 alkene, and more preferably C10 alkene, wherein more preferably the alkene of formula (II) is selected from the group consisting of optionally substituted ethylene, propylene, butene, pentene, hexene, heptene, octene, nonene, decene, undecene, dodecene, tridecene, tetradecene, pentadecene, and hexadecene, more preferably from the group consisting of optionally substituted 1 -hexene, 1 -heptene, 1 -octene, 1 -nonene, 1 -decene, 1 -undecene, 1- dodecene, 1 -tridecene, 1 -tetradecene, 1- pentadecene, and 1 -hexadecene, more prefera- bly from the group consisting of optionally substituted 1 -octene, 1 -nonene, 1 -decene, 1- undecene, and 1-dodecene, wherein more preferably the alkene of formula (II) is optional- ly substituted 1 -nonene or 1 -decene, preferably 1 -nonene or 1 -decene, and more prefera- bly 1 -decene.

22. The process of any of embodiments 18 to 21 , wherein the carboxylic acid of formula (G) is selected from the group consisting of optionally substituted oxalic acid, malonic acid, suc- cinic acid, glutaric acid, adipic acid, pimelic acid, suberic acid, azelaic acid, sebacic acid, undecanedioic acid, and dodecanedioic acid, preferably from the group consisting of op- tionally substituted succinic acid, glutaric acid, adipic acid, pimelic acid, and suberic acid, wherein more preferably the carboxylic acid of formula (G) is optionally substituted glutaric or adipic acid, preferably glutaric or adipic acid, and more preferably adipic acid.

23. The process of any of embodiments 18 to 22, wherein the alkene : carboxylic acid molar ratio of the alkene of formula (II) to the carboxylic acid of formula (G) in the mixture (M1) prepared in (1 ) and reacted in (3) is in the range of from 0.1 : 1 to 20 : 1 , preferably from 0.5 : 1 to 15 : 1 , more preferably from 1 : 1 to 10 : 1 , more preferably from 1.3 : 1 to 5 : 1 , more preferably from 1.5 : 1 to 3 : 1 , more preferably from 1.7 : 1 to 2.5 : 1 , more prefera- bly from 1.9 : 1 to 2.3 : 1 , and more preferably from 1.95 : 1 to 2.1 : 1.

24. The process of any of embodiments 18 to 23, wherein the mixture (M1) prepared in (1) and reacted in (3) contains 50 wt.-% or less of water based on 100 wt.-% of the carboxylic acid of formula (I’), preferably 20 wt.-% or less, more preferably 10 wt.-% or less, more preferably 5 wt.-% or less, more preferably 1 wt.-% or less, more preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more prefera- bly 0.01 wt.-% or less, more preferably 0.005 wt.-% or less, more preferably 0.001 wt.-% or less, more preferably 0.0005 wt.-% or less, and more preferably 0.0001 wt.-% or less of water based on 100 wt.-% of the carboxylic acid of formula (I’). The process of any of embodiments 18 to 24, wherein the mixture (M1) prepared in (1) and reacted in (3) comprises 50 mol% or less of an alcohol of formula (IV)

based on 100 mol% of the carboxylic acid of formula (I’), preferably 20 mol% or less, more preferably 10 mol% or less, more preferably 5 mol% or less, more preferably 1 mol% or less, more preferably 0.5 mol% or less, more preferably 0.1 mol% or less, more preferably 0.05 mol% or less, more preferably 0.01 mol% or less, more preferably 0.005 mol% or less, more preferably 0.001 mol% or less, more preferably 0.0005 mol% or less, and more preferably 0.0001 mol% or less of an alcohol of the formula (IV) based on 100 mol% of the carboxylic acid of formula (G). The process of any of embodiments 18 to 25, wherein the mixture (M1) prepared in (1) and reacted in (3) contains 50 wt.% or less of elements and/or compounds other than the carboxylic acid of formula (G) and the alkene of formula (II) based on 100 wt.-% of the car- boxylic acid of formula (G), preferably 20 wt.-% or less, more preferably 10 wt.-% or less, more preferably 5 wt.-% or less, more preferably 1 wt.-% or less, more preferably 0.5 wt- % or less, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more preferably 0.01 wt.-% or less, more preferably 0.005 wt.-% or less, more preferably 0.001 wt.-% or less, more preferably 0.0005 wt.-% or less, and more preferably 0.0001 wt.-% or less of elements and/or compounds other than the carboxylic acid of formula (G) and the alkene of formula (II) based on 100 wt.-% of the carboxylic acid of formula (G). The process of any of embodiments 18 to 26, wherein the mixture (M1) prepared in (1) and reacted in (3) consists of a mixture of the carboxylic acid of formula (G) and the alkene of formula (II). The process of any of embodiments 18 to 27, wherein the contacting of the mixture (M1 ) with the catalyst in (3) is conducted at a temperature in the range of from 80 to 250°C, preferably from 100 to 230°C, more preferably from 110 to 210°C, more preferably from 120 to 200°C, more preferably from 130 to 190°C, more preferably from 140 to 180°C, more preferably from 145 to 175°C, more preferably from 150 to 170°C, and more prefer- ably in the range of from 155 to 165°C. The process of any of embodiments 18 to 28, wherein the process further comprises:

(5) separating the ester of formula (IN’) and/or (III”) from the reacted mixture (M2) for obtaining a mixture (M3) containing unreacted carboxylic acid of formula (G) and/or unre- acted alkene of formula (II). The process of embodiment 29, wherein the process further comprises:

(6) recycling the mixture (M3) containing unreacted carboxylic acid of formula (G) and/or unreacted alkene of formula (II) to (1). The process of any of embodiments 1 to 30, wherein R” is hydrogen or an optionally branched and/or optionally substituted and/or optionally unsaturated alkyl group selected from the group consisting of optionally branched and/or optionally substituted and/or op- tionally unsaturated C1-C6 alkyl groups, preferably C1-C5 alkyl groups, more preferably C1-C4 alkyl groups, more preferably C1-C3 alkyl groups, more preferably C1-C2 alkyl groups, and more preferably C1 alkyl groups, wherein more preferably R” is hydrogen or an alkyl group selected from the group consisting of optionally substituted methyl, ethyl, propyl, butyl, pentyl, and hexyl, more preferably from the group consisting of optionally substituted methyl, ethyl, propyl, butyl, and pentyl, more preferably from the group consist- ing of optionally substituted methyl, ethyl, propyl, and butyl, more preferably from the group consisting of optionally substituted methyl, ethyl, and propyl, wherein more prefera- bly R is hydrogen or optionally substituted methyl or ethyl, wherein more preferably R is hydrogen, methyl, or ethyl, wherein more preferably R” is hydrogen. The process of any of embodiments 1 to 31 , wherein in (2) and (3) the catalyst in the reac- tor contains 200 wt.% or less of elements and/or compounds other than the zeolitic mate- rial having a BEA-type framework structure based on 100 wt.-% of the zeolitic material having a BEA-type framework structure, preferably 100 wt.-% or less, more preferably 50 wt.-% or less, more preferably 20 wt.-% or less, more preferably 10 wt.-% or less, more preferably 5 wt.-% or less, more preferably 1 wt.-% or less, more preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more prefera- bly 0.01 wt.-% or less, more preferably 0.005 wt.-% or less, more preferably 0.001 wt.-% or less, more preferably 0.0005 wt.-% or less, and more preferably 0.0001 wt.-% or less of elements and/or compounds other than the zeolitic material having a BEA-type framework structure based on 100 wt.-% of the zeolitic material having a BEA-type framework struc- ture. The process of any of embodiments 1 to 32, wherein in (2) and (3) the zeolitic material having a BEA-type framework structure comprised in the catalyst is in the H-form. The process of any of embodiments 1 to 33, wherein in (2) and (3) the zeolitic material having a BEA-type framework structure comprised in the catalyst contains 5 wt.-% or less of a metal AM calculated as the element and based on 100 wt.-% of YO ₂ contained in the framework structure of the zeolitic material having a BEA-type framework structure, pref- erably 1 wt.-% or less, more preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more preferably 0.01 wt.-% or less, more prefer- ably 0.005 wt.-% or less, more preferably 0.001 wt.-% or less, more preferably 0.0005 wt- % or less, and more preferably 0.0001 wt.-% or less of a metal AM calculated as the ele- ment and based on 100 wt.-% of Y0 ₂ contained in the framework structure of the zeolitic material having a BEA-type framework structure,

wherein the metal AM stands for Na, preferably for Na and K, more preferably for alkali metals, and more preferably for alkali and alkaline earth metals.

35. The process of any of embodiments 1 to 34, wherein in (2) and (3) the zeolitic material having a BEA-type framework structure comprised in the catalyst contains 5 wt.-% or less of a metal TM calculated as the element and based on 100 wt.-% of YO ₂ contained in the framework structure of the zeolitic material having a BEA-type framework structure, pref- erably 1 wt.-% or less, more preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more preferably 0.01 wt.-% or less, more prefer- ably 0.005 wt.-% or less, more preferably 0.001 wt.-% or less, more preferably 0.0005 wt- % or less, and more preferably 0.0001 wt.-% or less of a metal TM calculated as the ele- ment and based on 100 wt.-% of YO ₂ contained in the framework structure of the zeolitic material having a BEA-type framework structure,

wherein the metal TM stands for Pt, Pd, Rh, and Ir, and preferably stands for transition metal elements of groups 3-12.

36. The process of any of embodiments 1 to 35, wherein in (2) and (3) the catalyst in the reac- tor contains 5 wt.-% or less of a metal AM calculated as the element and based on 100 wt.-% of the catalyst, preferably 1 wt.-% or less, more preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more preferably 0.01 wt.- % or less, more preferably 0.005 wt.-% or less, more preferably 0.001 wt.-% or less, more preferably 0.0005 wt.-% or less, and more preferably 0.0001 wt.-% or less of a metal AM calculated as the element and based on 100 wt.-% of the catalyst,

wherein the metal AM stands for Na, preferably for Na and K, more preferably for alkali metals, and more preferably for alkali and alkaline earth metals.

37. The process of any of embodiments 1 to 36, wherein in (2) and (3) the catalyst contained in the reactor contains 5 wt.-% or less of a metal TM calculated as the element and based on 100 wt.-% of the catalyst, preferably 1 wt.-% or less, more preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more preferably 0.01 wt.-% or less, more preferably 0.005 wt.-% or less, more preferably 0.001 wt.-% or less, more preferably 0.0005 wt.-% or less, and more preferably 0.0001 wt.-% or less of a metal TM calculated as the element and based on 100 wt.-% of the catalyst,

wherein the metal TM stands for Pt, Pd, Rh, and Ir, and preferably stands for transition metal elements of groups 3-12.

38. The process of any of embodiments 1 to 37, wherein in (2) and (3) the zeolitic material having a BEA-type framework structure comprised in the catalyst contains 5 wt.% or less of phosphorous calculated as the element and based on 100 wt.-% of YO ₂ contained in the framework structure of the zeolitic material having a BEA-type framework structure, preferably 1 wt.-% or less, more preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more preferably 0.01 wt.-% or less, more prefer- ably 0.005 wt.-% or less, more preferably 0.001 wt.-% or less, more preferably 0.0005 wt- % or less, and more preferably 0.0001 wt.-% or less of phosphorous calculated as the el- ement and based on 100 wt.-% of YO ₂ contained in the framework structure of the zeolitic material having a BEA-type framework structure.

39. The process of any of embodiments 1 to 38, wherein in (2) and (3) the catalyst contains 5 wt.% or less of phosphorous calculated as the element and based on 100 wt.-% of the catalyst, preferably 1 wt.-% or less, more preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more preferably 0.01 wt.-% or less, more preferably 0.005 wt.-% or less, more preferably 0.001 wt.-% or less, more preferably 0.0005 wt.-% or less, and more preferably 0.0001 wt.-% or less of a metal AM calculated as the element and based on 100 wt.-% of the catalyst.

40. The process of any of embodiments 1 to 39, wherein the contacting of the mixture (M1) with the catalyst in (3) is conducted at a pressure in the range of from 2 to 50 bar, prefer- ably from 3 to 30 bar, more preferably from 4 to 25 bar, more preferably from 5 to 20 bar, more preferably from 6 to 17 bar, more preferably from 7 to 15 bar, more preferably from 7.5 to 13 bar, more preferably from 8 to 12 bar, more preferably from 8.5 to 11.5 bar, more preferably from 9 to 11 bar, and more preferably in the range of from 9.5 to 10.5 bar.

41. The process of any of embodiments 1 to 40, wherein the duration of the contacting of the mixture (M1 ) with the catalyst in (3) is in the range of from 0.05 to 12 h, preferably from 0.1 to 9 h, more preferably from 0.25 to 8 h, more preferably from 0.5 to 7.5 h, more pref- erably from 1 to 7 h, more preferably from 1.5 to 6.5 h, more preferably from 2 to 6 h, more preferably from 2.5 to 5.5 h, more preferably from 3 to 5 h, more preferably from 3.5 to 4.5 h, and more preferably in the range of from 3.75 to 4.25 h.

42. The process of any of embodiments 1 to 41 , wherein the contacting of the mixture (M1) with the catalyst in (3) and the collecting of the reacted mixture (M2) in (4) is conducted in a continuous mode and/or in a batch mode, preferably in a continuous mode.

43. The process of any of embodiments 1 to 42, wherein the process is conducted in a con- tinuous mode and/or in a batch mode, preferably in a continuous mode.

44. The process of any of embodiments 1 to 43, wherein the process is conducted in a con- tinuous mode at a weight hourly space velocity (WHSV) in the range of from 0.08 to 20 h- 1, preferably from 0.09 to 15 h- ¹ , more preferably from 0.1 to 10 h ¹ , more preferably from 0.12 to 8 h ¹ , more preferably from 0.14 to 5 h ¹ , more preferably from 0.16 to 3 h ¹ , more preferably from 0.18 to 1 IT ¹ , more preferably from 0.2 to 0.5 IT ¹ , more preferably from 0.22 to 0.3 IT ¹ , and more preferably in the range of from 0.24 to 0.26 IT ¹ . The process of any of embodiments 1 to 44, wherein the zeolitic material having a BEA- type framework structure comprised in the catalyst displays a YO ₂ : X ₂ O ₃ molar ratio in the range of from 2 to 300, preferably from 4 to 200, more preferably from 6 to 150, more preferably from 8 to 100, more preferably from 12 to 70, more preferably from 14 to 50, more preferably from 16 to 40, more preferably from 18 to 35, more preferably from 20 to 30, and more preferably from 22 to 26. The process of any of embodiments 1 to 45, wherein the tetravalent element Y of the zeo- litic material having a BEA-type framework structure comprised in the catalyst is selected from the group consisting of Si, Sn, Ti, Zr, Ge, and a mixture of two or more thereof, Y preferably being Si. The process of any of embodiments 1 to 46, wherein the trivalent element X of the zeolitic material having a BEA-type framework structure comprised in the catalyst is selected from the group consisting of Al, B, In, Ga, and a mixture of two or more thereof, X preferably being Al. The process of any of embodiments 1 to 47, wherein the zeolitic material having a BEA- type framework structure comprised in the catalyst has a total amount of acid sites in the range of from 0.25 to 1.0 mmol/g, preferably from 0.15 to 0.8 mmol/g, more preferably from 0.2 to 0.7 mmol/g, more preferably from 0.25 to 0.6 mmol/g, more preferably from 0.3 to 0.55 mmol/g, more preferably from 0.35 to 0.5 mmol/g, more preferably from 0.38 to 0.45 mmol/g, and more preferably from 0.4 to 0.42 mmol/g,

wherein the total amount of acid sites is defined as the total molar amount of desorbed ammonia per mass of the zeolitic material determined according to the temperature pro- grammed desorption of ammonia (NH3-TPD). The process of embodiment 48, wherein the zeolitic material having a BEA-type frame- work structure comprised in the catalyst has an amount of medium acid sites wherein the amount of medium acid sites is defined as the amount of desorbed ammonia per mass of the zeolitic material determined according to the temperature programmed desorption of ammonia (NH3-TPD) in the temperature range of from 250 to 500 °C, wherein the amount of medium acid sites is at least 40% of the total amount of acid sites, preferably from 42 to 90%, more preferably from 44 to 80%, more preferably from 46 to 75%, more preferably from 48 to 70%, more preferably from 50 to 65%, more preferably from 53 to 60%, and more preferably from 55 to 57% of the total amount of acid sites. 50. The process of embodiment 48 or 49, wherein the amount of medium acid sites is in the range of from 0.10 to 0.90 mmol/g, preferably from 0.12 to 0.7 mmol/g, more preferably from 0.14 to 0.5 mmol/g, more preferably from 0.16 to 0.4 mmol/g, more preferably from 0.18 to 0.3 mmol/g, more preferably from 0.2 to 0.26 mmol/g, and more preferably from 0.22 to 0.24 mmol/g.

51. The process of any of embodiments 48 to 50, wherein the amount of strong acid sites of the zeolitic material having a BEA-type framework structure comprised in the catalyst de- fined as the amount of desorbed ammonia per mass of the zeolitic material determined according to the temperature programmed desorption of ammonia (NH ₃ -TPD) in the tem- perature range above 500 °C is in the range of from 0 to 0.10 mmol/g, preferably from 0.00 to 0.07 mmol/g, more preferably from 0.00 to 0.05 mmol/g, more preferably from 0.00 to 0.04 mmol/g, more preferably from 0.00 to 0.03 mmol/g, more preferably from 0.00 to 0.02 mmol/g, more preferably from 0.00 to 0.015 mmol/g, more preferably from 0.00 to 0.01 mmol/g, and more preferably from 0.00 to 0.005 mmol/g.

52. The process of any of embodiments 48 to 51 , wherein the ratio of the amount of medium acid sites relative to amount of strong acid sites is greater than 0, preferably 10 or greater, more preferably 50 or greater, more preferably 100, more preferably 10 ³ or greater, more preferably 10 ⁴ or greater, more preferably 10 ⁵ or greater, more preferably 10 ⁶ or greater, more preferably 10 ⁷ or greater, more preferably 10 ⁸ or greater, and more preferably 10 ⁹ or greater.

53. The process of any of embodiments 1 to 52, wherein the zeolitic material having a BEA- type framework structure comprised in the catalyst is obtainable and/or obtained accord- ing to an organotemplate-free synthetic process.

54. The process of embodiment 53, the organotemplate-free synthetic process comprising

(A) preparing a mixture comprising one or more sources for YO ₂ , one or more sources for X ₂ O ₃ , and seed crystals, the seed crystals comprising one or more zeolitic materials having a BEA-type framework structure;

(B) crystallizing the mixture obtained in (A) for obtaining a zeolitic material having a BEA-type framework structure;

wherein Y is a tetravalent element, and X is a trivalent element, and

wherein the mixture prepared in (A) and crystallized in (B) does not contain an organo- template as structure-directing agent.

55. The process of embodiment 54, wherein in the mixture prepared in (A) and crystallized in (B) contains 5 wt.-% or less of carbon calculated as the element and based on 100 wt.-% of Y contained in the mixture, preferably 1 wt.-% or less, more preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more prefera- bly 0.01 wt.-% or less, more preferably 0.005 wt.-% or less, more preferably 0.001 wt.-% or less, more preferably 0.0005 wt.-% or less, and more preferably 0.0001 wt.-% or less of carbon calculated as the element and based on 100 wt.-% of Y contained in the mixture.

56. The process of embodiment 54 or 55, wherein the zeolitic material having a BEA-type framework structure obtained in (B) comprises one or more alkali metals M, wherein M is preferably selected from the group consisting of Li, Na, K, Cs, and combinations of two or more thereof, more preferably from the group consisting of Li, Na, K, and combinations of two or more thereof, wherein more preferably the alkali metal M is Na and/or K, more preferably Na.

57. The process of any of embodiments 54 to 56, wherein the molar ratio M : YO ₂ in the mix- ture prepared in (A) and crystallized in (B) is in the range of from 0.05 to 5, preferably from 0.1 to 2, more preferably from 0.3 to 1 , more preferably from 0.4 to 0.8, more preferably from 0.45 to 0.7, more preferably from 0.5 to 0.65, and more preferably from 0.55 to 0.6.

58. The process of any of embodiments 54 to 57, wherein Y is selected from the group con- sisting of Si, Sn, Ti, Zr, Ge, and a mixture of two or more thereof, Y preferably being Si.

59. The process of any of embodiments 54 to 58, wherein the one or more sources for YO ₂ contained in the mixture prepared in (A) and crystallized in (B) comprises one or more sil icates, preferably one or more alkali metal silicates, wherein the alkali metal is prefer ably selected from the group consisting of Li, Na, K, Rb, and Cs, wherein more prefer ably the alkali metal is Na and/or K, and wherein more preferably the alkali metal is Na, wherein more preferably the one or more sources for Y0 ₂ contained in the mixture prepared in (A) and crystallized in (B) comprises water glass, preferably sodium and/or potassium silicate, more preferably sodium silicate.

60. The process of any of embodiment 59, wherein the one or more sources for YO ₂ con- tained in the mixture prepared in (A) and crystallized in (B) further comprises one or more silicas, preferably one or more silica hydrosols and/or one or more colloidal silicas, and more preferably one or more colloidal silicas.

61. The process of any of embodiments 54 to 60, wherein X is selected from the group con- sisting of Al, B, In, Ga, and a mixture of two or more thereof, X preferably being Al.

62. The process of any of embodiments 54 to 61 , wherein the one or more sources for X ₂ O ₃ contained in the mixture prepared in (A) and crystallized in (B) comprises one or more aluminate salts, preferably an aluminate of an alkali metal, wherein the alkali metal is preferably selected from the group consisting of Li, Na, K, Rb, and Cs, wherein more preferably the alkali metal is Na and/or K, and wherein more preferably the alkali met al is Na.

63. The process of any of embodiments 54 to 62, wherein the molar ratio YO ₂ : X ₂ O ₃ of the mixture prepared in (A) and crystallized in (B) is in the range of from 1 to 200, preferably from 5 to 100, more preferably from 10 to 50, more preferably from 15 to 40, more preferably from 20 to 30, more preferably from 23 to 25, and more preferably from

23.5 to 24.

64. The process of any of embodiments 54 to 63, wherein the amount of seed crystals corn- prised in the mixture prepared in (A) and crystallized in (B) is in the range of from 0.1 to 30 wt.-% based on 100 wt.-% of the one or more sources of YO ₂ in the mixture, calculated as YO ₂ , preferably from 0.5 to 20 wt.-%, more preferably from 1 to 10 wt.-%, more preferably from 1.5 to 5 wt.-%, more preferably from 2 to 4 wt.-%, and more preferably from 2.5 to

3.5 wt.-%.

65. The process of any of embodiments 54 to 64, wherein the mixture prepared in (A) and crystallized in (B) further comprises one or more solvents, wherein said one or more sol- vents preferably comprises water, more preferably deionized water, wherein more prefer- ably water is employed as the solvent further comprised in the mixture prepared in (A) and crystallized in (B), preferably deionized water.

66. The process of embodiment 65, wherein the molar ratio H ₂ 0 : YO ₂ of the mixture prepared in (A) and crystallized in (B) is in the range of from 5 to 100, preferably from 10 to 50, more preferably from 13 to 30, more preferably from 15 to 20, and more preferably from 17 to 18.

67. The process of any of embodiments 54 to 66, wherein the crystallization in (B) involves heating of the mixture, preferably at a temperature in the range of from 80 to 200°C, more preferably from 90 to 180°C, more preferably from 100 to 160°C, more prefera bly from 1 10 to 140°C, and more preferably from 115 to 130°C.

68. The process of any of embodiments 54 to 67, wherein the crystallization in (B) is conduct- ed under autogenous pressure, preferably under solvothermal conditions, and more pref- erably under hydrothermal conditions.

69. The process of embodiment 67 or 68, wherein in (B) the mixture is heated for a period in the range of from 5 to 200 h, preferably from 20 to 160 h, more preferably from 60 to 140 h, and more preferably from 100 to 130 h. 70. The process of any of embodiments 54 to 69, wherein the organotemplate-free synthetic process for the preparation of the zeolitic material having a BEA-type framework structure further comprises

(C) isolating the zeolitic material having a BEA-type framework structure obtained in (B), preferably by filtration; and

(D) optionally washing the zeolitic material having a BEA-type framework structure ob- tained in (B) or (C), preferably in (C); and/or,

(E) optionally drying the zeolitic material having a BEA-type framework structure ob- tained in (B), (C) or (D), preferably in (D);

wherein the steps (C) and/or (D) and/or (E) can be conducted in any order, and wherein one or more of said steps is preferably repeated one or more times.

71. The process of embodiment 70, wherein the organotemplate-free synthetic process for the preparation of the zeolitic material having a BEA-type framework structure further corn- prises

(F) exchanging one or more of the ionic non-framework elements contained in the zeo- litic material having a BEA-type framework structure obtained in (C), (D), or (E), preferably in (E), against H ⁺ and/or NH ₄ ⁺ , preferably against NH ₄ ⁺ ; and/or, preferably and

(G) drying and/or calcining, preferably drying and calcining the zeolitic material having a BEA-type framework structure obtained in (C), (D), (E), or (F).

72. The process of embodiment 70 or 71 , wherein the organotemplate-free synthetic process for the preparation of the zeolitic material having a BEA-type framework structure further comprises

(H) treating the zeolitic material having a BEA-type framework structure obtained in (C), (D), (E), (F), or (G), preferably in (G), with an aqueous solution having a pH of at most 5; and

(I) isolating the zeolitic material having a BEA-type framework structure obtained in (H), preferably by filtration; and/or,

(J) optionally washing the zeolitic material having a BEA-type framework structure ob- tained in (H) or (I), preferably in (I); and/or,

(K) optionally drying and/or calcining, preferably drying and calcining the zeolitic materi- al having a BEA-type framework structure obtained in (H), (I), or (J), preferably in (J); wherein the steps (I) and/or (J) and/or (K) can be conducted in any order, and

wherein one or more of said steps is preferably repeated one or more times.

73. The process of embodiment 72, wherein the pH of the aqueous solution used for treating the zeolitic material in (H) has a pH in the range of from -1 to 4.5, preferably of from -0.5 to 4, more preferably of from -0.2 to 3.5, more preferably of from -0.15 to 3, more prefera- bly of from -0.1 to 2.5, more preferably of from -0.05 to 2, more preferably of from 0 to 1.5, more preferably of from 0.05 to 1 , more preferably of from 0.1 to 0.5, and more preferably of from 0.15 to 0.25. 74. The process of embodiment 72 or 73, wherein in (H) the zeolitic material is added to the aqueous solution, and the mixture is heated, preferably at a temperature in the range of from 30 to 100°C, more preferably from 35 to 90°C, more preferably from 40 to 80°C, more preferably from 45 to 75°C, more preferably from 50 to 70°C, and more preferably from 55 to 65°C.

75. The process of any of embodiments 72 to 74, wherein in (H) the mixture is heated for a period in the range of from 0.1 to 10 h, preferably from 0.1 to 7 h, more preferably from 0.5 to 5 h, more preferably from 0.5 to 4.5 h, more preferably from 1 to 4 h, more prefera- bly from 1 to 3.5 h, more preferably from 1.5 to 3 h, and more preferably from 1.5 to 2.5 h.

76. The process of any of embodiments 72 to 75, wherein the organotemplate-free synthetic process for the preparation of the zeolitic material having a BEA-type framework structure further comprises

(L) treating the zeolitic material obtained in (H), (I), (J), or (K), preferably in (K), with a liquid aqueous system having a pH in the range of from 5.5 to 8 and a temperature of at least 75°C; and/or,

(M) optionally washing the zeolitic material having a BEA-type framework structure ob- tained in (L); and/or,

(N) optionally drying the zeolitic material having a BEA-type framework structure ob- tained in (L) or (M), preferably in (M);

wherein the steps (M) and (N) can be conducted in any order, and

wherein one or more of said steps is preferably repeated one or more times.

77. The process of embodiment 76, wherein the pH of the liquid aqueous system used for treating the zeolitic material in (L) has a pH in the range of from 5.5 to 12, preferably from

5.5 to 10, more preferably from 6 to 9, more preferably from 6 to 8.5, more preferably from

6.5 to 8, and more preferably from 6.5 to 7.5.

78. The process of embodiment 76 or 77, wherein in (L) the zeolitic material is added to the liquid aqueous system, and the mixture is heated, preferably at a temperature in the range of from 40 to 100°C, preferably of from 50 to 100°C, more preferably of from 60 to 100°C, more preferably of from 65 to 95°C, more preferably of from 70 to 95°C, more preferably of from 75 to 95°C, more preferably of from 80 to 90°C, and more preferably of from 85 to 90°C.

79. The process of any of embodiments 76 to 78, wherein in (L) the mixture is heated for a period in the range of from 1 to 40 h, preferably from 3 to 30 h, more preferably from 5 to 25 h, more preferably from 6 to 20 h, more preferably from 7 to 15 h, more preferably from

7.5 to 12 h, more preferably from 8 to 10 h, and more preferably from 8.5 to 9.5 h. 80. The process of any of embodiments 76 to 79, wherein in (L) the liquid aqueous system comprises water, preferably deionized water, wherein more preferably the liquid aqueous system is water, preferably deionized water.

81. The process of any of embodiments 76 to 80, wherein (H) and (L), preferably (H), (I), and

(L), more preferably (H), (I), (K), and (L), and more preferably (H), (I), (J), (K), (L), (M), and

(N) are repeated one or more times, preferably one to five times, more preferably two to four times, and more preferably three times.

82. The process of any of embodiments 76 to 81 , wherein the organotemplate-free synthetic process for the preparation of the zeolitic material having a BEA-type framework structure further comprises

(O) treating the zeolitic material having a BEA-type framework structure obtained in (L),

(M), or (N), preferably in (N), with an aqueous solution having a pH of at most 3; and

(P) isolating the zeolitic material having a BEA-type framework structure obtained in (O), preferably by filtration; and/or,

(Q) optionally washing the zeolitic material having a BEA-type framework structure ob- tained in (O) or (P), preferably in (P); and/or,

(R) optionally drying and/or calcining, preferably drying and calcining the zeolitic materi- al having a BEA-type framework structure obtained in (O), (P), or (Q), preferably in (Q); wherein the steps (P) and/or (Q) and/or (R) can be conducted in any order, and

wherein one or more of said steps is preferably repeated one or more times.

83. The process of embodiment 82, wherein the pH of the aqueous solution used for treating the zeolitic material in (O) has a pH in the range of from -2 to 2, preferably from -1.5 to 1 , more preferably from -1 to 0, more preferably from -0.7 to -0.1 , more preferably from -0.5 to -0.3, and more preferably from -0.45 to -0.35.

84. The process of embodiment 82 or 83, wherein in (O) the zeolitic material is added to the aqueous solution, and the mixture is heated, preferably at a temperature in the range of from 30 to 100°C, more preferably from 35 to 90°C, more preferably from 40 to 80°C, more preferably from 45 to 75°C, more preferably from 50 to 70°C, and more preferably from 55 to 65°C.

85. The process of any of embodiments 82 to 84, wherein in (O) the mixture is heated for a period in the range of from 0.1 to 10 h, preferably from 0.1 to 7 h, more preferably from 0.5 to 5 h, more preferably from 0.5 to 4.5 h, more preferably from 1 to 4 h, more prefera- bly from 1 to 3.5 h, more preferably from 1.5 to 3 h, and more preferably from 1.5 to 2.5 h.

86. The process of any of embodiments 82 to 85, wherein in (H) and/or (O), preferably in (H) and (O), the aqueous solution comprises a mineral acid, preferably a mineral acid select- ed from the list consisting of HF, HCI, HBr, HNO3, H3PO4, H2SO4, H3BO3, HCIO4, and mix- tures of two or more thereof, more preferably from the list consisting of HCI, HBr, HNO ₃ , H ₂ SO ₄ , HCIO ₄ , and mixtures of two or more thereof, more preferably from the list consist- ing of HCI, HNO ₃ , H ₂ SO ₄ , and mixtures of two or more thereof, wherein more preferably the aqueous solution comprises HCI and/or HNO ₃ , preferably HNO ₃ . The process of any of embodiments 70 to 86, wherein drying in (E) and/or (G) and/or (K) and/or (N) and/or (R), preferably in (E), (G), (K), (N), and (R) is conducted at a tempera- ture in the range of from 80 to 200°C, more preferably from 90 to 180°C, more preferably from 100 to 160°C, more preferably from 1 10 to 140°C, and more preferably from 1 15 to 130°C. The process of any of embodiments 70 to 87, wherein drying in (E) and/or (G) and/or (K) and/or (N) and/or (R), preferably in (E), (G), (K), (N), and (R) is conducted for a period in the range of from 1 to 120 h, preferably from 5 to 96 h, more preferably from 8 to 72 h, more preferably from 10 to 60 h, more preferably from 12 to 48 h, more preferably from 14 to 42 h, more preferably from 16 to 36 h, more preferably from 18 to 30 h, more preferably from 20 to 24 h, and more preferably from 21 to 23 h. The process of any of embodiments 71 to 88, wherein calcining in (G) and/or (K) and/or (R), preferably in (G), (K) and (R) is conducted at a temperature in the range of from 250 to 1 ,000°C, preferably from 300 to 900°C, more preferably from 350 to 850°C, more pref- erably from 400 to 800°C, more preferably from 450 to 750°C, more preferably from 500 to 700°C, and more preferably from 550 to 650°C. The process of any of embodiments 71 to 89, wherein calcining in (G) and/or (K) and/or (R), preferably in (G), (K) and (R) is conducted for a period in the range of from 0.5 to 36 h, more preferably from 1 to 24 h, more preferably from 1.5 to 18 h, more preferably from 2 to 12 h, more preferably from 2.5 to 9 h, more preferably from 3 to 7 h, more preferably from 3.5 to 6.5 h, more preferably from 4 to 6 h, and more preferably from 4.5 to 5.5 h. The process of any of embodiments 54 to 90, wherein the zeolitic material having a BEA- type framework structure formed in (B) comprises zeolite beta. The process of any of embodiments 54 to 91 , wherein the seed crystals contained in the mixture prepared in (A) and crystallized in (B) comprise a zeolitic material having a BEA- type framework structure, preferably zeolite beta, and more preferably a zeolitic material having a BEA-type framework structure as obtainable and/or obtained according to the organotemplate-free synthetic process for the preparation of the zeolitic material having a BEA-type framework structure as defined in any of embodiments 48 to 65. DESCRIPTION OF THE FIGURES

Figure 1 displays the X-ray diffraction pattern (measured using Cu K alpha-1 radiation) of the zeolitic material obtained according to Reference Example 1. In the figure, the angle 2 theta in ° is shown along the abscissa and the intensities are plotted along the or- dinate.

Figure 2 shows the results from catalytic testing with regard to the yield in isopropyl myristate

(IPM) as obtained from Example 1 and Comparative Example 7. In the figure, the temperature in °C is shown along the abscissa and the yield in IPM in % plotted along the ordinate.

The present invention is further illustrated by the following reference examples, examples, and comparative examples.

EXAMPLES

X-ray diffraction

X-ray diffraction experiments on the powdered materials were performed using D8 Advance X- ray Diffractometer (Bruker AXS) equipped with a Lynx Eye detector using the Cu K alpha-1 ra- diation. In the experiment, the samples were lightly ground using a mortar and pestle and filled into flat sample holders with a 2mm x 20mm cavity. The surface was flattened using a glass plate. Cu-Ka radiation was used in a Bragg-Brentano geometry. Data was collected from 2- 50°(20) using a 0.02° step size and a dwell time of 2.4 seconds per step. The parameters used in the X-ray diffraction experiment were as follows:

Primary side: Divergence Slit, 0.1 ° with ASS

Secondary side : 0.1 fixed slit

Detector: Lynx Eye, 3°

Determination of the acid sites: Temperature programmed desorption of ammonia (NH3-TPD)

The temperature-programmed desorption of ammonia (NH ₃ -TPD) was conducted in an auto- mated chemisorption analysis unit (Micromeritics AutoChem II 2920) having a thermal conduc- tivity detector. Continuous analysis of the desorbed species was accomplished using an online mass spectrometer (OmniStar QMG200 from Pfeiffer Vacuum). The sample (0.1 g) was intro- duced into a quartz tube and analysed using the program described below. The temperature was measured by means of a Ni/Cr/Ni thermocouple immediately above the sample in the quartz tube. For the analyses, He of purity 5.0 was used. Before any measurement, a blank sample was analysed for calibration. 1. Preparation: Commencement of recording; one measurement per second. Wait for 10 minutes at 25 °C and a He flow rate of 30 cm ³ /min (room temperature (about 25 °C) and 1 atm); heat up to 600 °C at a heating rate of 20 K/min; hold for 10 minutes. Cool down under a He flow (30 cm ³ /min) to 100 °C at a cooling rate of 20 K/min (furnace ramp temperature); Cool down under a He flow (30 cm ³ /min) to 100 °C at a cooling rate of 3 K/min (sample ramp temperature).

2. Saturation with NH ₃ : Commencement of recording; one measurement per second.

Change the gas flow to a mixture of 10 % NH ₃ in He (75 cm ³ /min; 100 °C and 1 atm) at 100 °C; hold for 30 min.

3. Removal of the excess: Commencement of recording; one measurement per second. Change the gas flow to a He flow of 75 cm ³ /min (100 °C and 1 atm) at 100 °C; hold for 60 min.

4. NH ₃ -TPD: Commencement of recording; one measurement per second. Heat up under a He flow (flow rate: 30 cm ³ /min) to 600 °C at a heating rate of 10 K/min; hold for 30 min.

5. End of measurement.

Desorbed ammonia was measured by means of the online mass spectrometer, which demon- strated that the signal from the thermal conductivity detector was caused by desorbed ammo- nia. This involved utilizing the m/z = 16 signal from ammonia in order to monitor the desorption of the ammonia. The amount of ammonia adsorbed (mmol/g of sample) was ascertained by means of the Micromeritics software through integration of the TPD signal with a horizontal baseline.

Reference Example 1 : Organotemplate-free synthesis of zeolite beta a) Preparation of a zeolite having BEA framework structure (H-beta zeolite) a1) 335.1 g of NaAI0 ₂ (4.09 moles) were dissolved in 7314 g of H ₂ O (406 moles) while stir- ring, followed by addition of 74.5 g of zeolite Beta seeds (commercially available from Ze- olyst International, Valley Forge, PA 19482, USA, under the tradename CP814C, CAS Registry Number 1318-02-1 , which was converted to the H-form by calcination at 550°C for 5 h, wherein a heat ramp of 1 °C/min was used for attaining the calcination tempera- ture). The mixture was placed in a 20 L autoclave and 7340 g sodium waterglass solution (26 wt.-% S1O ₂ and 8 wt.-% Na ₂ 0) and 1436 g Ludox® AS40 (9.5 moles) were added af- fording an aluminosilicate gel with a molar ratio of 1.00 S1O ₂ : 0.0421 Al ₂ 0 ₃ : 0.285 Na ₂ 0 : 17.48 H ₂ O. The reaction mixture was heated in 3 h to a temperature of 120 °C using a constant heat ramp, wherein said temperature was then maintained 117 h. After having let the reaction mixture cool to room temperature, the solid was separated by filtration, re- peatedly washed with distilled water and then dried at 120 °C for 16 h. a2) 1000 g zeolitic material prepared according to a1) were added to 10 g of a 10 weight-% solution of ammonium nitrate. The suspension was heated to 80 °C and kept at this tem- perature under continuous stirring for 2h. The solid was filtered hot (without additional cooling) over a filter press. The filter cake was then washed with distilled water (room temperature wash water) until the conductivity of the wash water was below 200 mi- croSiemens/cm. The filter cake was dried for 16 h at 120 °C. This procedure was repeated once, affording ion exchanged crystalline product BEA in its ammonium form. A following calcination step at 500 °C for 5 h (heat ramp 1 K/min) afforded ion exchanged crystalline product BEA in its H-form. b) First acidic dealumination Materials used:

17.15 kg H-beta-Zeolite according to a): Si = 34 %; Al = 6.3 %; Na 0.07 %.

51.45 kg HN03 solution (4 %)

A stirred vessel was charged with 51.45 kg of a solution of HNO ₃ (4 weight-%). 17.15 kg of H-beta zeolite were added. The obtained suspension was stirred at 60 °C for 2 h. After cooling to 50 °C, the suspension was transferred to a filter press, filtered with a pressure of 3.2 bar and washed for 9 h with 5,484 L of distilled water. The zeolite was dried for 20 h at 120 °C. 15.912 kg of zeolite were obtained. This zeolite was calcined in a recirculated muffle furnace by raising the temperature at a rate of 1 K/min to 600 °C for 5 h. 15.889 kg of a white solid were obtained. Elementary analysis: Si = 35.5 %; Al = 4.9 %; Na = 0.05 %. c) Water treatment Materials used:

15.889 kg acid treated H-beta-zeolite

127 kg distilled H ₂ O

The zeolite was suspended in a vessel in distilled water. The suspension was heated to 90 °C and stirred for 9 h. The suspension was filtered off on a filter press and dried. The drying was carried out at 120 °C for 68 h. 15.547 kg of H-beta-zeolite were obtained. d) Second acidic dealumination Materials used:

15.538 kg H-beta zeolite of c)

46.614 kg HNOs (aq.; 4 weight-%)

A vessel was charged with 46.614 kg of a solution of HNO ₃ (4 weight-%). 1 5.538 kg of the H-beta zeolite were added. The obtained suspension was stirred at 60 °C for 2 h. Af- ter cooling to 50 °C, the suspension was transferred to a filter press, filtered with a pres- sure of 3.2 bar and washed for 3.5 h with 2,1 14 L of distilled water. The zeolite was dried for 48 h at 120 °C. 14.14 kg of zeolite were obtained. This zeolite was calcined in a recir- culated muffle furnace with the raising the temperature at a rate of 1 K/min to 600 °C for 5 h. 14.479 kg of a white solid (H-beta zeolite were obtained. Elementary analysis: Si = 37.5 %; Al = 3.8 %; Na = 0.03 % . e) Water treatment Materials used:

14.479 kg H-beta zeolite of d)

116 kg distilled hhO-dest.

14.479 kg of H-beta zeolite of were suspended in a vessel in distilled water. The solution was heated to 90 °C and stirred for 9 h. The suspension was filtered off on a filter press and dried. The drying was carried out at 120 °C for 22 h. 14.65 kg of H-beta zeolite were obtained. f) Third acidic dealumination Materials used:

13.65 kg H-beta zeolite of e)

40.95 kg HNO ₃ (aq., 4 weight-%)

A vessel was charged with 40.95 kg of a solution of HNO ₃ (4 weight-%). 13.65 kg of H- beta zeolite of e) were added. The obtained suspension was stirred at 60 °C for 2 h. After cooling to 50 °C, the suspension was transferred to a filter press, filtered with a pressure of 3.2 bar and washed for 16.5 h with 1 ,442 L of distilled water. The zeolite was dried for 68 h at 120 °C. 12.658 kg of zeolite were obtained. This zeolite was calcined in a recircu- lated muffle furnace by raising the temperature at a rate of 1 K/min to 600 °C for 5 h. 12.83 kg of a white solid were obtained. Elementary analysis: Si = 37.5 %; Al = 3.8 %; Na = 0.03 %. g) Water treatment

Materials used:

12.82 kg H-beta zeolite of f)

103 kg distilled H ₂ 0

12.82 kg of H-beta zeolite of f) were suspended in a vessel in distilled water. The sus- pension was heated to 90 °C and stirred for 9 h. The suspension was filtered off on a filter press and dried. The drying was carried out at 120 °C for 22 h. 12.73 kg of H-beta zeolite were obtained. h) Fourth Acidic dealumination Materials used:

12.72 kg H-beta zeolite of g)

38.16 kg HNO ₃ (aq., 8 weight-%)

A vessel was charged with 38.16 kg of an aqueous solution of HNO ₃ (8 %). 12.72 kg of H- beta zeolite of g) were added. The obtained suspension was stirred at 60 °C for 2 h. After cooling to 50 °C, the suspension was transferred to a filter press, filtered with a pressure of 3.2 bar and washed for 5 h with 1 ,055 I of distilled water. The zeolite was dried for 25 h at 120 °C. 11.802 kg of zeolite were obtained. This zeolite was calcined in a recirculated muffle furnace with raising the temperature at a rate of 1 K/min to 600 °C for 5 h. 11.852 kg of a white solid were obtained. Elementary analysis: Si = 42.0 %; Al = 1.8 %; Na < 0.01 %. i) Water treatment

Materials used:

11.842 kg H-beta zeolite of h)

95 kg distilled H ₂ O

11.842 kg of H-beta zeolite of h) were suspended in a vessel in distilled water. The sus- pension was heated to 90 °C and stirred for 9 h. The suspension was filtered off on a filter press and dried. The drying was carried out at 120 °C for 22 h. 11.512 kg of H-beta zeo- lite were obtained. j) Fifth Acidic Dealumination

Materials used:

11.502 kg H-beta zeolite of i)

34.506 kg HNO ₃ (aq., 15 weight-%)

A vessel was charged with 34.506 kg of an aqueous solution of HNO ₃ (15 weight-%).

11.502 kg of H-beta zeolite of i) were added. The obtained suspension was stirred at 60 °C for 2 h. After cooling to 50 °C, the suspension was transferred to a filter press, filtered with a pressure of 3.2 bar and washed for 2.25 h with 1 ,114 L of distilled water. The zeo- lite was dried for 24 h at 120 °C. This zeolite was calcined in a recirculated muffle furnace with raising the temperature at a rate of 1 K/min to 600 °C for 5 h. 11.097 kg of a white solid were obtained. The obtained zeolitic material has a crystallinity of 73% Elementary analysis: Si = 43.5 %; Al = 1.7 %; Na < 0.01 %.

Total amount of acid sites: 0.41 mmol/g, as determined according to the NH ₃ -TPD meth- od described above.

Total amount of medium acid sites: 0.23 mmol/g, as determined according to the NH ₃ - TPD method described above.

Total amount of strong acid sites: none detected according to the NH ₃ -TPD method de- scribed above.

The X-ray diffraction pattern of the dealuminated zeolite is shown in Figure 1 , and displays a pattern typical for the BEA framework type.

Reference Example 2: Commercial zeolite beta

The zeolitic material according to this Reference Example 2 is the zeolitic material CP814E as obtained from Zeolyst International. The zeolitic material CP814E has a molar Si:AI ratio of 12.5:1 (SiC> ₂ /Al ₂ C> ₃ molar ratio (SAR) = 25). Prior to use, this material was calcined in air at a temperature of 550 °C for 5 h, the heating rate to achieve this temperature was 2 K/min. Total amount of acid sites: 1.02 mmol/g, as determined according to the NH ₃ -TPD method de- scribed in Reference Example 1.1.

Total amount of medium acid sites: none detected according to the NH ₃ -TPD method described in Reference Example 1.1.

Total amount of strong acid sites: 0.02 mmol/g, as determined according to the NH ₃ -TPD meth- od described in Reference Example 1.1.

Reference Example 3: Synthesis of Chabazite

276.8 kg L/,L/,/V-trimethylcyclohexylammoniumhydroxide (20 wt-% solution in H ₂ O) were mixed with 34.80 kg of aluminiumtriisopropylate and 77.99 kg tetramethylammonium hydroxide (25 wt- % solution in H ₂ 0). Afterwards, 358.32 kg of colloidal silica (LUDOX AS 40; 40wt-% colloidal solution in H ₂ 0) and 5.73 kg CHA seeds were added to the stirred mixture. The resulting gel was placed in a stirred autoclave with a total volume of 1600 L. The autoclave was heated with- in 7h to 170°C. The temperature was kept constant for 18h. Afterwards the autoclave was cooled down to room temperature. Then, the solids were separated by filtration and intensively washed until the wash-water had a pH of 7. Finally the solid was dried for 10 hours at 120°C. The material was then calcined at 550°C for 5 hours.

The characterization of the material via XRD confirmed the CHA-type framework structure of the product.

Reference Example 4: Synthesis of CS _2.5 H _0.5 PW ₁₂ O ₄₀

Solution 1 : 64 g CS ₂ CO ₃ (99%) in 310 g Water

Solution 2: 521.35 g H ₃ PW ₁₂ O ₄₀ xH ₂ 0 (14% H ₂ 0) in 1 126 g Water

First the solutions are prepared separately. The solution of the HPW is placed in a 2 I beaker with magnetic stirrer. Solution 1 is then added to solution 2 by means of a dropping funnel within of 40 minutes time, in which white precipitate forms. The resulting suspension is stirred over- night, after which the suspension is evaporated to dryness (25-30 mbar at 50°C) on a rotary evaporator; the resulting powder is dried in the drying cabinet at 100°C for 16 h and then pressed through a 0.5 mm filter. The product is then heated in a muffle furnace to 300 ⁰ C. with 2 K / min and heat treated for 3 h. The elemental analysis of the product showed 9.9 wt.-% Cs and 66.7 wt.-% W.

Example 1 : Catalyst Testing - Reaction of a monocarboxylic acid with an alkene

Screening tests were carried out in 8 parallel hastelloy autoclave reactors (inner volume 300 ml). The quantification of products has been done by GC Analysis. The general experimental procedure for each screening experiment was as follows: in a first step, a starting reaction mix- ture was prepared by filling the reactor with 116 g of the carboxylic acid myristic acid (0.508 moles), and 5 mol% of homogeneous acid catalyst (H ₂ SO ₄ ) based on 100 mol% or the mixture or 5 wt% heterogeneous acid catalyst based on 100 wt.-% of the mixture. The reactions were carried out without a solvent using pure myristic acid. In a second step, the hastelloy autoclave reactor (inner volume 300 ml) was tightly sealed and then pressurized with 10 bar of the alkene propylene. The mixture was heated to a temperature of 130°C while stirring at 2000 rpm. After the corresponding reaction temperature was reached, the reaction temperature was maintained for 4h, while continuing stirring the reaction mixture inside the heated and pressurized hastelloy autoclave reactor. The temperature of the reaction was 130°C and the propylene pressure kept constant at 10 bar by adding propylene continuously during the reaction. Subsequently, the steel autoclave reactor was allowed to cool down to approximately 70°C, to keep the myristic acid liquid the pressure was released and the hastelloy autoclave reactor was opened. The suspension was filtered, to remove all rests from the catalyst and 1 ml of the reaction mixture was subjected to a GC analysis.

Cesium phosphotungstate and several types of zeolites were chosen as solid acid catalysts for the catalytic testing. The starting catalyst concentration was 5 wt%. The list of all catalysts and details about their performance with regard to their selectivities for isopropyl myristate (I PM) are shown in the Table 1.

Table 1 : Results from catalytic testing with regard to the yield in isopropyl myristate.

( ^* ) obtained from Clariant

( ^** ) obtained from Zeolyst (CBV 720)

( ^*** ) obtained from Zeolyst (CBV 600)

As one can readily see from table 1 , only two of the examples gave above 75% yield of isopro- pyl myristate (IPM) (example 1 and comparative example 7). The other comparative examples on the other hand giving significantly reduced yields ranging from 0.17% to 45.1 %, thereby hav- ing far lower selectivities for isopropyl myristate (IPM).

Furthermore, the Example 1 and Comparative Example 7 catalysts were each then evaluated for prolonged reaction time as shown in Table 2. Table 2: Results from catalytic testing with regard to the yield in isopropyl myristate (Prolonged Reaction Time)

As one can readily see from Table 2, it was surprisingly found that Example 1 outperforms comparative example 7 over time, since after 17 hours the Example 1 catalyst continues to pro- vide improved yields of I PM, whereas the comparative Example 7 catalyst selectivity is decreas- ing over time. Accordingly, the Example 1 catalyst would be particularly beneficial when pro- longed reaction times are employed in a batch process. In this light, when a continuous process is carried out the performance of Example 1 would be superior over time compared to the com- parative example 7 catalyst.

In addition, said catalysts were tested at reaction temperatures ranging from 70 °C to 130 °C. Thus, as may be taken from Figure 2, it was surprisingly found that with the catalyst of Example 1 the yield of I PM increases with increasing temperature. To the contrary, when the catalyst of Comparative Example 7 was employed the yield of I PM continually decreases with increasing temperature, such that the catalyst of Example 1 outperforms the catalyst of Comparative Ex- ample 7 at higher temperatures. Accordingly, it has surprisingly been found that higher yields may be obtained when employing the inventive process at higher temperatures, which is of considerable advantage since this coincides with higher reaction rates which are achieved with increasing temperature.

Example 2: Catalyst Testing - Reaction of a decarboxylic acid with an alkene

Screening tests were carried out in round bottom flasks (inner volume 100 ml). The quantifica- tion of products was done by GC Analysis, in form of GC areas in percentage. The general ex- perimental procedure for each screening experiment was as follows: in a first step, a starting reaction mixture was prepared by filling the reactor with adipic acid, and 5 wt-% of acid catalyst. In a second step, the round bottom flask was heated to 160°C so the adipic acid was melted and in liquid state. The 1-decene was added slowly to the mixture of acid and catalyst via pump within 3 hours. The flow rate ml/min was dependent on the amount of 1-decene in the reaction. During the addition, the mixture was continuously heated to a temperature of 160°C while stir- ring at 300 rpm. After the whole amount of 1-decene was added, the reaction temperature was maintained for an additional hour, while continuing stirring the reaction mixture. Subsequently, the flask was allowed to cool down. The suspension from the whole reaction was sent to GC analysis. 12 batch reactions were performed in the lab. These include chemical validation, catalyst screening and olefin/acid ratio variation. Reaction conditions: 160°C // solvent free // olefin/acid ratio 2, 10 and 20. For the reaction two heterogeneous catalysts were evaluated:

CS _2.5 H _0.5 PW ₁₂ O ₄₀ from Reference Example 4 and zeolite beta from Reference Example 1 , and these were benchmarked against H ₂ SO ₄ . The GC analysis includes GC-areas measured for the ester and acid in the reaction mixture. Results show clear formation of mono- and

diisodecylester of the adipic acid as products. Regarding polymerization of the olefin, only the dimer eicosene can be observed in the reactions. Unreacted adipic acid could be found in the precipitate, so the representation of the results below includes only the filtrate mixture.

In the first set of experiments, the two heterogeneous catalysts CS _2.5 H _0.5 PW ₁₂ O ₄₀ from Refer- ence Example 4 and template-free zeolite beta from Reference Example 1 were evaluated against sulphuric acid under the mentioned conditions. The selectivity for formed products are shown in the Table 3.

Table 3: Screened heterogeneous catalysts (reaction conditions: 12 g Adipic acid / 31.1 ml 1- decene / 5 wt% catalyst / T 160°C / 3+1 h reaction time)

Thus, as may be taken from the results, it has surprisingly been found that a high selectivity towards the adipic acid monoester is achieved using zeolite beta according to Example 2, which clearly outperforms the use of the heteropolyacid in Comparative Example 9. In comparison, the use of sulfuric acid offers a very low selectivity towards the monoester, as may be taken from the results for Comparative Example 8.

In a second experiment, the reaction using the amount of the alkene educt was considerably increased, wherein the results using an olefin to alkene ratio of 10 is shown in Table 4, and the results using an olefin to alkene ratio of 20 is shown in Table 4. Table 4: Olefin : Acid ratio 10 (reaction conditions: 4 g Adipic acid / 51.9 ml 1-decene / 5 wt% catalyst I T 160°C / 3+1 h reaction time)

Table 5: Olefin : Acid ratio 20 (reaction conditions: 4 g Adipic acid / 103.80 ml 1-decene / 5 wt% catalyst / T 160°C / 3+1 h reaction time)

Thus, as may be taken from the results displayed in Tables 4 and 5, it has quite surprisingly been found that even when raising the ratio of alkene to acid by 10, the higher selectivity of zeo- lite beta from Reference Example 1 towards the monoester product is maintained. This is par- ticularly surprising since, as may be taken from Table 4, Comparative Example 10 displays a highly diminished selectivity for the heteropolyacid from Reference Example 4 compared to zeo- lite beta from Reference Example 1 in Example 4 when increasing the ratio of alkene to acid by 5. As may be taken from Table 5, on the other hand, Comparative Example 11 shows that the increase by 10 leads to a higher selectivity of the diester product, whereas the higher selectivity towards the monoester product is quite unexpectedly maintained for zeolite beta from Refer- ence Example 1 in Example 5 despite the very high concentration of the alkene educt in the reaction mixture.

List of the cited prior art references:

- US 5,189,201

- WO 2010/146156 A1