Patent Application
20230108326
The invention relates to polymer dispersions made from (meth)acrylates having long side chains that can be used as paraffin inhibitors and have good low-temperature applicability here.
Flow aids are commonly used to improve the flow properties of crude oils and/or mineral oil fractions. They are especially necessary for allowing the flowability of the oil even at low temperatures, at which the untreated oil is already solid or viscous as a result of precipitation or crystallization of dissolved solid constituents, such as longer-chain paraffins and/or asphaltenes, or a of solid deposits occurs which, for example, lead to a narrowing of the pipelines.
Here, the flow aid can lower the pour point of the (crude) oil, and this prevents solidification of the oil below a certain temperature. In this case, the flow improver acts as a co-called pour point depressant.
Furthermore, the flow aid can lead to an inhibition or reduction of paraffin deposits on (cold) surfaces (e.g., the inner wall of pipelines). In this case, the flow aid acts as a so-called paraffin inhibitor. One or else both of these properties may be important, depending on the (crude) oil.
The performance of a flow aid is to be rated according to its ability to shift the pour point of the oil to lower temperatures and/or its ability to reduce the amount of deposited wax on (cold) surfaces.
Polymers which have long side chains (i.e. alkyl side chains≥C16) and act as crystallization inhibitors by cocrystallization with the longer-chain paraffins are commonly used as flow aids. The aforementioned polymers are commonly (co)polymers of (meth)acrylates having long side chains of the general formula (1)
where R=CnH2n+1 with n≥16 and R′=CH3 or H. Since such polymers are present as solids at the customary use temperatures, but must be distributed as homogeneously as possible in the oil in the end use, they are customarily used as solutions in organic solvents, usually in aromatic organic solvents. Besides the negative properties due to said organic solvents such as flammability and toxicity, such polymer solutions have further disadvantages. For instance, the flow aids themselves are not pourable at low temperatures owing to the side-chain crystallization of the polymers, and this hampers or prevents metering at low temperatures into the oil to be treated. To counteract this problem, either the tank farms and supply lines for metering the flow aid can be heated, this being associated with high energy costs, or the inherent pour point of the flow aid can be lowered in a certain range by further dilution with organic solvent to <10% active content. This however likewise being associated with high additional costs (solvent costs, transport costs, greater need of storage space, additional safety measures due to the flammability of the solvents).
To circumvent this problem, polymer dispersions in a continuous phase (e.g. water or mixtures of water with a water-miscible solvent) can be used instead of polymer solutions in organic solvents.
The advantage of this is that the viscosity and the flow behaviour of the formulation are hardly dependent on the properties and the amount of the polymer in the disperse phase, but are instead substantially dependent on the properties of the continuous phase. This allows, firstly, the use of highly concentrated formulations which can be pumped to their site of use without any problems owing to their low viscosity even at very low temperatures. Secondly, when selecting the polymers, the solubility behaviour thereof in organic solvents need not be heeded; instead, when selecting the polymers, it is possible to focus more on the performance as flow improver.
The laid-open specifications 9833846 A1, US20100025290 A1 and WO2019057396 A1 describe the preparation of such dispersions in the form of a secondary dispersion. This is a multistage process in which polymerization in organic solvent takes place first of all, followed by dispersion into a continuous phase. To generate the secondary dispersion with small particle sizes, what is necessary here is a high degree of shearing (e.g. via Ultraturrax, high-pressure homogenizer, ultrasound) in order to achieve a sufficient stability of the dispersions, this being complicated on an industrial scale. Where appropriate, it is moreover necessary at the end to distil off the organic solvent.
WO2019048663A1 and WO2017153462A1 describe the preparation of such dispersions via a so-called mini-emulsion polymerization. In this case, very small monomer droplets are formed before the actual polymerization with the aid of high shear rates (e.g. ultrasound treatment or high-pressure homogenization) in an aqueous phase, which are then subsequently converted to polymer particles by polymerization. However, such a process can only be implemented with difficulty on an industrial scale and is moreover very costly.
A further possibility is the direct preparation of a polymer dispersion by emulsion polymerization. Whereas aqueous emulsion polymerization is widespread for a multiplicity of different monomers, this type of polymerization is a challenge for (meth)acrylates having long side chains (i.e. alkyl side chains≥C16) owing to the hydrophobicity of these monomers. Therefore, stable, low-coagulate dispersions cannot be prepared with these monomers via standard emulsion polymerization recipes, as used for the synthesis of water-based coating resins for example. A successful emulsion polymerization of such monomers requires a particular reaction regime in combination with particular additives in order to allow transport of the hydrophobic monomers through the continuous phase during the polymerization and to obtain at the end a stable dispersion which has low amounts of coagulate and moreover remains stable over a broad temperature range.
DE3830913 describes the preparation of such polymer dispersions by emulsion polymerization. To obtain a low-coagulate and storage-stable dispersion, a high amount of ethylenically unsaturated mono- and/or dicarboxylic acid or anhydrides thereof must be used as comonomer. These large amounts of comonomer that must be used for stabilization lead to restrictions in the choice of copolymerization composition with regard to the effect as flow improver. For instance, an amount of 20% to 40% by weight of ethylenically unsaturated monocarboxylic acid or 5% to 20% by weight of dicarboxylic acids is required in order to obtain a stable, low-coagulate dispersion. Although the required amount can be additionally reduced by the incorporation of a third monomer component (of a (meth)acrylate having a short side group), this too leads to a great restriction with regard to the choice of copolymer composition.
The correct copolymer composition is, however, critical in many cases for the end use as flow improver in different (crude) oils. A good prediction of which polymer composition exhibits the optimal effect in which oil is not possible to date, since the exact mechanisms of action for pour point depression and paraffin inhibition, or improving the flow properties, have not been clarified. Therefore, the optimal polymer composition must generally be adapted empirically to the particular oil to be treated.
The preparation of stable polymer dispersions in which the polymers consist of a high proportion of (meth)acrylates having side chains≥C16 is not possible via the method described in the patent. Moreover, storage stability tests were only done at room temperature. Storability and/or pumpability at low temperatures were therefore not shown, though this is critical for the end use.
U.S. Pat. No. 7,790,821 B2 likewise describes the preparation of polymer dispersions made from acrylates having long side chains that are prepared via free-radical emulsion polymerization. In this case, the use of unsaturated mono- or dicarboxylic acids as stabilizing comonomers can be dispensed with, thereby achieving a higher flexibility with respect to the polymer composition. Besides the use of an emulsifier, the stabilization of the dispersion is achieved by a water-miscible cosolvent in the continuous phase of the dispersion.
However, it became apparent that a polymer dispersion prepared via this process and based on behenyl (meth)acrylate (C18 to C22 side chain) has a high amount of coagulate and is therefore difficult to filter. Moreover, the dispersions thus obtained were not found to be storage-stable, and they therefore cannot be used as paraffin inhibitors and/or pour point depressants in crude oils.
It is therefore an object of the invention to provide improved polymer dispersions for use as paraffin inhibitors and/or pour point depressants that have high contents of polymers having long side chains (i.e. alkyl side chains≥C16), that can be processed easily and that simultaneously have a high stability and flowability over a broad temperature range, and that especially remain applicable/pumpable even at low temperatures (<0° C.).
Said object is achieved by a polymer dispersion containing
The invention further relates to a process for preparing such a polymer dispersion by free-radical emulsion polymerization in water in the presence of at least one cosolvent and in the presence of an emulsifier system comprising at least one emulsifier from the group of the sulfosuccinates.
The invention further relates to the use of the polymer dispersion for inhibiting the deposition of paraffins in crude mineral oils and/or for lowering the pour point of crude mineral oils.
In the studies forming the basis of the invention, it was found that, surprisingly, use of an emulsifier system comprising at least one emulsifier from the group of the sulfosuccinates in combination with small amounts (1.0 to 8.0, preferably 2.0 to 5.0 parts by weight) of an unsaturated carboxylic acid as comonomer yields a polymer dispersion based on alkyl (meth)acrylates having long side chains (i.e. alkyl side chains≥C16) that has very low amounts of coagulate, can be easily filtered and moreover remains stable and flowable over a broad temperature range and especially has a good low-temperature applicability.
Sulfosuccinates (general formula 4) are surface-active metal salts of the mono- or diesters of sulfosuccinic acid. Mono- and diesters are equally suitable in principle for the polymer dispersion according to the invention. The metal salts are usually alkali metal or alkaline earth metal salts, especially sodium salts. Sulfosuccinates are used industrially as wetting agents and dispersants.
where M+=metal salt (e.g. alkali metal ion or 1/2 alkaline earth metal ion), RV & RVI=mutually independently alkyl, aryl, aralkyl or alkylaryl radicals or RVII(O—CH2—CH2)n, wherein RVII=alkyl, aryl, aralkyl or alkylaryl radicals.
The invention relates to a polymer dispersion containing or consisting of
A particular embodiment of the present invention relates to a polymer dispersion containing or consisting of
A further particular embodiment of the present invention relates to a polymer dispersion containing or consisting of
A further particular embodiment of the present invention relates to a polymer dispersion containing or consisting of
The expression (meth)acrylate as used in the context of this invention signifies the esters of (meth)acrylic acid and means here both methacrylate, such as, for example, methyl methacrylate, ethyl methacrylate, etc., and acrylate, such as, for example, methyl acrylate, ethyl acrylate, etc., and also mixtures of the two.
The units of the copolymers present in the polymer dispersion are derived from the components (a1) to (a4).
The monomer from the group of the alkyl (meth)acrylates (a1) is preferably behenyl (meth)acrylate, a mixture of C18, C20 and C22 (meth)acrylate (e.g. BEMA 1822 F and BEA 1822 from BASF; VISIOMER® C18-22-MA).
The unsaturated monocarboxylic acids, dicarboxylic acids, or salts thereof or acid anhydrides thereof (a2) are preferably compounds having chain lengths<C10. (Meth)acrylic acid and derivatives thereof are particularly preferred.
The at least one emulsifier from the group of the sulfosuccinates is preferably a dialkyl sulfosuccinate emulsifier. The alkyl group can be linear or branched or contain an aliphatic ring. Examples of suitable alkyl radicals (hydrophobic groups) are isobutyl, isohexyl, cyclohexyl, 2-ethylhexyl, isooctyl, isodecyl, and isotridecyl. In the case of diesters, the alkyl groups are preferably identical.
The at least one emulsifier from the group of the sulfosuccinates is preferably selected from the group consisting of sodium bis(2-ethylhexy) sulfosuccinate, sodium bistridecyl sulfosuccinate, sodium bisisooctyl sulfosuccinate, sodium biscyclohexyl sulfosuccinate, sodium bisoctyl sulfosuccinate, sodium diamyl sulfosuccinate, sodium diisobutyl sulfosuccinate, sodium dihexyl sulfosuccinate, disodium lauryl sulfosuccinate, disodium salt of ethoxylated nonylphenol sulfosuccinate, disodium ethylhexyl sulfosuccinate, and disodium N-octadecyl sulfosuccinate, and also analogous salts with other counterions such as Li+, K+, Mg2+, Ca2+, Sr2+, Ba2+, etc. (commercial products: for example Aerosol TR-70, TR-60, OT-75, GPG, OT-70, OT-100, MA-80, A196, AY-65, AY-100, IB-45, A-103 from Solvay; Tritonm GR-5M, GR-7M from Dow). In addition, sulfosuccinamates such as, for example, disodium N-octadecyl sulfosuccinamate (commercial products: for example, Aerosol 18P from Solvay) can also be used.
In one embodiment of the invention, the emulsifier system (b) contains a sulfosuccinate having at least one C10 to C15 alkyl radical and also a further sulfosuccinate having a C<10 alkyl radical. Preferably, the C10 to C15 alkyl radical is tridecyl and/or the C<10 alkyl radical is 2-ethylhexyl.
In one embodiment of the invention, the emulsifier system contains the emulsifiers sodium bis(2-ethylhexy) sulfosuccinate and sodium bistridecyl sulfosuccinate.
Sodium bis(2-ethylhexy) sulfosuccinate and sodium bistridecyl sulfosuccinate are preferably used in the ratio of 1:10 to 10:1, particularly preferably in the ratio of 1:1.
Furthermore, the emulsifier system can contain a solvent or a solvent mixture, for example alcohol (e.g. ethanol), water or mixtures of alcohols and water (e.g. an ethanol/water mixture). Quantitative ratios are usually chosen such that a liquid emulsifier system is obtained. Typical quantitative ratios between emulsifier and solvent are 1:1 to 4:1.
The water-miscible cosolvent(s) is/are preferably selected from the group consisting of short-chain alcohols, dialcohols, trialcohols, glycols and glycol ethers, ketones, and ethers. Examples of particularly suitable short-chain alcohols are butanol or isopropanol; examples of suitable dialcohols are 1,3-propanediol, 1,2-propanediol, neopentyl glycol; an example of a suitable thioalcohol is glycerol; examples of suitable glycols are ethylene glycol or propylene glycol, diethylene glycol or dipropylene glycol, polyethylene glycol having an average molar mass up to approx. 600 g/mol; examples of suitable glycol ethers are methyl glycol, ethylene glycol monoethyl ether, ethylene glycol monopropyl ether, ethylene glycol monoisopropyl ether, ethylene glycol monobutyl ether, ethylene glycol monobenzyl ether, diethylene glycol monomethyl ether, diethylene glycol monoethyl ether, butyl diglycol, 1-methoxy-2-propanol, ethoxypropanol, propylene glycol monobutyl ether, dipropylene glycol methyl ether, polyalkylene glycol ether of the general formula CnH2n+1(OCH2—CH2)mOH with n=0 to 5 and m=0 to 20, ethylene glycol dimethyl ether; examples of suitable ketones are acetone or methyl ethyl ketone; an example of a suitable ether is 1,4-dioxane.
The further emulsifiers (d) are emulsifiers which do not belong to the group of the sulfosuccinates. Said emulsifiers can be ionic or non-ionic.
The further emulsifier(s) is/are preferably selected from the group of the water-in-oil emulsifiers (W/O emulsifiers) or mixtures of these emulsifiers preferably having a Griffin HLB value of less than 9 or mixtures yielding together an HLB value of less than 9.
The Griffin HLB value is calculated via the formula
HLB=20*(1−(MI/M)),
where MI corresponds to the molar mass of the hydrophobic part of the molecule and M corresponds to the total molar mass of the molecule.
The further components (e) can, for example, be buffers, residues of polymerization initiators or chain transfer agents, biocides or defoamers.
After synthesis, the polymer dispersions according to the invention have a low amount of coagulate (<1%, preferably <0.5%, particularly preferably <0.2%), are easily filterable and are simultaneously readily flowable over a broad temperature range (≥+30° C. to ≤−10° C.; preferably ≥+30° C. to ≤−15° C.; particularly preferably ≥+30° C. to ≤−20° C.).
A sufficiently good flowability corresponds to a viscosity of <1000 mPa*s (preferably <500 mPa*s) at a shear rate of 100 s−1.
The invention further relates to a process for preparing a polymer dispersion as described above by free-radical emulsion polymerization in water in the presence of at least one cosolvent and in the presence of an emulsifier system comprising at least one emulsifier from the group of the sulfosuccinates.
Thus, in the process according to the invention, copolymers (10 to 70 parts by weight), the units of which are derived from
Initiators selected from the group consisting of peroxides, organic hydroperoxides, peracids, peroxodisulfates and azo initiators are preferably used for said free-radical emulsion polymerization.
Initiators (“radical initiators”) are known from the prior art. The radical initiators in the context of the invention that can be used are all commercially available initiators, for example azo compounds such as N,N-azobisisobutyronitrile (AIBN) and peroxides or peroxide derivatives, it being possible to use them individually or in a mixture. Examples of suitable peroxides or peroxide derivatives are benzoyl peroxides, such as dibenzoyl peroxide (BPO), dicumyl peroxide, tert-butyl cumyl peroxide, lauroyl peroxide, tert-butyl perbenzoate, tert-butyl peroxy-2-ethylhexanate and/or tert-butylperoxy isopropyl carbonate, or peracids, organic hydroperoxides or peroxodisulfates. Preference is given to using radical initiators which are soluble in water or in a mixture of water and cosolvent, such as, for example, potassium peroxodisulfate, sodium peroxodisulfate, ammonium peroxodisulfate, 2,2′-azobis(2-methylpropionamidine) dihydrochloride, hydrogen peroxides or other hydroxy peroxides. Potassium peroxodisulfate (KPS) or ammonium peroxodisulfate (APS) is preferably used. Besides a thermal initiation of initiator decomposition, it is also possible to initiate initiator decomposition by a redox reaction (so-called redox polymerization) or by a UV initiator.
A chain transfer agent can be used for the free-radical emulsion polymerization. This is a chemical compound which leads to a reduction in the average molar mass of the polymers as a result of radical transfer reactions. The chain transfer agent used is preferably an alkyl mercaptan, for example dodecyl mercaptan, 2-mercaptoethanol or 2-ethylhexyl thioglycolate.
The polymerization can be carried out within a temperature range from 20° C. to 100° C., preferably at about 80° C. The reaction time is 0.5 to 5 h.
For pH regulation, a buffer substance, such as, for example, sodium tetraborate, sodium carbonate or acetate buffer, or a base, for example sodium hydroxide solution or ammonia solution, can be added.
To obtain a dispersion according to one embodiment of the invention, an ionic or non-ionic emulsifier selected from the group of the water-in-oil emulsifiers (W/O emulsifiers) or mixtures of these emulsifiers preferably having a Griffin HLB value of less than 9 or mixtures yielding together an HLB value of less than 9 can be added after completion of the polymerization.
The preparation of the dispersions can be carried out batchwise in a so-called batch process, in a feed process (so-called semi-batch process or fed-batch process), or via a continuous process. Preferably, the preparation is carried out via a batch or semi-batch process.
The polymer dispersion according to the invention can be used for inhibiting the deposition of paraffins in crude mineral oils and/or for lowering the pour point of crude mineral oils, and for pour point depression of crude mineral oil. To this end, a direct addition of the polymer dispersion can be made to the crude oil. Alternatively, a dilute composition of the dispersion can also be used. The above-described cosolvents or a mixture of cosolvent and water are especially suitable for further dilution of the dispersion.
The following examples elucidate the subject matter of the invention without restricting it.
1. Preparation of polyBEMA and polyBEA Solution Polymers (Comparative Examples):
The preparation of the solution polymers was carried out analogously to U.S. Pat. No. 6,218,490 B1, example 4.
A 500 ml four-neck flask fitted with a reflux condenser, propeller stirrer, stirrer motor (200 rpm), thermometer (PT100 digital thermometer) and nitrogen inlet tube for introducing nitrogen under the liquid surface was initially charged with 128.8 g of BEMA (VISIOMER® C18-22MA) and 90.6 g of solvent naphtha S, which were heated to 40° C. with the aid of an oil bath and stirred for 30 min. The mixture was heated to a bottom temperature of 100° C., and 0.822 g of tert-butyl perbenzoate in 15.0 g of solvent naphtha S was subsequently metered in over 90 min (0.176 g/min). After a total reaction time of 6 h, the batch was diluted with 115.0 g of solvent naphtha S to a total solids content of 37%.
The reaction was carried out under a nitrogen atmosphere (nitrogen flow rate ˜45 L/h), with the nitrogen being conducted below the liquid surface. The polymer solutions obtained have a solids content of approx. 37%.
Procedure carried out analogously to 1a, but 128.8 g of BEMA (VISIOMER® C18-22MA) and 205.6 g of solvent naphtha S were initially charged. No dilution with solvent naphtha S was carried out therefor after the polymerization.
The procedure was carried out analogously to comparative examples 1a and 1b, but with use of BEA (BASF Behenyl Acrylate 1822 F) instead of BEMA.
Dispersions of differing composition were prepared. The amounts used of the varied substances and the analytical characteristic data of the dispersions are listed in Table 2 and Table 3.
Apparatus: 1 L double jacket reactor fitted with reflux condenser, propeller stirrer, stirrer motor (200 rpm), and circulating constant-temperature bath, Testo data logger with Pt100 digital thermometer for temperature measurement in the reactor and in the circulating constant-temperature bath. The reaction was carried out under a nitrogen atmosphere (nitrogen flow rate ˜6 L/h), with the nitrogen being conducted below the liquid surface by means of a glass tube.
The polymer dispersions obtained all have a solids content of about 35%.
To show the flow behaviour during later application at different temperatures, rheological measurements were carried out as a function of temperature. To simulate the shearing strain on the polymer dispersions or solutions during application into a well, for example when metering in via a supply line, the measurements were carried out at a constant shear rate of 100 s−1. The measurements were started at +30° C. and cooled to −30° C. at a cooling rate of 1 K/min.
By using sodium bis(2-ethylhexy) sulfosuccinate as emulsifier, it is possible to achieve a flat viscosity profile over a broad temperature range (
The use of a mixture of sodium bistridecyl sulfosuccinate and sodium bis(2-ethylhexy) sulfosuccinate achieves similarly flat viscosity profiles (
To ascertain below which temperature the polymer solutions or dispersions become solid without action of a shearing force (e.g. during storage at low temperatures), the pour point was ascertained in accordance with ASTM D5985.
As can be seen in Table 4, the solution polymers 1a to 1d have a pour point>0° C. Dispersion 2d shows a pour point of 3° C. By contrast, the pour points of the dispersions 2e, 3b and 3f are distinctly below 0° C.
In the case of use at even lower temperatures, an additional investigation was done to determine whether the pour point can be further reduced by subsequent addition of dipropylene glycol methyl ether (DPM). These results as well are compiled in Table 4. Whereas the dispersion 2d cannot be readily diluted because the dispersion becomes inhomogeneous, the dispersions 2e and 3b can be diluted with DPM up to a ratio of approx. 1:1 without the dispersion being destabilized. As a result, the pour point can be distinctly reduced to as far as <−45° C.
To test the effect of the different polymer solutions and dispersions as pour point depressant, the pour point of different crude oils with and without addition of the polymers was ascertained in accordance with ASTM D5985. Here, the amount of added polymer solution or dispersion was chosen such that the same amounts of polymer were added in each case (100 and 1000 ppm in each case, based on the crude oil). In the case of the test in Texas crude oil (from Texas Raw Crude), 5% of a paraffin wax were added in order to artificially increase the amount of wax in the crude oil. This system served as the reference for the comparison of the different polymer solutions and dispersions. Furthermore, tests in a Caspian crude oil were carried out.
As can be seen in Table 5 and Table 6, approximately the same pour point depressions are achieved both in Texas crude oil and in Caspian crude oil with the polymer dispersions as with the corresponding solution polymers. Thus, the alternative form of administration of the polymers does not have an adverse effect on the effect thereof as pour point depressant. In the case of low metering rates (100 ppm), the dispersions achieve even greater pour point depressions than with the corresponding solutions in organic solvent.
To test the effect of the polymer dispersions and solutions as paraffin inhibitors, the so-called cold finger deposition test was carried out. Here, paraffin deposition from crude oil on a cold finger was tested, by comparing the amount of deposition with and without addition of polymer. The polymers were added in the form of solutions or dispersions. The specified amount is also based here on the pure polymer in order to ensure better comparability. From the weighed wax deposits, wax inhibition was calculated via the following formula:
Wax inhibition (%)=(w0−wx)/w0*100
where w0 corresponds to the wax deposit in g without addition of polymer and wx corresponds to the wax deposit in g with addition of polymer.
Table 7 shows the results of the cold finger deposition test for selected polymer dispersions in comparison with a corresponding solution polymer at a bath temperature of 37° C. and a finger temperature of 4° C. in Texas crude oil.
What can be seen is that both the polymer solutions and the dispersions lead to a distinct reduction in wax deposition and that they therefore act as wax inhibitors. Here, in the case of the same metered addition of polymer, the dispersions 2e and 3b even achieved a higher wax inhibition than the polymer solution 1a.
To investigate whether the dispersions have a sufficient storage stability under different ambient conditions, freezing stability, warm-storage stability and storage stability at room temperature were tested.
Samples of 245 g each were weighed in 250 mL PE wide-neck bottles and cooled to −20° C. in a freezer. After 16 h at this temperature, thawing was carried out at 23° C. for 4 h in a constant-temperature bath and the pasty polymers were stirred using a propeller stirrer (500 rpm) for 30 min. Thereafter, an optical check for coagulate, specks and inhomogeneity was carried out, the polymers were filtered across a sieve fabric (Schnellsieb 125 μm) and the coagulate was weighed. After a further 2 hours of holding the temperature at 23° C., Brookfield viscosity and particle size were determined. This cycle of freezing and thawing was repeated 5 times.
The results are compiled in Table 8. What can be seen is that, in the case of the dispersion 2d, a distinct rise in Brookfield viscosity and in particle size already occurs after the first freeze-thaw cycle. Moreover, significant amounts of coagulate are formed in every cycle. In the case of the dispersions 2k, 3d and 3f, no coagulate can be seen in the filter with the naked eye, and the weighed amounts of coagulate are very low. Viscosity and particle size, too, remain unchanged in said dispersions within the limit of measurement accuracy.
Although dispersions made from BEA or BEMA as monomer can be prepared in accordance with example 1 of U.S. Pat. No. 7,790,821 B2 (examples 2a and 2c), they contain large amounts of coagulate and are very difficult to filter, this being unfavourable for commercial use. In example 2a, there was even the occurrence of a complete coagulation of the dispersion.
Just by copolymerization with small amounts of methacrylic acid (1%) (example 2d), it is possible to prepare dispersions containing at least one sulfosuccinate emulsifier that have low amounts of coagulate. By further increasing the amount of methacrylic acid to >1% (examples 2r, 2s, 2t, 2e, 2p and 2q), the amount of coagulate can be further reduced. Already the increase from 1 to 1.1% methacrylic acid reduces the amount of clot to <1%. At contents of 1.3% and higher, the filterability and the optical impression of the dispersion after filtration are also improved.
By a combination of two sulfosuccinate emulsifiers (sodium bistridecyl sulfosuccinate and sodium bis(2-ethylhexy) sulfosuccinate), it is possible to obtain dispersions which have a similar low-temperature flowability as the dispersions containing only sodium bis(2-ethylhexy) sulfosuccinate, but moreover contain a distinctly lower amount of coagulate than dispersions containing only one emulsifier. Moreover, the dispersions can be easily filtered and have only a low amount of specks after filtration.
At the same metered addition, the dispersions can achieve comparable pour point depressions of crude oils as comparable solution polymers, but with the advantage that the dispersions can additionally be metered in at distinctly lower temperatures owing to their flow behaviour.
5 g of sample were dried to constant weight in an aluminium dish in a vacuum drying cabinet at 80° C. for approx. 3 days.
The polymers were adjusted in temperature to 23° C. in a constant-temperature water bath, and dynamic viscosity was measured using a Brookfield rotary viscometer LVT DV II with guard leg at a rotational speed of 60 rpm with spindle I.
pH:
pH was measured using the pH meter Calimatic 761 from Knick, comprising a pH/Pt-100 glass combination electrode with ceramic diaphragm and 3 M KCl filling.
Particle size was measured using the Delsa Nanosizer from Beckmann Coulter (rDNC). The sample was diluted with distilled water before measurement.
The polymers (approx. 5 g) were dried in aluminium dishes in a vacuum drying cabinet at 80° C. for 3 days. Molar mass distribution was ascertained on the dried polymers by means of GPC (polymer standard for calibration: PMMA). The weight-average and the number-average molar mass (Mw and Mn) of the polymers were determined therefrom.
The pour points of the polymer solutions and polymer dispersions and of the crude oils doped with the polymers were measured in accordance with ASTM D5985 using a pour point tester PPT 45150 from PSL Systemtechnik. The measurement yields the “no flow point” with a measurement accuracy of 0.1° C. The “no flow point” was determined as the mean of a triplicate determination. From the “no flow point”, the pour point was then calculated in accordance with ASTM D97.
Cold Finger Deposition Test (Reduction in Wax Deposition from Crude Oils on Cold Surfaces by Addition of Polymer):
The cold finger deposition test was carried out using a cold finger deposition tester from PSL Systemtechnik (model CF15120).
Here, 80 mL of the mixture of crude oil+polymer solution or dispersion are heated to the desired bath temperature (e.g. 37° C.) and stirred continuously at the same time. The cold finger is immersed into the sample, with the result that the wax present deposits on the finger surface little by little. After certain time intervals (e.g. after 3 and 22 h), this amount of wax is determined by weighing. The cold finger is kept at a desired finger temperature (e.g. 4° C.) here. The chosen bath and finger temperature simulate here the passage of a warm oil through a pipeline having a cold surface (e.g. in winter or in the deep sea).
The change in viscosity as a function of temperature was measured using an Anton Paar rheometer MCR302 with cone-plate geometry CP50-1 (diameter 50 mm, cone angle 1°) with TrueGap. Measurement was carried out at a constant shear rate of 100 s−1 and a cooling rate of 1 K/min over a temperature range of +30 to −30° C. measurement range.
Wax content and WAT were determined by means of DSC. Measurement was carried out here with a cooling rate of 2 K/min.
| Number | Date | Country | Kind |
|---|---|---|---|
| 20165758.2 | Mar 2020 | EP | regional |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/EP2021/057732 | 3/25/2021 | WO |
