CN109503825B

CN109503825B - Production method of high ethylene oxide addition number secondary alcohol polyoxyethylene ether

Info

Publication number: CN109503825B
Application number: CN201811378187.3A
Authority: CN
Inventors: 徐兴建; 张江锋; 陈静; 王建臣; 侯海育
Original assignee: Shanghai Duolun Chemical Co Ltd
Current assignee: Shanghai Duolun Chemical Co Ltd
Priority date: 2018-11-19
Filing date: 2018-11-19
Publication date: 2022-02-01
Anticipated expiration: 2038-11-19
Also published as: CN109503825A

Abstract

The production method of the high-ethylene-oxide-adduct secondary alcohol polyoxyethylene ether comprises the following steps of reacting the low-ethylene-oxide-adduct secondary alcohol polyoxyethylene ether with ethylene oxide under the catalysis of alkali to obtain the high-ethylene-oxide-adduct secondary alcohol polyoxyethylene ether, wherein the low-ethylene-oxide-adduct secondary alcohol polyoxyethylene ether is prepared by adopting a preparation method comprising the following steps: in the presence of an acid catalyst, secondary alcohol reacts with ethylene oxide to obtain a crude product 1 of low-ethylene-oxide-adduct secondary alcohol polyoxyethylene ether; mixing the crude product 1 with water, standing above cloud point for layering to obtain an oil phase crude product 2; distilling under reduced pressure to remove secondary alcohol contained in the crude product 2 and crude product 3; mixing the crude product 3 with water to obtain a mixture A; uniformly mixing the mixture A and a fluorine boron remover to obtain a mixture B; removing water in the mixture B to obtain a mixture C; and mixing the mixture C with a filter aid, and filtering to obtain the refined low ethylene oxide adduct secondary alcohol polyoxyethylene ether.

Description

Production method of high ethylene oxide addition number secondary alcohol polyoxyethylene ether

Technical Field

The invention relates to a method for producing polyoxyethylene ether with high ethylene oxide addition number secondary alcohol.

Background

The secondary alcohol polyoxyethylene ether is almost colorless, tasteless and transparent liquid at normal temperature, has lower flow point and viscosity than primary alcohol nonionic surfactants, and is convenient to use. The application field of the secondary alcohol polyoxyethylene ether is wide, the depth and the breadth are continuously expanded, and the market demand is rapidly increasing. Limited by technology and scale, the quality is basically poor, the quantity is small, and the price is high at present, and if the situation is solved, the core competitiveness of domestic products is enhanced.

In the secondary alcohol epoxidation reaction, the research and research of the catalyst, the reaction conditions, the reaction kinetics, the reaction form, the separation and purification method of epoxide, the quality of the finished product and other problems are intensively researched, and because the hydroxyl group of the secondary alcohol is different from the primary alcohol in structure and chemical characteristics, when the secondary alcohol is added with ethylene oxide, if a basic catalyst is used, the reaction speed is lower, the distribution range of ethoxy in the addition product is very wide, and alcohol ethoxylate can not be prepared in practice, so that the selection of the secondary alcohol ethoxylation catalyst generally selects Friedel-Crafts type acid catalysts such as BF at home and abroad₃、BF₃Etherate, AlCl₃、H₂SO₄、HClO₄、H₃PO₄Etc. in which BF is set₃The ether solution is most suitable, in the presence of an acidic catalystThen, the ethoxylation reaction of the secondary alcohol is fast to prepare the secondary alcohol ethoxylation compound.

However, the by-products produced by the existing preparation method include dioxane, residual fluorine element, boron element, carbonyl aldehyde compound produced in the reaction process, free unreacted alcohol and the like, especially residual fluorine element and boron element, and when secondary alcohol polyoxyethylene ether prepared by a boron fluoride-containing acidic catalyst is used as an initiator to catalyze the addition of ethylene oxide, the product of secondary alcohol polyoxyethylene ether with higher ethylene oxide addition number obtained by alkali catalysis is high in chroma and turbid in appearance, so that the application range of the product is limited.

Disclosure of Invention

The invention mainly solves the technical problems of high fluorine and boron impurity content and deep color of high-ethylene oxide adduct secondary alcohol polyoxyethylene ether obtained by the existing secondary alcohol polyoxyethylene ether preparation method, and provides a novel secondary alcohol polyoxyethylene ether preparation method which has the advantages of low fluorine and boron impurity content, light color and high transparency.

In order to solve the technical problems, the technical scheme of the invention is as follows:

the production method of the high-ethylene-oxide-adduct secondary alcohol polyoxyethylene ether comprises the following steps of reacting the low-ethylene-oxide-adduct secondary alcohol polyoxyethylene ether with ethylene oxide under the catalysis of alkali to obtain the high-ethylene-oxide-adduct secondary alcohol polyoxyethylene ether, wherein the low-ethylene-oxide-adduct secondary alcohol polyoxyethylene ether is prepared by adopting a preparation method comprising the following steps:

(1) in the presence of an acid catalyst, secondary alcohol reacts with ethylene oxide to obtain a crude product 1 of low-ethylene-oxide-adduct secondary alcohol polyoxyethylene ether; the acidic catalyst comprises boron trifluoride;

(2) mixing the crude product 1 of the low-ethylene oxide adduct secondary alcohol polyoxyethylene ether with water, standing and layering above the cloud point of the low-ethylene oxide adduct secondary alcohol polyoxyethylene ether to obtain an oil phase, wherein the oil phase is the crude product 2 of the low-ethylene oxide adduct secondary alcohol polyoxyethylene ether;

(3) carrying out reduced pressure distillation to remove the secondary alcohol which is not reacted in the step (1) and is contained in the low-ethylene-oxide-adduct secondary alcohol polyoxyethylene ether crude product 2, so as to obtain a low-ethylene-oxide-adduct secondary alcohol polyoxyethylene ether crude product 3;

(4) mixing the crude product 3 of low ethylene oxide adduct secondary alcohol polyoxyethylene ether with water to obtain a mixture A;

(5) uniformly mixing the mixture A and a fluorine boron remover to obtain a mixture B;

(6) removing water in the mixture B through heat and/or vacuum treatment to obtain a mixture C;

(7) mixing the mixture C with a filter aid, and filtering to obtain refined low ethylene oxide adduct secondary alcohol polyoxyethylene ether;

the fluorine boron remover comprises at least one selected from the group consisting of sodium hydroxide, potassium hydroxide, calcium oxide, calcium carbonate, magnesium hydroxide, magnesium oxide, magnesium carbonate, aluminum hydroxide, aluminum oxide and aluminum carbonate;

the low ethylene oxide addition number secondary alcohol polyoxyethylene ether conforms to the following general formula:

R-(O-CH₂CH₂)_n-OH；

wherein R is a secondary alkyl group having 8 to 18 carbon atoms; n is the addition number of ethylene oxide, n is more than 0 and less than 6;

the molar ratio of ethylene oxide to secondary alcohol in the step (1) is Q, and n/Q is 0.25-12.

Because the boron-fluorine remover is used in the step (5), the content of fluorine and boron impurities in the refined low-ethylene-oxide-adduct secondary alcohol polyoxyethylene ether product is reduced, so that the content of fluorine and boron impurities in the high-ethylene-oxide-adduct secondary alcohol polyoxyethylene ether product is correspondingly reduced, and the obtained high-ethylene-oxide-adduct secondary alcohol polyoxyethylene ether product is light in color and high in transparency.

As non-limiting examples of the carbon content of R, 8, 9, 10, 11, 12, 13, 14, 15, 16, 17, 18, etc. The secondary alcohol can be a secondary alcohol with a single carbon number in the range of C8-C18, or a mixture of more than two of the substance group consisting of secondary alcohols with carbon numbers of C8-C18.

As non-limiting examples of n, n can be 0.5, 0.8, 1, 1.2, 1.4, 1.6, 1.8, 2, 2.2, 2.4, 2.6, 2.8, 3, 3.2, 3.4, 3.6, 3.8, 4, 4.2, 4.4, 4.6, 4.8, 5.0, 5.2, 5.4, 5.6, 5.8, and so forth. However, n is preferably 1 to 3.

By way of non-limiting examples of n/Q values, there are, but not limited to, 0.28, 0.5, 1, 1.5, 1.7, 2, 2.5, 3, 3.6, 4, 4.5, 5, 5.5, 6, 6.5, 7, 7.5, 8, 8.5, 9, 9.5, 10, 11, and the like.

The technical key point of the invention is the use of the boron fluoride remover in the step (5), and the reaction process conditions of the low-ethylene oxide adduct secondary alcohol polyoxyethylene ether and the ethylene oxide which react under the alkali catalysis to obtain the high-ethylene oxide adduct secondary alcohol polyoxyethylene ether are not particularly limited. Further, it is known to those skilled in the art that the refined low ethylene oxide adduct number secondary alcohol polyoxyethylene ether is terminated with a hydroxyl group, and those skilled in the art are well known for the reaction of a hydroxyl group-containing compound with ethylene oxide under alkaline conditions.

By way of non-limiting example, the base may be an alkali metal hydroxide and/or an alkali metal alkoxide of a C1-C2 alcohol.

In the above technical scheme, the alkali metal hydroxide is sodium hydroxide and/or potassium hydroxide which are commonly used.

In the technical scheme, the C1-C2 alcohol is preferably methanol and/or ethanol.

In the above technical scheme, the alkali metal alkoxide is preferably sodium alkoxide and/or potassium alkoxide.

As a non-limiting example, the amount of the base used in the reaction under base catalysis is 0.05 to 1% by weight of the polyoxyethylene ether of the high ethylene oxide adduct secondary alcohol. Such as but not limited to 0.10%, 0.2%, 0.3%, 0.4%, 0.5%, 0.6%, 0.7%, 0.8%, 0.9%, etc.

As a non-limiting example, the reaction pressure in the reaction under base catalysis is 0.05 to 0.5 MPa. Such as, but not limited to, 0.08MPa, 0.1MPa, 0.15MPa, 0.2MPa, 0.25MPa, 0.30MPa, 0.35MPa, 0.40MPa, 0.45MPa, and the like.

As a non-limiting example, the reaction temperature in the reaction under base catalysis is 95-170 ℃. For example, but not limited to, 100 ℃, 115 ℃, 120 ℃, 125 ℃, 130 ℃, 135 ℃, 140 ℃, 145 ℃, 150 ℃, 155 ℃, 160 ℃, 165 ℃, etc.

In the above technical scheme, the high ethylene oxide adduct secondary alcohol polyoxyethylene ether preferably conforms to the following general formula:

R-(OCH₂CH₂)_mOH；

wherein m is the ethylene oxide addition number of the high ethylene oxide addition number secondary alcohol polyoxyethylene ether, and m is less than or equal to 50.

The size of m is not particularly limited as long as it is larger than the specific value of n, and m.ltoreq.50 is merely preferable. Non-limiting examples of values for m are 4, 5, 6, 7, 8, 9, 10, 15, 20, 25, 30, 35, 40, 45, etc.

In the technical scheme, m is preferably 4-50.

In the above technical scheme, the specific process conditions of step (1) are not particularly limited, and those skilled in the art can reasonably select, for example, but not limited to:

the acidic catalyst can be boron trifluoride;

the dosage of the acid catalyst can be 0.05-1% of the weight of the low ethylene oxide adduct secondary alcohol polyoxyethylene ether crude product 1; such as, but not limited to, 0.10, 0.15, 0.20, 0.25, 0.30, 0.35, 0.40, 0.45, 0.50, 0.55, 0.60, 0.65, 0.70, 0.75, 0.80, 0.85, 0.90, 0.95, and the like.

The pressure of the reaction in the step (1) can be 0-0.5 MPa; such as, but not limited to, 0.05, 0.10, 0.15, 0.20, 0.25, 0.30, 0.35, 0.40, 0.45, etc.

The reaction temperature in the step (1) can be selected from 10-120 ℃; such as, but not limited to, 20, 25, 30, 35, 40, 45, 50, 55, 60, 65, 70, 75, 80, 85, 90, 95, 100, 105, 110, 115, and the like.

As known to those skilled in the art, boron trifluoride is a gas at normal temperature in pure state, and is inconvenient to use, store and transport. In order to solve the problem of convenient use and storage and transportation, boron trifluoride is usually dissolved in solvents such as alcohol, ether and ketone for storage and transportation. Such as, but not limited to, boron trifluoride, which may be present in a concentration of 10 to 50% by weight (e.g., boron trifluoride may be present in a concentration of 15%, 20%, 25%, 30%, 35%, 40%, 45%, etc.). The boron trifluoride used in the embodiments of the invention was boron trifluoride etherate in a concentration of 46.5% by weight of boron trifluoride, but the metering was still carried out as boron trifluoride.

In the above technical scheme, the amount of water used in step (2) is not particularly limited as long as the amount required for static demixing is above the cloud point of the low ethylene oxide adduct secondary alcohol polyoxyethylene ether, and those skilled in the art can reasonably select the water without creative work. But the mass ratio of the crude product 1 of the low ethylene oxide adduct secondary alcohol polyoxyethylene ether in the step (2) to water is preferably 0.2-20. Such as, but not limited to, 0.5, 1, 1.5, 2, 2.5, 3, 3.5, 4, 4.5, 5, 5.5, 6, 6.5, 7, 7.5, 8, 8.5, 9, 9.5, 10, 12, 15, 17, 19, etc.

For those skilled in the art, in the above technical scheme, the temperature for mixing and the mixing time in the step (2) are not particularly required, and those skilled in the art can reasonably select the temperature without creative efforts.

In the above technical scheme, the process conditions for the distillation under reduced pressure in the step (3) are not particularly limited, and can be reasonably selected by a person skilled in the art. Preferably, the distillation temperature is lower than the thermal decomposition temperature of the secondary alcohol polyoxyethylene ether, and is generally controlled to be below 180 ℃, such as 140-180 ℃, further non-limiting examples are 145 ℃, 150 ℃, 155 ℃, 160 ℃, 165 ℃, 170 ℃, 175 ℃ and the like; the pressure (gauge pressure) of the distillation is preferably more than-0.1 MPa and not more than-0.090 MPa. Such as but not limited to-0.099 MPa, -0.098 MPa, -0.097 MPa, -0.096 MPa, -0.095 MPa, -0.094 MPa, -0.092 MPa, -0.091 MPa, etc.

In the technical scheme, the water consumption in the step (4) is 0.5-10% of the weight of the low ethylene oxide adduct secondary alcohol polyoxyethylene ether crude product 3. Such as but not limited to 1%, 1.5%, 2%, 2.5%, 3%, 3.5%, 4%, 4.5%, 5%, 5.5%, 6%, 6.5%, 7%, 7.5%, 8%, 8.5%, 9%, 9.5%, etc. Further preferably 1 to 5%.

For those skilled in the art, in the above technical solution, the temperature and mixing time for the step (4) are not particularly required, and those skilled in the art can reasonably select the temperature and mixing time without creative efforts.

As a non-limiting example, the mixing temperature in step (4) may be selected to be 25 to 100 ℃. In this temperature range, as the temperature point value in step (4), for example, but not limited to, 30 ℃, 35 ℃, 40 ℃, 55 ℃, 60 ℃, 65 ℃, 70 ℃, 75 ℃, 80 ℃, 85 ℃, 90 ℃, 95 ℃, and the like. More preferably 25 to 70 ℃.

The mixing time in the step (4) is not particularly limited, and those skilled in the art know that increasing the mixing time is beneficial to mixing, but generally the mixing time is controlled to be 10-100 minutes for economic purposes. Such as, but not limited to, 15 minutes, 20 minutes, 25 minutes, 30 minutes, 35 minutes, 40 minutes, 45 minutes, 50 minutes, 55 minutes, 60 minutes, 65 minutes, 70 minutes, 75 minutes, 80 minutes, 85 minutes, 90 minutes, 95 minutes, and the like; preferably 30 to 60 minutes.

In the technical scheme, the dosage of the boron fluoride remover in the step (5) is preferably 0.5-10 times of that of the acid catalyst in the step (1) by weight. Such as, but not limited to, 0.7 times, 0.9 times, 1 times, 1.2 times, 1.5 times, 2 times, 2.1 times, 2.2 times, 2.3 times, 2.4 times, 2.5 times, 2.6 times, 2.7 times, 2.8 times, 3 times, 3.5 times, 4 times, 4.5 times, 5 times, 5.5 times, 6 times, 6.5 times, 7 times, 7.5 times, 8 times, 8.5 times, 9 times, 9.5 times, and the like; more preferably 0.5 to 6 times; further 2-4 times; most preferably 2.9 to 3.5 times.

For those skilled in the art, in the above technical solution, the temperature and mixing time for the step (5) are not particularly required, and those skilled in the art can reasonably select the temperature and mixing time without creative efforts.

In the technical scheme, the mixing temperature in the step (5) can be selected to be 25-100 ℃. In this temperature range, the temperature point value for mixing in step (5) is, for example, but not limited to, 30 ℃, 35 ℃, 40 ℃, 55 ℃, 60 ℃, 65 ℃, 70 ℃, 75 ℃, 80 ℃, 85 ℃, 90 ℃, 95 ℃, and the like. More preferably 25 to 70 ℃.

The mixing time in the step (5) is not particularly limited, and those skilled in the art know that increasing the mixing time is beneficial to mixing, but generally the mixing time is controlled to be 10-180 minutes for economic purposes. Such as, but not limited to, 15 minutes, 20 minutes, 25 minutes, 30 minutes, 35 minutes, 40 minutes, 45 minutes, 50 minutes, 55 minutes, 60 minutes, 65 minutes, 70 minutes, 75 minutes, 80 minutes, 85 minutes, 90 minutes, 95 minutes, 100 minutes, 105 minutes, 110 minutes, 115 minutes, 120 minutes, and the like. More preferably 60 to 120 minutes.

In the above technical solution, the specific process conditions of the heat and/or vacuum treatment in step (6) for removing water from the mixture B are not particularly limited, and can be reasonably selected by those skilled in the art without creative efforts.

In the above technical solution, for the step (6) of simultaneously performing the heat treatment and the vacuum treatment, the treatment temperature is preferably 50 to 200 ℃. For example, but not limited to, 55 deg.C, 60 deg.C, 65 deg.C, 70 deg.C, 75 deg.C, 80 deg.C, 85 deg.C, 90 deg.C, 95 deg.C, 100 deg.C, 105 deg.C, 110 deg.C, 115 deg.C, 120 deg.C, 125 deg.C, 130 deg.C, 135 deg.C, 140 deg.C, 145 deg.C, etc.

In the above technical solution, for the step (6) of simultaneously applying heat and vacuum, the pressure of the treatment is greater than-0.1 MPa and less than 0MPa, such as but not limited to-0.099 MPa, -0.098 MPa, -0.097 MPa, -0.095 MPa, -0.093 MPa, -0.090 MPa, -0.085 MPa, -0.08 MPa, -0.075 MPa, -0.07 MPa, -0.065 MPa, -0.06 MPa, -0.055 MPa, -0.05 MPa, -0.045 MPa, -0.04 MPa, -0.035 MPa, -0.03 MPa, -0.025 MPa, -0.02 MPa, -0.015 MPa, -0.01 MPa, etc.; preferably-0.098 MPa to-0.05 MPa.

In the above technical solution, for the step (6) of simultaneously performing the heat treatment and the vacuum treatment, the treatment time is preferably 30 to 300 minutes. Such as, but not limited to, 40 minutes, 50 minutes, 60 minutes, 70 minutes, 80 minutes, 90 minutes, 100 minutes, 110 minutes, 120 minutes, 130 minutes, 140 minutes, 150 minutes, 160 minutes, 170 minutes, 180 minutes, 190 minutes, 200 minutes, 210 minutes, 220 minutes, 230 minutes, 240 minutes, 250 minutes, 260 minutes, 270 minutes, 280 minutes, 290 minutes, and the like.

For those skilled in the art, in the above technical scheme, the temperature for mixing in the step (7) and the mixing time are not particularly required, and those skilled in the art can reasonably select the temperature without creative efforts.

The mixing time in the step (7) is not particularly limited, and those skilled in the art know that increasing the mixing time is beneficial to mixing, but generally the mixing time is controlled to be 30-120 minutes for economic purposes. Such as, but not limited to, 35 minutes, 40 minutes, 45 minutes, 50 minutes, 55 minutes, 60 minutes, 65 minutes, 70 minutes, 75 minutes, 80 minutes, 85 minutes, 90 minutes, 95 minutes, 100 minutes, 105 minutes, 110 minutes, 115 minutes, 120 minutes, 125 minutes, and the like. More preferably 60 to 90 minutes.

In the technical scheme, the mixing temperature in the step (7) can be 20-150 ℃. For example, but not limited to, 25 ℃, 30 ℃, 35 ℃, 40 ℃, 55 ℃, 60 ℃, 65 ℃, 70 ℃, 75 ℃, 80 ℃, 85 ℃, 90 ℃, 95 ℃, 100 ℃, 105 ℃, 110 ℃, 115 ℃, 120 ℃, 125 ℃, 130 ℃, 135 ℃, 140 ℃, 145 ℃, etc.

In the above technical solution, if the transparency of the product is sought, the filtration in the step (7), such as the filtration is not transparent, may be repeated for an unlimited number of times until the obtained filtrate is transparent, which is the best state.

In the above technical scheme, the amount of the filter aid is not particularly limited, and those skilled in the art can reasonably select the filter aid without creative work, for example, but not limited to, the amount of the filter aid is 0.1-1% of the mass of the mixture C.

In the above technical solution, the filter aid is not particularly limited, and may be reasonably selected by those skilled in the art without creative efforts, for example, the filter aid may be selected from at least one of the group consisting of activated clay, attapulgite, montmorillonite, kaolin, alunite, tuff, diatomaceous earth, magnesium silicate, perlite, silica, activated carbon, epoxy resin, 4A molecular sieve, γ -alumina, and ZSM-5 molecular sieve.

In the above technical solution, preferably, the fluorine and boron remover comprises calcium hydroxide and magnesium carbonate at the same time. We have found that when the boron fluoride remover comprises both calcium hydroxide and magnesium carbonate, the two have a synergistic effect in reducing the level of fluorine impurities, reducing the level of boron impurities and reducing the colour. At this time, the specific ratio of calcium hydroxide to magnesium carbonate is not particularly limited, and any ratio can achieve a comparable synergistic effect. For example, but not limited to, the weight ratio of calcium hydroxide to magnesium carbonate is 1-10, and non-limiting values within the weight ratio range may be 1.5, 2, 2.5, 3, 3.5, 4, 4.5, 5, 5.5, 6, 6.5, 7, 7.5, 8, 8.5, 9, 9.9, and the like. The weight ratio of the calcium hydroxide to the magnesium carbonate is further 1-8, and the weight ratio of the calcium hydroxide to the magnesium carbonate is further 3-5.

In the above technical solution, preferably, the boron fluoride remover comprises calcium hydroxide and aluminum carbonate at the same time. We have found that when the boron fluoride remover comprises both calcium hydroxide and aluminium carbonate, the two have a synergistic effect in reducing the level of fluorine impurities, reducing the level of boron impurities and reducing colour. At this time, the specific ratio of calcium hydroxide to aluminum carbonate is not particularly limited, and any ratio can achieve a comparable synergistic effect. For example, but not limited to, the weight ratio of calcium hydroxide to aluminum carbonate is 1-40, and non-limiting values within this weight ratio range may be 5, 10, 15, 20, 25, 30, 35, and so forth. The weight ratio of the calcium hydroxide to the aluminum carbonate is further selected from 5 to 30, and the weight ratio of the calcium hydroxide to the aluminum carbonate is further selected from 10 to 20.

The content of fluorine and boron in the specific embodiment of the invention, the analysis method respectively comprises:

1. determination of fluoride ion

1.1 principle

By using a lanthanum fluoride electrode as an indicating electrode and a saturated calomel electrode (or a silver chloride electrode) as a reference electrode, when fluorine ions exist in water, electrode response can be generated on a negative electrode.

The working cell is represented as follows:

when the total ion intensity in the water is controlled to be a fixed value, the electromotive force E of the battery changes along with the change of the concentration of the fluorine ions in the solution to be determined:

e and lgC_FIn a straight line relationship, 2.303RT/F is the slope of the line (59.1 at 25 ℃ C.)

The pH of the solution is measured to be 5-9. The effect of interfering ions and acidity is eliminated with a total ionic strength buffer solution.

The minimum detection concentration of the method is 0.05 mg fluorine/L, and the upper limit of the measurement can reach 4000 mg fluorine/L.

1.2 instruments

Precision acidimeter

Fluoride ion composite electrode

Electromagnetic stirrer

1.3, reagents

1.3.1, fluorine standard solution:

0.2210 g of sodium fluoride (dried at 500-650 ℃ for 40-45 minutes, dried and cooled) are weighed, dissolved in water, transferred into a 1000 ml volumetric flask and diluted to the marked line. This solution contained 100. mu.g fluorine per ml and was stored in a polyethylene bottle.

1.3.2 Total Ionic Strength buffer

Weighing 58.8 g of sodium citrate dihydrate and 85 g of sodium nitrate, adding water to dissolve, adjusting the pH to 5.5-6.0 by using 6mol/L hydrochloric acid aqueous solution, transferring into a 1000 ml volumetric flask, and diluting with water to the marked line. This solution was 0.2M sodium citrate-1M sodium nitrate.

1.4, step

1.4.1 Instrument calibration

According to the instruction of the instrument.

1.4.2, drawing a standard curve

(1) A series of 100ml volumetric flasks were filled with 20, 100, 500, 1000, 2000, 3000, 4000, 5000, 6000, 7000 micrograms of fluorine standard solution, and then with 20 ml of total ionic strength buffer solution, diluted with water to the marked line. The corresponding concentrations were 0.20, 1.00, 5.00, 10.0, 20.0, 30.0, 40.0, 50.0, 60.0, 70.0 mg/l fluorine, respectively. Shaken well and transferred to a 100ml beaker.

(2) And inserting the electrode into the solution, starting an electromagnetic stirrer, stirring for 1-3 minutes, and starting reading after the potential is stable. Before discharging the electrode again, stirring is not needed, so that the situation that air enters around the crystal to cause wrong reading or pointer shaking is avoided. Before each measurement, the electrodes were rinsed with water and blotted dry with filter paper.

(3) Drawing E-logC on semi-logarithmic coordinate paper_F ^-Curve line.

1.4.3 measurement of samples

Weighing W g of polyether sample (according to the content of fluorine), placing the W g of polyether sample into a 100ml volumetric flask, adding 20 ml of total ionic strength buffer solution, diluting the solution to a marked line by using water, uniformly mixing to obtain a sample test solution, placing 70 ml of the sample test solution into a 100ml beaker, measuring according to the procedure in the step (2) in 1.4.2 for drawing a standard curve, reading a millivolt value, and searching a fluorine ion concentration value C milligram/liter of fluorine from the standard curve.

W is related to the content of fluorine in the polyether sample, and a proper W value is selected according to the approximate fluorine content in the polyether sample, and the corresponding relation is as follows:

polyether sample fluorine content, ppmw	W, g
		Greater than 1000 and less than 5000	1.0～1.3
More than 500 and 1000 or less	3.0～3.5
		Greater than 100 and less than 500	7.0～7.5
Less than 100	8.0～8.5

1.5, calculating

The calculation formula is as follows:

the content of fluorine element in the polyether sample (ppmw) is 100C/W;

c is the value in mg/l of the fluorine concentration of the sample solution read on the standard curve;

w is the weight of the polyether sample in grams.

1.6 notes

(1) The standard curve is measured at the same temperature of the sample, so that the influence caused by temperature difference can be eliminated;

(2) preferably, a polyethylene beaker is used for measurement;

(3) care is taken to eliminate air bubbles at the electrode surface.

2. Determination of boron element by ICP-AES method

2.1 principle

When ICP-AES is used for quantitative analysis, under a certain condition, the spectral line intensity I and the content C of the element to be detected form a certain linear relation: according to the characteristic, at the corresponding wavelength of the element, standard solutions with different concentrations are prepared, the spectral intensity is measured, a standard curve is drawn, and the concentration of the element in the sample is measured by a standard curve method.

2.2 instruments and Experimental conditions

United states Varian inductively coupled plasma emission spectroscopy; VISTA-PRO (vertical rectangular tube);

ICP-AES working conditions: high frequency generator power 1100W; sample injection atomization argon pressure is 200 kPa; the plasma gas flow is 15.0L/min; the auxiliary gas flow is 1.5L/min; observation degree: 10 mm; analytical line wavelength 249.772 nm.

2.3, experimental reagent:

mother liquor of boron standard solution: 0.57g of boric acid is weighed, dissolved in water, transferred into a 1000 ml volumetric flask and diluted to the marked line. The boron concentration of the solution is 100 mg/L;

1% of hydrochloric acid aqueous solution.

2.4, step(s)

2.4.1 drawing of working curve

(1) A series of 100ml volumetric flasks were filled with standard solutions containing 20, 100, 500, 1000, 2000, 3000, 4000. mu.g of boron, respectively, and diluted with water to the mark. Obtaining standard series of boron with corresponding concentrations of 0.20, 1.00, 5.00, 10.0, 20.0, 30.0 and 40.0 mg/L respectively, measuring according to the instrument conditions of the step 2.2, and drawing a working curve by taking the concentration of the boron element as a horizontal coordinate and the spectral line intensity as a vertical coordinate.

2.4 sample determination

Weighing W g of polyether sample (according to the content of boron) in a 200ml polytetrafluoroethylene beaker, adding 50ml of 1% hydrochloric acid aqueous solution by weight, covering a watch glass, and heating and slightly boiling for 5min on an electric hot plate. Taking down and cooling. The solution was transferred to a 100ml plastic volumetric flask, and the volume was determined by using a 1% by weight aqueous hydrochloric acid solution, shaken up, and filtered to obtain a sample solution.

The sample solution was measured according to the above instrument conditions, and the concentration of boron element C mg/L was read on the curve.

W is related to the content of boron in the polyether sample, and a proper W value is selected according to the approximate fluorine content in the polyether sample, and the corresponding relation is as follows:

boron content, ppmw, of polyether samples	W, g
		Greater than 1000 and less than 5000	1.0～1.3
Greater than 500 and 1000 or soLower part	3.0～3.5
		Greater than 100 and less than 500	7.0～7.5
Less than 100	8.0～8.5

2.5, calculating

The calculation formula is as follows:

the content of boron element in the polyether sample (ppmw) is 100C/W;

c is the value of the boron concentration in mg/l of the sample solution read on the standard curve;

w is the weight of the polyether sample in grams.

3. Appearance and color

The appearance is visually observed (at 25 ℃); the color and luster are determined by GB/T9282-.

4. Hydroxyl number

The hydroxyl value of the secondary alcohol polyoxyethylene ether is measured by GB/T7383-2007 determination of hydroxyl value of nonionic surfactant, and the ethylene oxide addition number is calculated according to the hydroxyl value according to the following formula:

n＝[(56110/OHV)-Mw]/44.052

in the formula: n-ethylene oxide addition number

56110-1 mole of mgKOH number corresponding to hydroxyl, mgKOH;

hydroxyl value of OHV-secondary alcohol polyoxyethylene ether, mgKOH/g;

molecular weight of Mw-secondary alcohol;

44.052-molecular weight of ethylene oxide.

The inventor finds that the content of fluorine and boron in a secondary alcohol polyoxyethylene ether product can be greatly reduced after the method is used; and when the boron fluoride remover simultaneously comprises calcium hydroxide and magnesium carbonate or the boron fluoride remover simultaneously comprises calcium hydroxide and aluminum carbonate, the chroma of the secondary alcohol polyoxyethylene ether product is obviously reduced and the transparency of the secondary alcohol polyoxyethylene ether product is increased.

In the present invention, unless otherwise specified, the pressure is in terms of gauge pressure.

The present invention will be described in detail with reference to specific examples.

Detailed Description

[ example 1 ]

Preparation of mono-and secondary alcohol polyoxyethylene ether

(1) A1L stirred autoclave was charged with 1 mol of C13 secondary alcohol and 1.68g of boron trifluoride, the reactor was sealed and the stirring was started. Replacing air in the reaction kettle with nitrogen for three times, introducing ethylene oxide into the reaction kettle, controlling the reaction temperature to be 70 ℃ and the reaction pressure to be 0.2MPa until the total amount of the introduced ethylene oxide is 1.8 mol, and reducing the pressure of the reaction kettle to 50 ℃ to obtain a crude product 1 of 280 g of low-ethylene-oxide adduct secondary alcohol polyoxyethylene ether;

(2) adding 70g of water into the crude product 1 of the low-ethylene oxide adduct secondary alcohol polyoxyethylene ether with the weight of 280 g, stirring and heating to 60 ℃, standing and layering for 45 minutes at the temperature to obtain a crude product 2 of the low-ethylene oxide adduct secondary alcohol polyoxyethylene ether with the oil phase;

(3) distilling under reduced pressure at 160 ℃ and under the pressure of-0.092 MPa to remove unreacted secondary alcohol in the crude product 2 of the low ethylene oxide adduct secondary alcohol polyoxyethylene ether, thus obtaining 168 g of crude product 3 of the low ethylene oxide adduct secondary alcohol polyoxyethylene ether;

(4) adding 8g of pure water into the 168 g of crude low ethylene oxide adduct secondary alcohol polyoxyethylene ether product 3, and stirring for 30 minutes at the temperature of 90 ℃ to obtain a mixture A;

(5) then, maintaining the temperature constant, adding 5.50 g of a boron fluoride remover (consisting of calcium hydroxide) and stirring for 120 minutes to obtain a mixture B;

(6) vacuum dehydrating at 85 deg.C and-0.093 MPa for 120 min to obtain mixture C;

(7) cooling to 60 ℃, adding 1.0 g of activated clay, stirring for 45 minutes, and filtering to obtain refined low-ethylene oxide adduct secondary alcohol polyoxyethylene ether; the measured OHV is 168, and the ethylene oxide addition number is calculated to be 3 according to the measured OHV;

(8) 150 g (0.45 mol) of refined low ethylene oxide adduct secondary alcohol polyoxyethylene ether and 0.6 g of sodium hydroxide were added to the autoclave, the reactor was sealed, and stirring was started. Replacing air in the reaction kettle with nitrogen for three times, introducing ethylene oxide into the reaction kettle, controlling the reaction temperature to be 150 ℃ and the reaction pressure to be 0.2MPa until the total amount of the introduced ethylene oxide is 120 g, and indicating that the pressure of the reaction kettle is not reduced, namely finishing the curing reaction, thus obtaining the high ethylene oxide adducted secondary alcohol polyoxyethylene ether product: c13 Secondary alcohol polyoxyethylene (9) ether.

Secondly, refining the residual fluorine and boron content in the low-ethylene oxide addition secondary alcohol polyoxyethylene ether, and the appearance and the chroma of the high-ethylene oxide addition secondary alcohol polyoxyethylene ether

For comparison, the composition of the fluoroboron remover, the measured residual fluorine and boron contents in the refined low ethylene oxide adduct secondary alcohol polyoxyethylene ether, and the appearance and color of the high ethylene oxide adduct secondary alcohol polyoxyethylene ether are shown in Table 1. The measurement results are shown in table 1 for convenience of comparison.

[ example 2 ]

Preparation of mono-and secondary alcohol polyoxyethylene ether

(5) then, maintaining the temperature, adding 5.50 g of a boron fluoride remover (magnesium carbonate) and stirring for 120 minutes to obtain a mixture B;

[ example 3 ]

Preparation of mono-and secondary alcohol polyoxyethylene ether

(5) then, maintaining the temperature constant, adding 5.50 g of a boron fluoride remover (the composition is aluminum carbonate) and stirring for 120 minutes to obtain a mixture B;

[ example 4 ]

Preparation of mono-and secondary alcohol polyoxyethylene ether

(5) then, maintaining the temperature, adding 5.50 g of a boron fluoride remover (consisting of sodium hydroxide) and stirring for 120 minutes to obtain a mixture B;

[ example 5 ]

Preparation of mono-and secondary alcohol polyoxyethylene ether

(5) then, maintaining the temperature constant, adding 5.50 g of a boron fluoride remover (consisting of potassium hydroxide) and stirring for 120 minutes to obtain a mixture B;

[ COMPARATIVE EXAMPLE ]

Preparation of mono-and secondary alcohol polyoxyethylene ether

(5) then, maintaining the temperature unchanged, and stirring for 120 minutes without adding a boron fluoride remover to obtain a mixture B;

[ example 6 ]

Preparation of mono-and secondary alcohol polyoxyethylene ether

(5) then, maintaining the temperature, adding 5.50 g of a boron fluoride remover (a mixture of calcium hydroxide and magnesium hydroxide, wherein the weight ratio of the calcium hydroxide to the magnesium hydroxide is 5) and stirring for 120 minutes to obtain a mixture B;

[ example 7 ]

Preparation of mono-and secondary alcohol polyoxyethylene ether

(5) then, maintaining the temperature, adding 5.50 g of a boron fluoride remover (a mixture of calcium hydroxide and magnesium hydroxide, wherein the weight ratio of the calcium hydroxide to the magnesium hydroxide is 3) and stirring for 120 minutes to obtain a mixture B;

[ example 8 ]

Preparation of mono-and secondary alcohol polyoxyethylene ether

(5) then, maintaining the temperature constant, adding 5.50 g of a boron fluoride remover (which is a mixture of calcium hydroxide and aluminum carbonate, and the weight ratio of the calcium hydroxide to the aluminum carbonate is 10) and stirring for 120 minutes to obtain a mixture B;

[ example 9 ]

Preparation of mono-and secondary alcohol polyoxyethylene ether

(5) then, maintaining the temperature constant, adding 5.50 g of a boron fluoride remover (which is a mixture of calcium hydroxide and aluminum carbonate, and the weight ratio of the calcium hydroxide to the aluminum carbonate is 20) and stirring for 120 minutes to obtain a mixture B;

[ example 10 ]

Preparation of mono-and secondary alcohol polyoxyethylene ether

(5) then, maintaining the temperature, adding 5.50 g of a boron fluoride remover (a mixture of calcium hydroxide and sodium hydroxide, wherein the weight ratio of the calcium hydroxide to the sodium hydroxide is 20) and stirring for 120 minutes to obtain a mixture B;

[ example 11 ]

Preparation of mono-and secondary alcohol polyoxyethylene ether

(5) then, maintaining the temperature, adding 5.50 g of a boron fluoride remover (a mixture of calcium hydroxide and potassium hydroxide, wherein the weight ratio of the calcium hydroxide to the potassium hydroxide is 20) and stirring for 120 minutes to obtain a mixture B;

TABLE 1

Claims

1. The production method of the high-ethylene-oxide-adduct secondary alcohol polyoxyethylene ether comprises the following steps of reacting the low-ethylene-oxide-adduct secondary alcohol polyoxyethylene ether with ethylene oxide under the catalysis of alkali to obtain the high-ethylene-oxide-adduct secondary alcohol polyoxyethylene ether, wherein the low-ethylene-oxide-adduct secondary alcohol polyoxyethylene ether is prepared by adopting a preparation method comprising the following steps:

R-(O-CH₂CH₂)_n-OH；

the molar ratio of ethylene oxide to secondary alcohol in the step (1) is Q, and n/Q is 0.25-12;

the dosage of the boron fluoride remover in the step (5) is 0.5-10 times of that of the acid catalyst in the step (1) by weight.

2. The process according to claim 1, wherein the base is an alkali metal hydroxide and/or an alkali metal alkoxide of a C1-C2 alcohol.

3. The production method as claimed in claim 1, wherein the amount of the base used in the reaction under base catalysis is 0.05-1% of the weight of the high ethylene oxide adduct secondary alcohol polyoxyethylene ether.

4. The production process according to claim 1, wherein the reaction pressure in the reaction is 0.05 to 0.5MPa in the presence of a base catalyst.

5. The production process according to claim 1, wherein the reaction temperature in the reaction under base catalysis is 95 to 170 ℃.

6. The process according to claim 1, wherein said high oxyethylene adduct secondary alcohol polyoxyethylene ether has the following general formula:

R-(OCH₂CH₂)_mOH；

7. The production method according to claim 1, wherein the mass ratio of the crude product 1 of low ethylene oxide adduct secondary alcohol polyoxyethylene ether to water in the step (2) is 0.2 to 20.

8. The method according to claim 1, wherein the amount of water used in the step (4) is 0.5 to 10% by weight based on 3% by weight of the crude low ethylene oxide adduct secondary alcohol polyoxyethylene ether.

9. The method according to claim 1, wherein the mixing temperature in the step (4) is 25 to 100 ℃.