EP3752542A1

EP3752542A1 - Method for producing hydrocarbon resins and hydrogenation products thereof

Info

Publication number: EP3752542A1
Application number: EP19703754.2A
Authority: EP
Inventors: Jun Liu; Manuel NAU
Original assignee: Rain Carbon Germany GmbH
Current assignee: Rain Carbon Germany GmbH
Priority date: 2018-02-14
Filing date: 2019-02-14
Publication date: 2020-12-23
Also published as: CN111971314B; CN111971314A; RU2020129948A; CA3092183C; KR20200120662A; KR102556496B1; WO2019158638A1; JP2021514414A; TWI804576B; AR116070A1; US12077624B2; JP7133631B2; TW201938594A; BR112020016531B1; CA3092183A1; BR112020016531A2; RU2020129948A3; US20210189038A1

Abstract

The invention relates to a method for producing a hydrocarbon resin from at least one cyclic diolefin component and at least one ethylenically unsaturated aromatic component having 8 to 13 carbon atoms, in which method the monomer mixture is heated at a heating rate of 0.5 to 10°C/second to a polymerisation temperature of at least 180°C in order to obtain a hydrocarbon resin having a reduced proportion of by-products, the monomer mixture being substantially single-phase and liquid during the heating to at least 180°C and during the polymerisation, and the subsequently hydrogenated hydrocarbon resin exhibiting good compatibility with other constituents of hot-melt adhesives.

Description

Process for the preparation of hydrocarbon resins and their hydrogenation products

TECHNICAL FIELD OF THE INVENTION The invention relates to a process for preparing a hydrocarbon resin from at least one cyclic diolefin component and at least one ethylenically unsaturated aromatic component, hydrogenation thereof and the hydrogenation products.

TECHNICAL BACKGROUND OF THE INVENTION

Hydrocarbon resins are often used as tackifiers in hot melt adhesives. Of particular interest are bright as possible hot glue with good processing properties. Essential for good processing properties of the hot melt adhesive are high compatibility of tackifier and base polymer. To produce bright and easily processable hot-melt adhesives, it is important that the at least partially hydrogenated hydrocarbon resins used for this purpose are as free as possible from unwanted by-products. These can lead to dark discolorations in the hydrocarbon resin and incompatibilities with other components of a hot-melt adhesive. To assess discolorations, the Gardner, Yellowness Index or Hazen color number is often used. The compatibility of the components of the hot melt adhesive is assessed by the determination of the cloud point.

Processes for the preparation of hydrogenated hydrocarbon resins are known. For example, in these methods, a cyclic diolefin such as cyclopentadiene and an ethylenically unsaturated aromatic component such as styrene or indene are copolymerized, and the resulting hydrocarbon resin in a further step at least partially hydrogenated. The hydrocarbon resin thus obtained may be used alone or together with other additives as a hot melt tackifier.

Such a process is described in US Pat. No. 5,502,140, in which particularly inexpensive dicyclopentadiene-containing starting materials are used. EP 2 251 364 B1 describes a process for the preparation of hydrocarbon resins of the type described in the introduction which have an aromatic compound content of 5 to 25% by weight.

By-products can be produced in various places from different causes in the production of hydrocarbon resins. For example, in addition to the desired hydrocarbon resin, low molecular weight waxy or high molecular weight duromer-type by-products may form in the polymerization which may affect the quality of the final product and contribute to intolerance in the hot melt adhesive.

Also in the purification and / or isolation of intermediates or in the isolation of the final product, adverse by-products may form. Thus, both the polymerization and the hydrogenation are normally carried out in the presence of different inert solvents, so that considerable amounts of solvent have to be removed both after the polymerization and after the hydrogenation. The removal of the often high-boiling solvents usually requires heating to high temperatures, with by-products can arise by Nachreak functions.

Various solutions have been proposed to avoid by-products. For example, EP 3 124 503 A1 describes a process for the preparation of hydrocarbon resins in which dicyclopentadiene is reacted with a vinylaromatic compound to give a phenylnorbornene derivative at a reasonable cost increase in a preliminary reaction in order to improve the compatibility Polymerization reaction serves as a starter. The resulting hydrocarbon resin is then hydrogenated. A disadvantage of this method is that it contains an additional step with the Vorre action, in which also the temperature must be kept in a window in order to obtain the Phenylnorbornenderivat with high Selec activity.

SUMMARY OF THE INVENTION

The invention is therefore an object of the invention to provide a cost-effective method be, with the hydrocarbon resins as far as possible without byproducts bar.

This object is achieved by a method for producing a hydrocarbon resin from at least one cyclic diolefin component and at least egg ner ethylenically unsaturated aromatic component, wherein a monomer mixture comprising at least one cyclic diolefin component and at least one ethylenically unsaturated aromatic component having 8 to 13 carbon atoms heated to a temperature of at least 180 ° C at a heating rate of 0.5 ° C / second to 10 ° C / second to obtain a hydrocarbon resin from at least one cyclic diolefin component and at least one ethylenically unsaturated aromatic component, wherein the monomer mixture during warming to at least 180 ° C and during the polymerization is substantially single phase liquid.

The invention further relates to a hydrocarbon resin, comprising at least partially hydrogenated hydrocarbon resin component of a cyclic diolefin component and an ethylenically unsaturated aromatic component having 8 to 13 carbon atoms, in particular 8 to 10 carbon atoms, wherein the carbon hydrogen resin has a molecular weight Mz of less than 2,500 g / mol, in particular of less than 2,000 g / mol or less than 1,800 g / mol. The invention finally relates to the use of the hydrocarbon resin according to the invention in paint, in particular as additives in paint, in plastics, in particular as modifiers in plastics, in rubber products, in particular for improving the mechanical and dynamic properties in rubber products, in bitumen, especially as an additive and / or as water repellents in bi tumen, in polypropylene films, in particular as modifying and / or hydrophobicizing agent in polypropylene films, in particular BOPP films, in cosmetics, in printing inks or as tackifiers in adhesive compositions, in particular for applications in the hygiene industry and for use in food telverpackungen.

By the temperature control according to the invention with a substantially single-phase liquid monomer mixture, the formation of waxy low molecular weight, but also the high molecular weight duromer-like by-products is significantly reduced. There is obtained a light hydrocarbon resin.

Fig. 1 shows a schematic representation of the method according to the invention.

PREFERRED EMBODIMENTS OF THE INVENTION

In the process according to the invention cyclic diolefins are used as starting material. Cyclic diolefins are in particular cycloalkenes having at least two carbon-carbon double bonds, which may in particular be conjugated. Cyclic diolefins may be present as a monomer, as a dimer or as a mixture of monomer and dimer. If mixtures of different cyclic diolefins is used, mixed dimers can also be present. Cyclic diolefins used according to the invention may have as monomer 5 to 10, in particular 5 to 7, carbon atoms and / or two conjugated carbon-carbon double bonds. Examples of cyclic diolefins suitable according to the invention are cyclopentadiene, cyclopentadiene derivatives such as methylcyclopentadiene, ethylcyclopentadiene, pentamethylcyclopentadiene, ethyltetramethylcyclopentadiene and dicyclopentadienes. Cyclopentadiene and cyclopentadiene derivatives tend to spontaneously dimerize at room temperature, with the monomers again forming on heating in the reverse reaction. In mixtures of cyclopentadiene and methylcyclopentadiene, the two monomers, cyclopentadiene-cyclopentadiene dimers, methylcyclopentadiene-methylcyclopentadiene dimers and cyclopentadiene-methylcyclopentadiene-co-dimers may be present.

In addition to pure cyclic diolefins, mixtures containing cyclic diolefins can be used as the cyclic diolefin component. As a cyclic Diolefinkomponen te in the process according to the invention a petroleum fraction with a content of pure cyclic diolefin of at least 25 wt .-%, based on the mass of a set Petroleumfraktion be used. A pure compound according to the invention has a degree of purity of at least 95%, preferably at least 97%, more preferably at least 99% or 100%, in each case based on the mass of the compound.

Preferably, the cyclic diolefin component may be cyclopentadiene and / or dicyclopentadiene. The cyclic diolefin component may further preferably be methylcyclopentadiene and / or the dimer of methylcyclopentadiene.

In one embodiment, the cyclic diolefin component includes cyclopenta-diene, dicyclopentadiene, methylcyclopentadiene, the co-dimer of methylcyclopentadiene, and cyclopentadiene.

The further component of the monomer mixture is at least one ethylenically unsaturated aromatic compound having 8 to 13 carbon atoms. This can be a pure connection. According to another preferred embodiment, however, it is also possible to prepare a petroleum fraction or a constituent from the tar preparation containing ethylenically unsaturated aromatic compound of at least 25% by weight, based on the mass of the petroleum fraction or on the mass of the fraction from the tar processing.

Advantageously, the ethylenically unsaturated aromatic component contains further aromatic compounds having a carbon-carbon double bond outside the aromatic ring and especially 8 to 13 carbon atoms. Examples of aromatic compounds are styrene, α-methylstyrene, o-vinyltoluene, m-vinyltoluene, p-vinyltoluene, indene and / or one or more methylindenes.

According to one embodiment, the ethylenically unsaturated aromatic component contains styrene, α-methylstyrene, o-vinyltoluene, m-vinyltoluene, p-vinyltoluene, indene and one or more methylindenes.

The cyclic diolefin component and the ethylenically unsaturated aromatic component may be present in different proportions in the monomer mixture. Advantageously, the two components are metered so that the monomer mixture 20 wt .-% to 95 wt .-%, preferably 20 wt .-% to 80 wt .-% or 40 wt .-% to 60 wt .-%, of cyclic Diolefin or cyclic diolefins containing and 80 wt .-% to 5 wt .-%, preferably 80 wt .-% to 20 wt .-% or 60 wt .-% to 40 wt .-% of ethylenically unsaturated aromatic compound or ethylenically unsaturated contains aromatic compounds, each based on the total mass of the monomers in the monomer mixture. According to one embodiment, the cyclic diolefin component and the ethylenically unsaturated aromatic component are metered such that the monomer mixture contains from 50% by weight to 95% by weight, preferably from 60% by weight to 95% by weight, more preferably 65% by weight. % to 90% by weight, more preferably from 70% to 80% by weight, of cyclic diolefin or cyclic diolefins and from 50% to 5% by weight, preferably 40% by weight to 5 wt .-%, more preferably 35 wt .-% to 10 wt .-%, particularly preferably 20 wt .-% to 30 wt .-% of ethylenically unsaturated aromatic compound or contains ethylenically unsaturated aromatic compounds, in each case based on the total mass of the monomers in the monomer mixture.

The monomer mixture may contain a non-polymerizable solvent. Suitable solvents are aromatic and naphthenic solvents. Suitable solvents are therefore, for example, benzene, toluene, xylene, ethylbenzene, cyclohexane, dimethylcyclohexane, ethylcyclohexane or mixtures thereof. Particular preference is given to using monosubstituted or polysubstituted alkyl-substituted benzene compounds having from 7 to 10 carbon atoms. These preferably have a boiling point above 100 ° C, in particular above 130 ° C. If xylene is used as the solvent, it may be present as a pure compound or as a mixture of two or more of the isomers o-xylene, m-xylene and p-xylene. According to a further preferred embodiment, a C8 isomer mixture can be used. The C8 isomer mixture preferably comprises a mixture of o-xylene, m-xylene, p-xylene and ethylbenzene. Petroleum fractions and components from the tar distillation may already contain non-polymerizable Lösemit tel. Thus, the addition of a solvent can be dispensed with if a petroleum fraction is used as the cyclic diolefin component and / or a petroleum fraction or a constituent from the tar distillation is used as the ethylenically unsaturated aromatic component.

The non-polymerizable solvent may be contained in the monomer mixture in an amount of 0 to 40% by weight based on the mass of the monomer mixture. Preferably, a solvent amount of 5 to 35 wt .-%, particularly preferably 5 to 30 wt .-%, for example about 30 wt .-%, each based on the mass of the monomer mixture used.

In one embodiment, the process is performed substantially with the exclusion of oxygen. As a result, the formation of by-products can be reduced. In particular, the formation of acid and ester groups in the product can be avoided. This helps to achieve as colorless as possible hydrocarbon resins. Preferably, the cyclic diolefin component and / or the ethylenically unsaturated aromatic component, in particular the Lagerbehäl ter for the cyclic diolefin and / or the ethylenically unsaturated aromatic components, inertized with an inert gas such as nitrogen. Advantageously, the non-hydrogenated and / or hydrogenated hydrocarbon resin, in particular the storage containers for the non-hydrogenated and / or the hydrogenated hydrocarbon resin, are also rendered inert with a protective gas such as nitrogen.

An essential feature of the process according to the invention is the rapid Aufhei zen the monomer mixture to the polymerization. According to the invention, the heating of the monomer mixture takes place at a rate of

0.5 ° C / second to 10 ° C / second, preferably 1 ° C / second to 10 ° C / second, especially 2 ° C / second to 10 ° C / second, more preferably 2 ° C / second to

7 ° C / second, more preferably 2 ° C / second to 5 ° C / second or 2 ° C / second to 4 ° C / second. In particular, the abovementioned heating rates are used when the monomer mixture is heated to the temperature at which the polymerization reaction begins, in particular up to a temperature of 180 ° C. to 235 ° C. As soon as the monomer mixture has reached a temperature above 180 ° C. or more, subsequent temperatures can also be set at heating rates other than the abovementioned. It has been determined that at the heating rates according to the invention, the amount of by-products is low. This means that the hydrocarbon resins obtained according to the invention have a high compatibility with other constituents in application formulations of hot-melt adhesives.

Although the polymerization already starts at a temperature of 180 ° C., the polymerization in the process according to the invention can also be carried out at relatively high temperatures. In the process according to the invention, the polymerization is carried out at a temperature of 180.degree. C. or higher. Thus, the polymerization may be carried out at a temperature of from 200 ° C to 300 ° C or from 250 ° C to 300 ° C or from 260 ° C to 280 ° C. For example, a polymerization temperature of from 265 ° C. to 275 ° C. is also preferred. During the polymerization, the temperature to be changed. For example, the temperature during the polymerization can be increased up to a final temperature. According to one embodiment, the aforementioned temperatures are final temperatures. These are reached at the end of the polymerization process.

It has been found that sparingly soluble high molecular weight products are formed when the monomer mixture is heated rapidly, especially at the beginning of the polymerization, to high temperatures, in particular to temperatures above 240 ° C. Such poorly soluble products are particularly problematic for continuous driving. Furthermore, it has been found that the products have a low softening point and are waxy when the polymerization is carried out entirely at lower temperatures, in particular at temperatures below 240 ° C. Conveniently, therefore, the temperature is changed during the polymerization reaction.

Therefore, according to one embodiment, the monomer mixture is first heated to a temperature below the temperature at which the polymerization reaction begins, in particular to a temperature of about 140 ° C to 165 ° C. Subsequently, the monomer mixture to a final temperature of 250 ° C to 280 ° C, in particular from 255 ° C to 270 ° C, heated. Conveniently, the subsequent He heat to a final temperature of 250 ° C to 280 ° C, in particular from 255 ° C to 270 ° C, according to a temperature profile. Preferably, the temperature profile includes a ramp, one or more stages, or combinations thereof. Preferably, the temperature at the beginning of the polymerization reaction is heated linearly from 180 ° C to a final temperature of 280 ° C. More preferred is a linear ramp of 190 ° C to 270 ° C. Particularly preferred is a linear ramp of 200 ° C to 250 ° C. Since this can be technically difficult to implement technically, the linear temperature ramp can also be approximated in temperature stages in which the respective temperature is kept for a certain time before the next temperature level is set. Before zugt is also a combination of stages and ramps. It has been found, for example, to be favorable, a lower temperature, ideally from 180 ° C to 230 ° C, preferably from 200 ° C to 220 ° C for a longer time, in particular for a period of 10 to 45 minutes, preferably from 15 to 35 minutes, and then line ar the temperature to the preferred final temperature of 280 ° C or 270 ° C or 250 ° C increase. Preferably, the linear increase in temperature is performed at a rate of 50 ° C / hour to 250 ° C / hour. More preferably, the temperature profile comprises a first step in which the monomer mixture is heated to a first temperature of 180 ° C to 230 ° C, preferably from 200 ° C to 220 ° C. Advantageously, the temperature profile comprises a further step in which the temperature of the monomer mixture is heated from the first temperature to a final temperature of from 250 ° C to 280 ° C, in particular from 255 ° C to 270 ° C. The heating from the first temperature to the final temperature can be carried out stepwise or continuously, in particular linear. Further, the heating from the first temperature to the final temperature may be smoothly or unevenly. In particular, the heating from the first temperature to the final temperature uniformly step by step he can follow. According to one embodiment, the monomer mixture in a first step to a first temperature of 180 ° C to 230 ° C, in particular from 200 ° C to 220 ° C, and in a further step, stepwise to a final temperature of 250 ° C to 280 ° C. , in particular from 255 ° C to 270 ° C, heated. Preferably, the monomer mixture is held at the final temperature for 20 minutes or less.

By means of a temperature profile during the polymerization, the molecular weight Mz of the hydrocarbon resin can be controlled. Likewise, with a temperature profile, the degree of polymerization and / or the polydispersity can be controlled. In addition, the softening point can be controlled with a temperature profile. In addition, with a temperature profile, the color and the amount of by-products formed can be controlled In particular, can be avoided with the above temperature profiles, in which temperatures above 240 ° C towards the end of the polymerization reaction can be achieved that large amounts of insoluble high molecular weight products arise. At the same time, hydrocarbon resins having the desired indexing points can be obtained with these temperature profiles. The polymerization can be carried out at a pressure of 10 bar or more. For example, the pressure may be 10 to 25 bar, in particular 15 bar to 25 bar or 10 to 15 bar. If the polymerization is carried out at less than 10 bar, the end product is of lower quality. In addition, the yield is clotting ger. Furthermore, the presence of a gas phase can be substantially avoided by the aforementioned pressures. This allows better control of the reaction.

The polymerization can be carried out continuously or batchwise. Preferably, the polymerization is carried out continuously. The continuous procedure has the advantage that the heat transfer is better than in the batch process. Furthermore, the operating costs are lower in continuous operation and the process can be carried out safely.

The polymerization can be carried out in different reaction vessels who the. Preferably, the polymerization is carried out in a tubular reactor. This procedure has proved particularly advantageous in the case of continuous polymerization. In the tube reactor, the polymerization can be carried out in particular during a residence time of from 30 to 180 minutes, in particular from 40 to 120 minutes, or from 50 to 90 minutes.

If the properties of the hydrocarbon resin obtained according to the invention are to be changed, the resulting hydrocarbon resin can be partially or completely digested in the tubular rekiller. This measure will be useful, for example, if higher molecular weights of the hydrocarbon resin to be achieved. The recycle is preferably carried out in the raw material mixture of the input current. The amount of recycled hydrocarbon resin can be 0 to 90 wt .-%, based on the mass of the exiting product stream, Betra conditions. Such a recycling can be carried out particularly easily in tubular reactors. The hydrocarbon resin obtained after the polymerization can be directly further processed after separation of the solvent and unreacted monomer or it can be stored in an intermediate tank storage. Preferably, it is stored in an intermediate tank storage. The intermediate storage facility compensates for any fluctuations in production volumes. The hydrocarbon resin can also be used directly for the applications mentioned herein, especially for rubber applications. Furthermore, the hydrocarbon may also be functionalized or hydrogenated. Unreacted monomers can be thermally separated from the solvent and recycled again by addition to the raw material mixture of the feedstream. This additionally increases the resin yield.

Preferably, the polymerization of the raw materials to the hydrocarbon resin is carried out without catalyst.

The hydrocarbon resin obtained according to the invention is preferably partially or completely hydrogenated. The hydrogenation takes place in the presence of a catalyst. As a catalyst, various catalysts come into consideration. Thus, in the hydrogenation nickel, palladium, cobalt, platinum and rhodium-based catalysts can be used. Advantageously, nickel is used as catalyst. The aforementioned catalysts may be supported on a support such as alumina, silica, zeolites, clay minerals such as montmorillonite and silicon carbide. Preferably, the hydrogenation of the hydrocarbon resin is carried out in the presence of a nickel catalyst. According to another preferred embodiment of the invention, a nickel catalyst is used on an alumina / silica support. These catalysts are commercially available. The nickel catalyst can be present in particular in heterogeneous form. As a result, after completion of the hydrogenation, it can be easily removed by filtration. The term "partial hydrogenation" is understood to mean that predominantly isolated double bonds are hydrogenated or that additionally some of the aromatic constituents of the hydrocarbon resin are hydrogenated. Preference, the hydrocarbon resin is completely hydrogenated in the hydrogenation. In the case of complete hydrogenation, therefore, 95% or more, in particular 98% or more or 99% or more or all unsaturated constituents are converted. The complete hydrogenation has the advantage that fewer by-products are formed by Nachre actions and thus discoloration in the hydrocarbon resin AS POSSIBLE be largely avoided. Whether the hydrocarbon resin was partially or completely hydrogenated can be determined by NMR spectroscopy, in particular by determining the content of double bonds by means of * H NMR spectroscopy.

The hydrogenation can be carried out in the presence of a solvent, in particular an aliphatic solvent. Suitable solvents are, for example, refined gasolines, in particular a mixture of saturated hydrocarbons which are liquid at room temperature. Such mixtures are commercially available under the designation D40, for example Exxsol D40 or Shellsol D40. By adding the solvent, the viscosity of the hydrocarbon resin can be reduced. Fer ner can be saved with the use of an aliphatic solvent such as D40 over the use of an aromatic solvent hydrogen.

Preferably, the hydrocarbon resin 80 wt .-% or more, in particular 90 wt .-% or more or 100 wt .-% or more, based on the mass of hydrocarbon Hydro, be added to solvent. Preferably, a hydrogenation mixture containing hydrocarbon resin and solvent is used. Before geous enough, the hydrogenation mixture is a solution. Preferably, the hydrogenation mixture comprises 50% hydrocarbon resin.

The hydrogenation can be carried out batchwise or continuously. Preferably, the reaction is continuous. Advantageously, the hydrogenation in a Loop reactor can be performed. Preferably, the hydrogenation mixture is circulated. The loop reactor advantageously has a gas-liquid ejector. By using a loop reactor in conjunction with a gas-liquid ejector, a particularly good mixing of the hydrocarbon resin to be hydrogenated with hydrogen and the optionally added catalyst can be achieved, whereby the hydrogenation time can be shortened.

The hydrogenation is preferably carried out at a pressure of more than 70 bar, in particular from 75 bar to 105 bar or from 80 bar to 100 bar or from 85 bar to 95 bar. Thereby, the hydrogenation of the hydrocarbon resin can be adjusted to the desired degree of hydrogenation.

The hydrogenation is further preferably carried out at a temperature of 250 ° C or higher, more preferably from 250 ° C to 300 ° C or from 260 ° C to 280 ° C. It was found that at a hydrogenation temperature of less than 250 ° C, the hydrogenation is slow and at temperatures above 300 ° C again increased by-products can form.

In a commonly used loop reactor, the hydrogenation may be carried out for 80 to 160 minutes, preferably for 90 to 150 minutes, and more preferably for 100 to 150 minutes or for 110 to 150 minutes. Thereby, the desired degree of hydrogenation of the hydrocarbon resin as well as the brightness can be adjusted.

According to a particularly preferred embodiment of the invention, an expansion stage is provided both after the polymerization and after the hydrogenation. The first post-polymerization relaxation step is to remove volatile components, particularly solvent and / or unreacted monomer, from the hydrocarbon resin-containing polymerization mixture. By exploiting the pressure gradient in the first expansion stage, the polymerisation mixture is flashed, as a result of which the more volatile components are released. be removed. Preferably, the hydrocarbon containing polymerization tion mixture in the first relaxation step at a temperature of 240 ° C to 300 ° C, more preferably at a temperature of 250 ° C to 290 ° C or 260 ° C to 280 ° C are introduced.

Preferably, the hydrocarbon resin after the first relaxation step, only 3 wt .-% or less, more preferably 1 wt .-% or less or 0.5 wt .-% or less of solvent and / or unreacted monomer, each based on the Mass of hydrocarbon resin, on.

In the first expansion stage, the absolute pressure can be lowered to 1 bar or less, preferably 0.1 bar or less, and more preferably 0.03 bar or less. Due to the drop in pressure can be dispensed with elaborate stirred Anla conditions such as thin film evaporator or water stripping facilities. This makes the process cheaper and less susceptible to failure. However, a thin film evaporator can be used in the process after the polymerization and subsequent first flash stage. This can achieve a low content of solvent in the hydrocarbon resin after the polymerization.

After the hydrogenation of the hydrocarbon resin, a second expansion stage may preferably be provided. In the second expansion stage, at least part of the volatile constituents, in particular of the solvent, can be removed from the hydrocarbon, without a large amount of by-products being produced by additional thermal loading and the color numbers of the resin deteriorating. Preferably, the hydrocarbon resin after the second expansion stage 2 wt .-% or less, preferably 0.5 wt .-% or less or 0.03 wt .-% or less of solvent, each based on the mass of the hydrocarbon resin, on. The pressure reduction in the second expansion stage can be made in two relaxation steps. In this case, in a first expansion step, the absolute pressure can be reduced to 0.5 bar or less, preferably 0.2 bar or less, preferably 0.05 bar or less or particularly preferably 0.01 bar or less. After the hydrogenation, the catalyst is preferably first removed. The catalyst can be removed by filtration, for example. The hydrogenation mixture is preferably used at a temperature of from 190 ° C to 270 ° C, more preferably from 200 ° C to 260 ° C, more preferably from 210 ° C to 250 ° C, further preferably from 220 ° C to 240 ° C , even more preferably initiated by 230 ° C in the first relaxation step. After the first expansion step, the hydrogenation mixture may be in the second expansion step at a temperature of 190 ° C to 270 ° C, preferably from 200 ° C to 260 ° C, more preferably from 210 ° C to 250 ° C, or from 220 ° C to 240 ° C are initiated. In the second expansion step, the absolute pressure may preferably be lowered to 0.1 bar or less, preferably 0.05 bar or less, more preferably 0.03 bar or less, further preferably 0.01 bar or less.

The first and second flash stages may also be referred to as devolatilization.

In addition, the hydrogenation mixture, from which previously optionally added catalyst has been removed, can be introduced into a preliminary expansion stage immediately before the second expansion stage. The hydrogenation mixture may have a temperature of 240 ° C to 300 ° C, preferably from 250 ° C to 290 ° C and more preferably from 260 ° C to 280 ° C. Preferably, in the Vorentspan tion stage, the pressure to 3 bar or less, preferably 2 bar or less, wei ter preferably 1.5 bar or less, even more preferably 1 bar or less, are lowered abge. If a preliminary relaxation stage is provided, the mixture taken from the preliminary expansion stage is preferably introduced into the second expansion stage. By performing one or more flash stages, the period of time during which the hydrocarbon resin is held at temperature can be reduced. This measure can also serve to reduce by-products.

According to one embodiment, after the hydrogenation of the hydrocarbon resin, two flash evaporation steps are provided. These two flash evaporation steps preferably form the second flash stage. For this purpose, the catalyst is preferably first removed. The catalyst can be removed by filtration, for example. Subsequently, in the first expansion-evaporation step, the preferably catalyst-free hydrogenation mixture is passed into a first pressure vessel. The pressure in the first pressure vessel is lower than the pressure of the hydrogenation mixture. Preferably, the pressure of the hydrogenation mixture in the first pressure vessel is lowered to an absolute pressure of 3 bar or less, preferably 2 bar or less, more preferably 1.5 bar or less, even more preferably 1 bar or less. In particular, this allows hydrogen to be removed from the hydrogenation mixture.

In the second flash evaporation step, the resulting mixture is passed to a second pressure vessel. The pressure in the second pressure vessel is lower than the pressure of the resulting mixture. Preferably, the pressure of the resulting mixture in the second pressure vessel is lowered to 0.1 bar or less, preferably 0.05 bar or less, more preferably 0.03 bar or less. As a result, in particular solvents can be removed. Advantageously, after the second flash evaporation step, a thin film evaporator is provided which is operated at 0.01 bar or less, preferably at 0.005 bar or less, more preferably at 0.003 bar or less. In this way, the solvent can be largely removed from the hydrogenated hydrocarbon resin who the. The hydrogenation mixture is preferably at a temperature of from 190 ° C to 270 ° C, more preferably from 200 ° C to 260 ° C, more preferably from 210 ° C to 250 ° C, further preferably from 220 ° C to 240 ° C more preferably introduced from 230 ° C in the first flash evaporation step. After the first flash evaporation step, the hydrogenation mixture may be introduced into the second flash evaporation step at a temperature of from 190 ° C to 270 ° C, preferably from 200 ° C to 260 ° C, more preferably from 210 ° C to 250 ° C, or from 220 ° C up to 240 ° C. After the second flash evaporation step, the hydrogenation mixture may be introduced into the thin film evaporator at a temperature of from 180 ° C to 260 ° C, preferably from 190 ° C to 250 ° C, more preferably from 200 ° C to 240 ° C, or from 210 ° C to 230 ° C ° C be initiated.

The hydrocarbon resin obtained according to the invention may have a molecular weight Mz of less than 2,500 g / mol, preferably less than 2,000 g / mol, more preferably less than 1,800 g / mol.

The hydrocarbon resin obtained according to the invention is preferably hydrogenated. The term "hydrogenated" also includes those hydrocarbon resins in which the double bonds are hydrogenated to at least 90%, preferably 95% to 100%.

If the hydrocarbon resin is completely hydrogenated, preferably at least 95%, more preferably at least 98%, particularly preferably at least 99% of the double bonds of the hydrocarbon resin are hydrogenated. Higher levels of hydrogenation can improve the thermal stability of the hydrocarbon resin. The content of double bonds can be determined by means of ^X H NMR spectroscopy.

Various molecular weights are known to those skilled in the art. Thus, the number-average molecular weight Mn, the weight-average molecular weight Mw and the centrifuge-average molecular weight Mz are known to him. In the present case, the Zentrifu mean molecular weight Mz is also abbreviated as the molecular weight Mz. Methods for determining the molecular weight Mz are known to the person skilled in the art. For example, it can determine the molecular weight Mz by means of gel permeation chromatography or by mass spectrometry. For measurements with gel permeation chromatography, THF is preferably used as the eluent. The calibration standard used is preferably polystyrene. The measurements with gel permeation chromatography are advantageously carried out with linear columns having a porosity of 1000 Å. Preferably, RI and UV detectors are used. With a UV detector, the degree of hydrogenation of a molecular weight section can be displayed in addition to the molar mass.

The hydrocarbon resin obtained in the present invention preferably has a polydispersity index of 2.5 or less, preferably 2 or less, more preferably 1.5 or less.

The softening point of the hydrocarbon resin is preferably 170 ° C or less, more preferably 60 ° C to 150 ° C or 70 ° C to 140 ° C or 80 ° C to 130 ° C or 90 ° C to 140 ° C. For the determination of the softening point, the ring and gel method according to standard ASTM D 3461 is used.

Further, the hydrocarbon resin obtained by the present invention may have a hu- ene color number of 40 or less, especially 25 or less. The Haze color number is determined according to the standard DIN EN ISO 6271: 2016-05. The Hazen color number can also be referred to as platinum-cobalt color number.

The hydrocarbon resin obtained in the present invention may have a yellowness index of 4 or less, especially 2 or less. The Yellowness In dex is determined according to the standard ASTM D1209-05 (2011).

The invention furthermore relates to the use of the hydrocarbon resin according to the invention in paint, in particular as additives in paint, in plastics, in particular as modifiers in plastics, in rubber products, in particular for improving the mechanical and dynamic properties in rubber products, in bituminous products. men, in particular as an additive and / or as a hydrophobing agent in bitumen, in Polyp ropylenfolien, especially as modifying and / or hydrophobizing agents in polypropylene films, in particular BOPP films, in cosmetics, in printing inks or as a tackifier for hot melt adhesives, especially for applications in the hygiene article industry and for use in food packaging.

Preferably, the non-hydrogenated hydrocarbon resin is used to improve the mechanical and dynamic properties in rubber products such as tires, in bitumen, especially for asphalt, and in printing inks.

Preferably, the hydrogenated hydrocarbon resin in paint, especially as additives in paint, in plastic, especially as a modifier in plastic, in bitumen, in particular as water repellents in bitumen, for example, for Dachbah NEN, in polypropylene films, in particular as a modifying and / or hydrophobizing agent in Polypropylene films, in particular BOPP films, in cosmetics or as a tackifier in adhesive compositions, in particular for applications in the hygiene industry and for use in food packaging ver used.

EXAMPLE

The invention will be explained in more detail below with reference to an exemplary, non-limiting position of manufacture of a hydrocarbon resin according to the invention including hydrogenation. The pressures given are absolute pressures.

In the continuous process shown schematically in Figure 1, the storage tank 11 contains a petroleum fraction (hereinafter referred to as BN-200) rich in dicyclopentadiene, methylcyclopentadiene dimers and cyclopentadiene-methylcyclopentadiene dimers (hereinafter referred to as cyclic diolefins). In the storage tank 12 is another petroleum fraction (hereinafter referred to as C9 fraction) which is rich in styrene, vinyltoluenes, indene and methylindenes (hereinafter referred to as ethylenically unsaturated aromatics). Storage tank 13 ent holds dicyclopentadiene with a purity of at least 95%. Storage tank 14 contains xylene as an inert solvent. From the storage tanks 11, 12, 13 and 14, a monomer mixture is now prepared in the template 15. The monomer mixture is mixed on introduction into the receiver 15 by means of a static mixer. The template 15 may also have a stirrer for mixing. From the storage tanks 11, 12, 13 and 14, the components BN-200, C9 fraction, pure dicyclopentadiene and xylene are taken in an amount such that the monomer mixture contains cyclic diolefins and ethylenically unsaturated aromatics in a ratio of 3: 1 to the mass of the cyclic diolefins and ethylenically unsaturated flavorings in the monomer mixture. The ratio can be adjusted in particular by the addition of pure dicyclopentadiene from storage tank 13. In addition, the monomer mixture contains 50% of solvent, based on the mass of the monomer mixture.

From the template 15, the mixture with a feed flow of 12 kg / h in the Erhit 16 is introduced. Subsequently, the monomer mixture is brought in the heater 16 to a reaction temperature of 192 ° C and then in the tubular reactor 20 poly merisiert .. The temperature of the monomer mixture is increased at a rate of l ° C / second to 192 ° C, whereby the not yet hydrogenated Hydrocarbon resin is formed. The tubular reactor 20 consists of five pipe segments. In each of the pipe segments, the temperature of the monomer mixture is gradually increased. In the first tube segment, the temperature of the monomer mixture is increased to 219 ° C. This causes the monomer mixture to react to form the hydrocarbon still unhydrogenated. In the second tube segment, the temperature of the monomer mixture is raised to 231 ° C. The temperature is gradually increased in each of the tube segments of the tube reactor 20. In the third pipe segment, the temperature of the monomer mixture is increased to 243 ° C. In the fourth tube segment, the temperature of the monomer mixture is increased to 252 ° C. In the fifth tube ment the temperature of the monomer mixture is increased to 263 ° C. The pressure in the tubular reactor 20 is 15 bar. The residence time in the tubular reactor 20 is 60 minutes. During warm-up and during the polymerization, the monomer mixture is essentially single-phase liquid.

From the tubular reactor 20, a stream of 12 kg / h of unhydrogenated Kohlenwas hydrogen, residual solvent and residual monomers are obtained and introduced into the expansion evaporator 21. The stream enters the flash evaporator 21 at a temperature of 263 ° C. and a pressure of 15 bar. In the expansion evaporator 21, the pressure of the stream is reduced to 30 mbar. The content of solvent and unreacted monomer in the hydrocarbon resin is reduced to 10,000 ppm or less. The bottom product from the expansion evaporator 21, which consists essentially of not yet hydrogenated hydrocarbon resin, is fed to the intermediate storage tank 22 as an intermediate flow of 3.7 kg / h. About the top of the expansion evaporator 21, a condensate stream of 8.3 kg / h containing solvent and unreacted monomers is removed. In order to further purify the hydrocarbon in the hydrocarbon, a thin-film evaporator can be used after the expansion evaporator 21. The hydrocarbon resin in the storage tank 22 has a centrifuge average molecular weight of less than 1800 g / mol. Furthermore, the hydrocarbon resin in the intermediate storage tank 22 has a softening point, determined by the ring and ball method according to standard ASTM D 3461, of 95 ° C. The Hazen color number, determined according to D1N EN ISO 6271: 2016-05, of the hydrocarbon resin in the interim storage tank 22 is 13. The unhydrogenated hydrocarbon resin can be removed from the interim storage tank 22 via the line 22 '.

For the preparation of a hydrogenated hydrocarbon resin hydrocarbon resin is removed from the storage tank 22 and introduced together with an aliphatic solvent, such as Exxsol D40, from the tank 17 in the original tank 23. To mix the hydrocarbon resin with the aliphatic's solvent, a static mixer is used. In the template tank 23 is the Hydrocarbon resin dissolved in the aliphatic solvent at a concentration of 50 wt .-%. From the solution in the storage tank 23 7.4 kg / h are fed into the loop reactor 30 for hydrogenation. The loop reactor 30 is supplied from the catalyst reservoir 31 with a nickel catalyst on silica. The catalyst is renewed periodically. The amount of catalyst in the loop reactor 30 is 1.5 wt .-%, based on the mass of not yet hydrogenated hydrocarbon resin. From the hydrogen production 32, the loop reactor 30 is supplied with hydrogen. The pressure in the loop reactor 30 is set to 90 bar. In the loop reactor 30, the hydrogenation mixture is circulated at a ratio of 100: 1, based on the inlet flow into the loop reactor 30. The hydrogenation is carried out at a temperature of 270 ° C in the loop reactor 30. The residence time for the hydrogenation mixture in the loop reactor 30 is 120 minutes.

The catalyst is removed from the loop reactor via the reactor filter 33 and a product flow of 7.5 kg / h is introduced into the first pressure vessel 34. The product stream is introduced into the pressure vessel 34 at a pressure of 85 bar. The temperature of the product stream is 270 ° C. In the pressure vessel 34, the pressure is reduced to 1.2 bar .. 4.2.2 kg / h from the Druckbe container 34 are introduced into the second pressure vessel 35 as the bottom product. 3.3 kg / h of aliphatic solvent and hydrogen are removed overhead.

The bottom product from the pressure vessel 34 is introduced via an expansion valve at a temperature of 240 ° C in the combined container 35 with a second pressure vessel with connected thin-film evaporator. The pressure is lowered to 0.03 bar in the second pressure vessel. 3.64 kg / h of resin are obtained as the bottom product, and 0.36 kg / h of aliphatic solvent as top product. The bottom product is then expanded at 230 ° C in the downstream thin-film evaporator, which is operated at 0.003 bar. About 0.04 kg / aliphatic solvent are removed overhead. 3.60 kg / h of hydrogenated hydrocarbon resin having a residual solvent content of less than 300 ppm are obtained as the bottom product and introduced into the Product storage tank 36 delivered. This can be removed via the removal 36 who the.

The steps of polymerization, hydrogenation and material separation described in the previous example can also be carried out separately from one another, for example in a batchwise manner.

The process described in the preceding example can also be carried out essentially with the exclusion of oxygen.

The hydrogenated hydrocarbon resin in the product storage tank 36 has a number average molecular weight of less than 1800 g / mol. The yellowness index of the hydrogenated hydrocarbon resin, measured according to ASTM D1209-05 (2011), is less than 1. Further, the hydrogenated hydrocarbon resin has a softening point, as determined by the ring and ball method according to ASTM D 3461, of 100 ° C , In the hydrogenated hydrocarbon resin, more than 98% of the double bonds of the unhydrogenated hydrocarbon resin are hydrogenated. The hydrogenated hydrocarbon resin has a VOC content of less than 300 ppm.

REFERENCE NUMBERS

11 storage tank BN-200

12 storage tank C9 fraction

13 storage tank of pure dicyclopentadiene

14 storage tank xylene

15 template

16 heaters

17 storage tank D40

20 tubular reactor 21 relaxation evaporator

22 storage tank

22 'removal

23 template tank

30 loop reactor

31 Catalyst stock

32 hydrogen production

33 reactor filter

34 First pressure vessel

35 combined container on second pressure vessel with downstream

thin film evaporator

36 product storage tank

36 'removal

Claims

Patent claims

1. A process for the preparation of a hydrocarbon resin from at least one cyclic diolefin component and at least one ethylenically unsaturated aromatic component, characterized in that

a monomer mixture comprising at least one cyclic diolefin component and at least one ethylenically unsaturated aromatic component having 8 to 13 carbon atoms heated to a temperature of at least 180 ° C at a heating rate of 0.5 to 10 ° C / second is selected from a hydrocarbon resin at least one cyclic diolefin component and at least one ethylenically unsaturated aromatic component, wherein the monomer mixture during warming to at least 180 ° C and during the polymerization is substantially single-phase liquid.

2. Process according to claim 1, characterized in that the cyclic diolefin component contains or consists of cyclopentadiene, cyclopentadiene derivatives such as methylcyclopentadiene, ethylcyclopentadiene, pentamethylcyclopentadiene, ethyltetramethylcyclopentadiene, dicyclopentadiene or mixtures thereof and / or that the ethylenically unsaturated aromatic component is styrene , a-methylstyrene, o-vinyltoluene, m-vinyltoluene, p-vinyltoluene, indene, one or more methylindenes or mixtures thereof or consisting thereof.

3. The method according to any one of the preceding claims, characterized in that the monomer mixture comprises a non-polymerizable solvent, in particular re o-xylene, m-xylene, p-xylene and / or ethylbenzene.

4. The method according to any one of the preceding claims, characterized in that the polymerization at a pressure of 10 bar to 25 bar, in particular from 15 bar to 25 bar or from 10 to 15 bar.

5. The method according to any one of the preceding claims, characterized in that the polymerization at a temperature of 200 ° C to 300 ° C, insbesonde re from 250 ° C to 300 ° C or from 260 ° C to 280 ° C, is performed.

6. The method according to any one of the preceding claims, characterized in that the monomer mixture is first heated to a temperature of 140 ° C to 165 ° C and then to a final temperature of 250 ° C to 280 ° C, in particular from 255 ° C to 270 ° C, heated.

7. The method according to claim 6, characterized in that the subsequent heating to a final temperature of 250 ° C to 280 ° C, in particular from 255 ° C to 270 ° C, according to a temperature profile, in particular the monomer mixture in a first step a first temperature of 180 ° C to 230 ° C, in particular from 200 ° C to 220 ° C, and in a further step, gradually to a final temperature of 250 ° C to 280 ° C, in particular from 255 ° C to 270 ° C, is heated.

8. The method according to any one of the preceding claims, characterized in that the heating rate l ° C / second to 10 ° C / second, in particular 2 ° C / second to 10 ° C / second, more preferably 2 ° C / second to 7 ° C / second, more preferably 2 ° C / second to 5 ° C / second or 2 ° C / second to 4 ° C / second.

9. The method according to any one of the preceding claims, characterized in that the polymerization is carried out continuously, in particular continuously in a tubular reactor, and in particular a residence time of 30 to 180 minutes, in particular 40 to 120 minutes or 50 to 90 minutes in the tubular reactor.

10. The method according to any one of the preceding claims, characterized in that the hydrocarbon resin is partially or completely hydrogenated.

11. The method according to claim 10, characterized in that the hydrogenation in the presence of a solvent, in particular aliphatic solvent or a mixture of saturated, liquid at room temperature hydrocarbons, is performed.

12. The method according to claim 10 or 11, characterized in that the hydrogenation of the copolymer in the presence of a catalyst, in particular a nickel catalyst is performed.

13. The method according to any one of claims 10 to 12, characterized in that the hydrogenation is carried out continuously.

14. The method according to any one of claims 10 to 13, characterized in that the hydrogenation at a pressure of more than 70 bar, in particular from 75 to 105 bar or from 80 to 100 bar or from 85 to 95 bar or 90 bar, and / or at a temperature of 250 ° C or higher, in particular from 250 ° C to 300 ° C or from 260 ° C to 280 ° C, is performed.

15. The method according to any one of the preceding claims, characterized in that the method holds a first relaxation stage ent after the polymerization.

16. The method according to any one of claims 10 to 15, characterized in that the method after the hydrogenation of the hydrocarbon resin contains a second expansion stage.

17. Hydrocarbon resin of at least one cyclic diolefin component and at least one ethylenically unsaturated aromatic component having 8 to 13 carbon atoms, wherein the hydrocarbon resin has an Mz of less than 2,500 g / mol, in particular less than 2,000 g / mol or less than 1,800 g / mol.

18. Hydrocarbon resin according to claim 17, characterized in that the cyclic diolefin component contains cyclopentadiene, cyclopentadiene derivatives such as methylcyclopentadiene, ethylcyclopentadiene, pentamethylcyclopentadiene, ethyltetamethylcyclopentadiene, dicyclopentadiene or mixtures thereof or there is out and / or that the ethylenically unsaturated aromatic components te styrene , α-methylstyrene, o-vinyltoluene, m-vinyltoluene, p-vinyltoluene, indene, one or more methylindenes or mixtures thereof or consisting thereof.

19. A hydrocarbon resin according to any one of claims 17 or 18, characterized in that the hydrocarbon resin is hydrogenated and / or a softening point of 170 ° C or less, in particular from 60 to 150 ° C or from 70 to 140 ° C or 80 to 130 ° C or from 90 to 120 ° C, and / or a Hazen color number of 40 or less, in particular of 25 or less, and / or a yellowness index of 4 or less, in particular 2 or less, has.

20. A hydrocarbon resin according to any one of claims 17 to 19, characterized in that the hydrocarbon resin is obtainable by a process according to any one of claims 1 to 16.

21. Use of a hydrocarbon resin according to any one of claims 17 to 20 in paint, especially as additives in paint, in plastics, especially as Modifika tion medium in plastic, in rubber products, in particular for improving the mechanical and dynamic properties in rubber products, in Bi tumen, in particular as an additive and / or as a hydrophobing agent in bitumen, in polypropylene films, in particular as modifying and / or hydrophobizing agent in polypropylene films, in particular BOPP films, in cosmetics, in Printing inks or as a tackifier for hot melt adhesives, in particular for Applikati onen in the hygiene industry and for use in food packaging.