CN1502601A - Method for purifying hydroxyalkyl ester acrylate (methacrylate) - Google Patents
Method for purifying hydroxyalkyl ester acrylate (methacrylate) Download PDFInfo
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- CN1502601A CN1502601A CNA021453748A CN02145374A CN1502601A CN 1502601 A CN1502601 A CN 1502601A CN A021453748 A CNA021453748 A CN A021453748A CN 02145374 A CN02145374 A CN 02145374A CN 1502601 A CN1502601 A CN 1502601A
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Abstract
The present invention provides a purification process of (methyl) hydroxyalkyl acrylate. Said process adopts a thin-film evaporator and a falling film evaporator, and makes them be formed into the invented technological process for purification. Said process can obtain high-quality (methyl) hydroxyalkyl acrylate product with high purity, low water content and low chromaticity.
Description
Technical field
The present invention relates to the method that at least two thin-film evaporators of a kind of employing and at least one falling-film evaporator between thin-film evaporator are purified to (methyl) acrylic acid hydroxy alkyl ester.
Background technology
(methyl) acrylic acid hydroxy alkyl ester is a kind of unsaturated compound that has hydroxyl and two keys, and chemical property is very active, and the end-group polymer of self not only can take place, and can with other vinyl, the generation copolymerization of cyano group class monomer and polycondensation.
Usually, (methyl) acrylic acid hydroxy alkyl ester reacts in the presence of catalyzer by (methyl) vinylformic acid and oxyalkylene and obtains.But be reflected at when generating target product (methyl) acrylic acid hydroxy alkyl ester, also generated as aklylene glycol two (methyl) acrylate (abbreviation dibasic acid esters), the impurity of two alkylene glycol monos (methyl) acrylate and the acrylic acid dipolymer of oxyalkylene etc., so (methyl) acrylic acid hydroxy alkyl ester reaction solution that reaction obtains must be purified.
Up to the present, the method that the purifying technique of (methyl) acrylic acid hydroxy alkyl ester adopts usually is under reduced pressure, and the method for the thick liquid of distillation (methyl) acrylic acid hydroxy alkyl ester is separated and purifying.(US4365081)。Yet in this method, for example, when using a distillation column, be in for a long time under the relatively-high temperature owing to contain the reaction solution of (methyl) acrylic acid hydroxy alkyl ester of catalyzer, (methyl) acrylic acid hydroxy alkyl ester is easy to take place disproportionation reaction, thereby causes a large amount of generations of dibasic acid esters.The existence of dibasic acid esters, on the one hand, make purity drop as (methyl) acrylic acid hydroxy alkyl ester of principal product, on the other hand, the generation of a large amount of dibasic acid esters is easy to make (methyl) acrylic acid hydroxy alkyl ester generation polymerization, causes distillation long period to go on and to stop.In the present invention, we use thin-film evaporator to separate apace with the thick liquid of (methyl) acrylic acid hydroxy alkyl ester of catalyzer coexistence earlier, also with regard to existing problem in the purifying technique of having avoided US4365081.
Be in for a long time under the high temperature for fear of the thick liquid of (methyl) acrylic acid hydroxy alkyl ester that contains catalyzer, the method (German Patent NO152540) that can adopt thin-film evaporator is to (methyl) acrylic acid hydroxy alkyl ester purifying.This method is shorter owing to residence time of material, and service temperature is lower, so, in purification process, can suppress the generation of by product (dibasic acid esters) and the polymerization of material effectively.But, on the one hand because the film of its water surface of evaporation is rotation by the thin-film evaporator inner cylinder and scraper plate is formed and keep at the water surface of evaporation stirred solution, rotation and stirring are very easy to produce splash and entrainment, thereby pollute the distillatory product.On the other hand, because the separation efficiency of thin-film evaporator refined product is limited, so can't obtain high purity by a thin film evaporation, (methyl) acrylic acid hydroxy alkyl ester product of low impurity.
Yet no matter adopt distillation tower or thin-film evaporator, moisture and some other light constituent in the thick liquid of (methyl) acrylic acid hydroxy alkyl ester all can't remove from product, thereby cause the moisture content height in the finished product, have influence on the application of its back.As: cause the higher or postorder product problem such as prolongation inductive phase in polymerization process of water-content in the postorder product.
Summary of the invention
The purpose of this invention is to provide at least two thin-film evaporators of use and at least one method that falling-film evaporator is purified to (methyl) acrylic acid hydroxy alkyl ester between thin-film evaporator.
Second purpose of the present invention provides the device of purification (methyl) vinylformic acid hydroxyalkyl acrylate, and this device comprises at least two thin-film evaporators and at least one falling-film evaporator between thin-film evaporator.
The evaporation area of falling-film evaporator is 0.1-1 a times of the thin-film evaporator total evaporation area before it, is preferably 0.5 times.
Can connect between a plurality of thin-film evaporators, also can be connected in parallel.Equally, falling-film evaporator can connect or and connect, thin-film evaporator and falling-film evaporator can link together and carry out operate continuously.
The working pressure of thin-film evaporator is 200Pa～1500Pa, is preferably 200Pa～800Pa.The falling-film evaporator working pressure is 50Pa～1200Pa, is preferably 200Pa～600Pa, and the temperature of falling-film evaporator internal heating medium is 40 ℃～100 ℃, is preferably 60 ℃～75 ℃.
The whole process of production of (methyl) acrylic acid hydroxy alkyl ester comprises: react (methyl) acrylic acid hydroxy alkyl ester reaction mixture that obtains in the presence of catalyzer by (methyl) vinylformic acid and oxyalkylene, through removing excessive oxyalkylene, and the thick liquid of (methyl) acrylic acid hydroxy alkyl ester that obtains.Adopt the mode of a plurality of thin film evaporation units and a plurality of falling-film evaporators, the thick liquid of (methyl) acrylic acid hydroxy alkyl ester is purified.Specifically, the thick liquid of (methyl) acrylic acid hydroxy alkyl ester that will contain catalyzer is introduced a thin-film evaporator, product is separated apace with catalyzer, thereby shorten the material and the catalyzer residence time at high temperature, the generation and the polymeric that suppress by product (dibasic acid esters) effectively produce.The material that distillates that will remove catalyzer is then introduced the thin-film evaporator of back and is purified further, with solve the caused product colourity of entrainment that the front produces because of the defective of rapid evaporation and thin film evaporation itself bad with problems such as separating effect former thereby product quality that cause such as undesirable is not high.Or the overhead product that will remove catalyzer is introduced the falling film evaporation device, to remove moisture and some other light constituents in the product, the falling liquid film liquid that will remove moisture is again introduced the thin-film evaporator of postorder, to solve in the thin film evaporation process of front because of rapid evaporation and product contamination problem because of producing in the falling liquid film process, go forward side by side heavy constituent (dibasic acid esters and other impurity) in the one-step removal product so just can be guaranteed high purity, low moisture and the low dibasic acid esters of (methyl) acrylic acid hydroxy alkyl ester product.
The characteristics of purifying technique of the present invention are exactly in the process of (methyl) acrylic acid hydroxy alkyl ester of purifying, in order to obtain high-quality (methyl) acrylic acid hydroxy alkyl ester product, use the first film vaporizer and at least one falling-film evaporator of alternative and at least one thin-film evaporator, use two thin-film evaporators and falling-film evaporator to obtain (methyl) acrylic acid hydroxy alkyl ester product of high purity, low moisture, low dibasic acid esters content preferably.Preferably use according to use in order two thin-film evaporators and a falling-film evaporator of the first film vaporizer, falling-film evaporator and second thin-film evaporator (methyl) acrylic acid hydroxy alkyl ester is purified.
When enforcement is of the present invention, the thick liquid of employed (methyl) acrylic acid hydroxy alkyl ester, be in the presence of catalyzer, to carry out addition reaction,, and after remove excessive oxyalkylene and obtain when (methyl) acrylic acid transformation efficiency＞99.0% by (methyl) vinylformic acid and oxyalkylene.
Implement when of the present invention, the raw material that is preferred for preparation (methyl) acrylic acid hydroxy alkyl ester (i.e. the target product of Ti Chuning) is (methyl) vinylformic acid and oxyalkylene.Used (methyl) vinylformic acid of the present invention refers to vinylformic acid and methacrylic acid.Used oxyalkylene preferably has the oxyalkylene of 2-6 carbon atom, more preferably the oxyethane of 2 and 3 carbon atoms and propylene oxide.(methyl) vinylformic acid hydroxyalkyl acrylate of preparation better is that wherein alkyl is (methyl) vinylformic acid hydroxyalkyl acrylate that the alkyl of 2-6 carbon atom is arranged, and is more preferably (methyl) Hydroxyethyl acrylate or (methyl) Propylene glycol monoacrylate.
Implement when of the present invention, the catalyzer that is used for preparing (methyl) acrylic acid hydroxy alkyl ester can be selected iron cpd for use, as: iron trichloride, ironic acetate, the molysite of unsaturated acid; Chromium cpd, as: ammonium dichromate, chromic anhydride, chromium trichloride, and other organic acid chromic salts; Amine compound, as: quaternary ammonium salt, triethylamine etc.Other available auxiliary agent has: protonic acid, polyvalent alcohol, lipid acid, complexing agent etc.
For preventing the polymerization of (methyl) acrylic acid hydroxy alkyl ester, in reaction and purification process, add a certain amount of stopper.Available stopper has: phenolic compound is as quinhydrones, 2,6-di-tert-butyl hydroquinone, hydroquinone monomethyl ether, para benzoquinone etc.; To phenyl amines as N ' N '-dinaphthyl Ursol D, NN '-diphenyl-para-phenylene diamine, N-sec.-propyl-N '-diphenyl-para-phenylene diamine etc., the copper class is as cupric dimethyldithiocarbamate, copper dibutyldithiocarbamate, neutralized verdigris etc., the nitroxyl free radical class as: 2,2,6,6-tetramethyl--4-acetoxyl group piperidines-1-oxygen base, 2,2,6,6-tetramethyl piperidine-1-oxygen base, 4-hydroxyl-2,2,6,6-tetramethyl piperidine-1-oxygen base.Wherein, the stopper of preferentially selecting for use is: hydroquinone monomethyl ether, cupric dimethyldithiocarbamate and 2,2,6,6-tetramethyl--4-acetoxyl group piperidines.The consumption of stopper is generally 0.005%～0.5% of material gross weight, is preferably 0.05%～0.20%.
The thin film evaporation equipment of implementing to use among the present invention is a kind of vertical device, comprises having the distillation plant that vertical rotating shaft is housed in steam heating chuck simplified.This equipment uses paddle wheel or scraper plate to form film, and is evaporated.Splash and entrainment when preventing thin film evaporation are equipped with scum dredger (as silk screen) in device.In order to prevent the condensation of steam on scum dredger, it is overheated that scum dredger must keep simultaneously.The working pressure of thin-film evaporator should be below 800Pa, and we can carry out thin film evaporation by red-tape operati pressure under alap temperature.Can suppress the generation of polymeric generation and by product (dibasic acid esters) like this, purification operations can be carried out reposefully.
Condenser used in the present invention is a vertical stratification, can direct ester-introduced steam monomer, and also can allow the spray liquid of precooling be in contact with it.The condenser upper inside wall, the direct contact site of the steam of importing and spray liquid must be cooled to be lower than the boiling temperature of ester.Generally be lower than 10 ℃ of boiling points, at room temperature, be preferably lower than 20 ℃.The shell side of condenser leads to water coolant, and ester steam monomer and the spray liquid that imports in the tube side carried out condensation.And the tube side inner wall surface must be smooth.Like this, the monomer that has liquefied can flow away apace.
The part by weight of spray liquid and steam is to be advisable in 10: 1～100: 1.If measure too little, just can not with the ester vapor generation fully the surface contact.Thereby cause polymeric to produce.The temperature of spray liquid is lower than the boiling temperature of ester, and is suitable to being lower than 20 ℃ of boiling points.Contain a certain amount of stopper in the spray liquid, because spray liquid the finished product just, employed stopper preferably can be to the not influence of colourity of product.
Employed falling-film evaporator is made up of tube bank and shell among the present invention.(methyl) acrylic acid hydroxy alkyl ester distillate through thin film evaporation is directly added by the heating chamber top of falling-film evaporator after stopper is added in condensation, and inwall becomes membranaceous decline in the effect lower edge of gravity.In this decline process, moisture and part light constituent in (methyl) acrylic acid hydroxy alkyl ester are evaporated, and major product and heavy constituent still exist with liquid state, and thus, moisture is able to separate from product and removes with the part light constituent.Thereby reach the purpose that removes moisture and part light constituent.The falling liquid film sparger must be equipped with in the top of every heating tube in the falling-film evaporator, to guarantee that material becomes membranaceous and descends equably along inside pipe wall.In the present invention, under comparatively high temps, coexist for a long time for avoiding catalyzer and material, so the material that falling film evaporation is adopted is not the thick liquid of (methyl) acrylic acid hydroxy alkyl ester, but the distillate after thin film evaporation is handled.Working pressure 50Pa～the 1200Pa of falling-film evaporator is preferably 200Pa～800Pa.The temperature of heating medium that shell is walked is 40 ℃～100 ℃ a circulating hot water, is preferably 50 ℃～70 ℃, under this working pressure and temperature, guarantees that moisture and light constituent are evaporated and major product does not evaporate.
Falling liquid film liquid after falling liquid film is handled directly enters the thin-film evaporator of postorder.Mist eliminator is housed on the thin-film evaporator.In operating process, by the quantity of distillate of material and the ratio of inlet amount (following abbreviation distillates ratio) are controlled in the scope of 65%-90%, splash and entrainment phenomenon when stoping thin film evaporation effectively, go forward side by side heavy constituent in the one-step removal product, with the not enough problem of separation efficiency of solution front thin-film evaporator, thereby guarantee the high-quality of product.
Among the present invention, in product purifying technique process, enough falling film evaporation areas and a plurality of thin-film evaporator can carry out moisture effectively and separate, thereby can access low moisture, highly purified acrylic acid hydroxy alkyl ester product, so must be arranged with light constituent and heavy constituent ground.The preferential falling film evaporation area of selecting is 1/2 times of first thin film evaporation area.Selected thin film evaporation unit is 2, can meet the requirements of the product requirement of (methyl) acrylic acid hydroxy alkyl ester.
In the purifying technique process of (methyl) of the present invention acrylic acid hydroxy alkyl ester, owing to the catalyzer in the thick liquid of (methyl) acrylic acid hydroxy alkyl ester is separated apace with major product by first thin-film evaporator, shorten catalyzer and the material residence time under comparatively high temps, thereby suppressed the formation of by product such as dibasic acid esters and polymerisate; By using falling-film evaporator, removed moisture and the light constituent in the product, and use the thin-film evaporator of postorder to solve the entrainment problem that forms by first thin-film evaporator, thereby improved the purity of (methyl) acrylic acid hydroxy alkyl ester, made it possible to stably produce (methyl) acrylic acid hydroxy alkyl ester product of high purity, low moisture, low colourity.
This technology can reduce product effectively and generate dibasic acid esters and polymerization takes place in purification process, significantly reduce moisture and the colourity of improving product in the product, prolong the production cycle of device, improved throughput, obtained high purity, high-quality (methyl) acrylic acid hydroxy alkyl ester product.
The accompanying drawing summary
Fig. 1 is a process flow sheet of describing an embodiment of method of purification of the present invention.
Fig. 2 is a process flow sheet of describing an embodiment of existing (methyl) acrylic acid hydroxy alkyl ester method of purification.
Fig. 3 is a process flow sheet of describing another embodiment of existing (methyl) acrylic acid hydroxy alkyl ester method of purification.
The invention embodiment
An embodiment of a purification of the present invention (methyl) acrylic acid hydroxy alkyl ester as shown in Figure 1, the thick liquid of (methyl) acrylic acid hydroxy alkyl ester that will contain catalyzer is introduced the first film vaporizer 1 by feeding line 8, product is separated apace with catalyzer, and catalyst waste solution is discharged from waste liquid vent line 16.The material that distillates that will remove catalyzer is then introduced condenser 4, enter falling-film evaporator 2 through pipeline 9 again, to remove moisture and some other light constituents in the product, the falling liquid film liquid that will remove moisture is again introduced the thin-film evaporator 3 of postorder through discharging pipeline 10, overhead product to condenser 6 condensations, enters product holding tank 7 through pipeline 12.Among Fig. 1, mark 13 and 14 is represented the spray liquid pipeline, and mark 5 refers to condenser, and 11 refer to falling film evaporation top discharge pipeline, and 15 is the liquid effluent pipeline of second thin-film evaporator 3.
Fig. 2 is the process flow sheet of an embodiment of existing (methyl) acrylic acid hydroxy alkyl ester method of purification, a thin-film evaporator purification of this process using (methyl) vinylformic acid hydroxyalkyl acrylate.Reference numeral 17 wherein refers to thin-film evaporator, 18 fingering material pipelines, and 19 refer to the product holding tank, and 20 refer to condenser, and 21 refer to the spray liquid pipeline, and 22 refer to the waste liquid vent line.
Fig. 3 is the process flow sheet of another embodiment of (methyl) acrylic acid hydroxy alkyl ester method of purification, two placed in-line thin-film evaporators purification (methyl) vinylformic acid hydroxyalkyl acrylates of this process using.Reference numeral 26 wherein and 27 refers to thin-film evaporator, 31 fingering material pipelines, and 30 refer to the product holding tank, and 28 and 29 refer to condenser, and 34 and 35 refer to the spray liquid pipeline, and 36 refer to vent line, 32 and 33 is pipeline.
Listed some embodiments of the present invention below, its purpose just illustrates content of the present invention, and unrestricted its range of application.Adopt vapor-phase chromatography, adopt the karl Fischer method, adopt platinum cobalt colorimetry for the proximate analysis of product in the embodiments of the invention for the colorimetric analysis of product for the water analysis in the product.
According to method shown in Figure 1, by using two thin-film evaporators and a falling film evaporation device thick liquid of (methyl) acrylic acid hydroxy alkyl ester of purifying simultaneously.Employed thin film evaporation unit 1,3 all has scum dredger.The heat transfer surface area of thin film evaporation unit 1 is 6m
2, the heat transfer surface area of thin film evaporation unit 3 is 4m
2, the heat transfer surface area of falling film evaporation device 2 is 3m
2
In the presence of vinylformic acid iron, protonic acid, ammonium dichromate composite catalyst and ZJ-705 stopper (being nitroxyl free radical type stopper), vinylformic acid and propylene oxide react.After treating that acrylic acid transformation efficiency reaches 99.0%, after removing excessive propylene oxide, the thick liquid of Propylene glycol monoacrylate (comprising dibasic acid esters and other impurity) imports thin-film evaporator 1 with the inlet amount of 400Kg/Hr, its working pressure is about 500Pa, flow velocity with 360Kg/Hr obtains overhead product, and this overhead product is directly imported falling-film evaporator 2 after the hydroquinone monomethyl ether stopper is added in condensation.The working pressure of falling-film evaporator 2 is 500Pa, circulating hot water temperature in the shell side is under 60 ℃ the condition, wherein gaseous condensate obtains 10Kg/Hr, the falling liquid film liquid of resulting 350Kg/Hr is entered thin-film evaporator 3 after adding stopper ZJ-705, its working pressure is 500Pa, obtains distillate with the flow velocity of 320Kg/Hr, its part overhead product is after the stopper hydroquinone monomethyl ether is added in condensation, spray respectively to condenser 4,6 by pipeline 13,14.With the end discharging 30Kg/Hr warp 15 of thin-film evaporator 3, import thin-film evaporator 1 and carry out recycle, and the end discharging of thin-film evaporator 1 is discharged as waste liquid with 40Kg/Hr.
Colourity, moisture, Propylene glycol monoacrylate and other foreign matter content of thick liquid, the finished product and the waste liquid of aforesaid propylene acid hydroxypropyl acrylate are listed in the table 1.
Above technological process is moved three months continuously, and polymerism does not take place stable operation.
Table 1
| The colourity of Propylene glycol monoacrylate, moisture, purity situation | ||||||
| Colourity APHA | ??H 2O ??wt％ | ????AA ????Wt％ | ??HPA ??wt％ | Dibasic acid esters wt% | Other impurity wt% | |
| Infeed solution | ??/ | ??0.35 | ????0.25 | ??94.50 | ??2.90 | ??2.00 |
| The overhead product product | ??＜5 | ??0.10 | ????0.20 | ??98.50 | ??0.20 | ??1.00 |
| Raffinate | ??/ | ??0.05 | ????0.02 | ??68.36 | ??19.10 | ??12.47 |
By the purifying technique route of embodiment 1, obtain low colourity, low moisture and highly purified Propylene glycol monoacrylate product.
Annotate: HPA: Propylene glycol monoacrylate AA: vinylformic acid
Purify according to Propylene glycol monoacrylate being reacted thick liquid with embodiment 1 identical mode, wherein the operational condition of thin-film evaporator is identical with embodiment 1, and the operational condition of falling-film evaporator is: working pressure is about 200Pa, the temperature of recirculated water is about 60 ℃, with this understanding, the gaseous condensate of falling-film evaporator is 30Kg/Hr, and the quality product that obtains is listed in the table 2.
Table 2
| The colourity of Propylene glycol monoacrylate, moisture, purity situation | ||||||
| Colourity APHA | ??H 2O ??wt％ | ????AA ????Wt％ | ??HPA ??wt％ | Dibasic acid esters wt% | Other impurity wt% | |
| Infeed solution | ??/ | ??0.35 | ????0.25 | ??94.50 | ??2.90 | ??2.00 |
| The overhead product product | ??＜5 | ??0.05 | ????0.15 | ??98.50 | ??0.20 | ??1.10 |
| Raffinate | ??/ | ??0.04 | ????0.02 | ??68.36 | ??19.10 | ??12.48 |
Operation under these conditions, the product moisture content that obtains is low than embodiment 1, but the loss of product is big.
Purify according to Propylene glycol monoacrylate being reacted thick liquid with embodiment 1 identical mode, wherein the operational condition of thin-film evaporator is identical with embodiment 1, and the operational condition of falling-film evaporator is: working pressure is about 800Pa, the temperature of recirculated water is about 60 ℃, with this understanding, the gaseous condensate of falling-film evaporator is 5Kg/Hr, and the quality product that obtains is listed in the table 3.
Table 3
| The colourity of Propylene glycol monoacrylate, moisture, purity situation | ||||||
| Colourity APHA | ??H 2O ??wt％ | ????AA ????Wt％ | ??HPA ??wt％ | Dibasic acid esters wt% | Other impurity wt% | |
| Infeed solution | ??/ | ??0.35 | ????0.25 | ??94.50 | ??0.20 | ??4.70 |
| The overhead product product | ??＜5 | ??0.15 | ????0.20 | ??98.50 | ??0.20 | ??0.95 |
| Raffinate | ??/ | ??0.04 | ????0.02 | ??68.06 | ??19.45 | ??12.43 |
Operation under these conditions, the moisture content of product wants high than embodiment 1, but the loss of product is low.
Purify according to embodiment 1 identical mode Propylene glycol monoacrylate being reacted thick liquid, wherein the heat transfer surface area of thin film evaporation unit 1 is 6m
2, the heat transfer surface area of thin film evaporation unit 3 is 4m
2, the heat transfer surface area of falling film evaporation device 2 is 6m
2The operational condition of thin-film evaporator and falling-film evaporator is identical with embodiment 1.
With this understanding, the gaseous condensate of falling-film evaporator is 10Kg/Hr, and the quality product that obtains is listed in the table 4.
Table 4
| The colourity of Propylene glycol monoacrylate, moisture, purity situation | ||||||
| Colourity APHA | ??H 2O ??wt％ | ????AA ????Wt％ | ??HPA ??wt％ | Dibasic acid esters wt% | Other impurity wt% | |
| Infeed solution | ??/ | ??0.35 | ????0.25 | ??94.50 | ??2.90 | ??2.00 |
| The overhead product product | ??＜5 | ??0.10 | ????0.18 | ??98.50 | ??0.22 | ??1.00 |
| Raffinate | ??/ | ??0.04 | ????0.02 | ??66.45 | ??20.05 | ??13.44 |
Operation under these conditions, moisture and acrylic acid content are substantially the same manner as Example 1 in the product that obtains, and the area that the heat transfer area of falling-film evaporator is mated more than the first film vaporizer is described.
Purify according to embodiment 1 identical mode Propylene glycol monoacrylate being reacted thick liquid, wherein the heat transfer surface area of thin film evaporation unit 1 is 6m
2, the heat transfer surface area of thin film evaporation unit 3 is 4m
2, the heat transfer surface area of falling film evaporation device 2 is 1m
2The operational condition of thin-film evaporator and falling-film evaporator is identical with embodiment 1.With this understanding, the gaseous condensate of falling-film evaporator is 3Kg/Hr, and the quality product that obtains is listed in the table 5.
Table 5
| The colourity of Propylene glycol monoacrylate, moisture, purity situation | ||||||
| Colourity APHA | ??H 2O ??wt％ | ??AA ??Wt％ | ??HPA ??wt％ | Dibasic acid esters wt% | Other impurity wt% | |
| Infeed solution | ??/ | ??0.35 | ??0.25 | ??94.50 | ??2.90 | ??2.00 |
| The overhead product product | ??＜5 | ??0.20 | ??0.22 | ??98.40 | ??0.18 | ??1.00 |
| Raffinate | ??/ | ??0.04 | ??0.02 | ??66.45 | ??20.05 | ??13.44 |
Operation under these conditions, the moisture of product and acrylic acid content obviously want high than embodiment 1, but the loss of product is low.Illustrate that not matching of falling-film evaporator heat transfer area will make moisture and some other lights removal in the product incomplete.
Comparative example 1
By method shown in Figure 2, only use a thin-film evaporator (methyl) acrylic acid hydroxy alkyl ester of purifying.Used thin-film evaporator 17 is that heat transfer area is 6m
2The vertical thin-film vaporizer.
With the flow importing thin-film evaporator 17 of the thick liquid of the Propylene glycol monoacrylate among the embodiment 1 (comprising dibasic acid esters and other impurity) with 400Kg/Hr.Its working pressure is about 500Pa, obtains overhead product with the flow velocity of 360Kg/Hr, and the part overhead product sprays to condenser 20 through pipeline 21 after adding stopper.All the other are discharged through pipeline 22 as waste liquid 40Kg/Hr.
The above-mentioned colourity that infeeds solution, distillates product and waste liquid, moisture, Propylene glycol monoacrylate and other foreign matter content are listed in the table 6.
Above technological process was carried out three months continuously, did not produce polymerism, and this technological process can stably be carried out.But owing to only use a thin-film evaporator, the moisture in the overhead product, colourity are all higher than the Propylene glycol monoacrylate among the embodiment 1, and the purity of product is low.
Table 6
| The colourity of Propylene glycol monoacrylate, moisture, purity situation | ||||||
| Colourity APHA | ??H 2O ??wt％ | ????AA ????Wt％ | ????HPA ????wt％ | Dibasic acid esters wt% | Other impurity wt% | |
| Infeed solution | / | ??0.35 | ????0.25 | ????94.50 | ????2.90 | ??2.00 |
| The overhead product product | ＜25 | ??0.45 | ????0.35 | ????96.80 | ????0.90 | ??1.50 |
| Raffinate | / | ??0.12 | ????0.15 | ????75.84 | ????13.52 | ??10.37 |
Comparative example 2
By method shown in Figure 3, use the thin film evaporation unit of two serial connections Propylene glycol monoacrylate of purifying.The heat transfer area of used thin film evaporation unit 26 is 6m
2, the heat transfer area of thin film evaporation unit 27 is 4m
2
With the inlet amount importing thin-film evaporator 26 of the thick liquid of the Propylene glycol monoacrylate among the embodiment 1 (comprising dibasic acid esters and other impurity) with 400Kg/Hr, flow velocity with 360Kg/Hr obtains overhead product, and this overhead product is directly imported thin-film evaporator 27 after stopper is added in condensation.The working pressure of thin-film evaporator 27 is about 500Pa, obtains overhead product with the flow velocity of 320Kg/Hr, and its part overhead product adds stopper after pipeline 34,35 sprays to condenser 28,29 through condensation.The end discharging 40Kg/Hr of thin-film evaporator 27 is carried out recycle through pipeline 36 importing thin film evaporation units 26.The end discharging of thin-film evaporator 26 is discharged through pipeline 37 as waste liquid with 40Kg/Hr.
The above-mentioned colourity that infeeds solution, distillates product and waste liquid, moisture, Propylene glycol monoacrylate and other foreign matter content are listed in the table 7.Though adopt two thin-film evaporators that product is purified, the colourity that can improve the purity of product and improve product, moisture and residual acid content are all higher in the product.
Above technological process was carried out three months continuously, and polymerism does not take place, and said process can stably be operated.
Table 7
| The colourity of Propylene glycol monoacrylate, moisture, purity situation | ||||||
| Colourity APHA | ??H 20 ??wt％ | ????AA ????Wt％ | ????HPA ????wt％ | Dibasic acid esters wt% | Other impurity wt% | |
| Infeed solution | ??/ | ??0.35 | ????0.25 | ????94.50 | ??2.90 | ??2.00 |
| The overhead product product | ??＜5 | ??0.50 | ????0.20 | ????98.0 | ??0.20 | ??1.10 |
| Raffinate | ??/ | ??0.12 | ????0.15 | ????69.46 | ??19.64 | ??10.63 |
In the presence of the composite catalyst of vinylformic acid iron, protonic acid and ZJ-705 stopper, vinylformic acid and oxyethane react under 75 ℃.After treating that acrylic acid transformation efficiency reaches 99.0%, remove excessive oxyethane and obtain the thick liquid of Hydroxyethyl acrylate (comprising dibasic acid esters and other impurity), this thick liquid is purified by the purifying technique flow process of Fig. 1.Use two thin-film evaporators and a falling-film evaporator that the thick liquid of Hydroxyethyl acrylate is purified.Operational condition is identical with embodiment 1.
Thick liquid, the colourity that distillates product and waste liquid, moisture, Hydroxyethyl acrylate and other foreign matter content of aforesaid propylene acid hydroxyl ethyl ester are listed in the table 8.
Above technological process is moved one month continuously, polymerism does not take place, and said process can be operated stably.
Table 8
| The colourity of Hydroxyethyl acrylate, moisture, purity situation | ||||||
| Colourity APHA | ??H 2O ??wt％ | ????AA ????Wt％ | ??HEA ??wt％ | Dibasic acid esters wt% | Other impurity wt% | |
| Infeed solution | ??/ | ??0.35 | ????0.50 | ??90.50 | ??5.80 | ??2.85 |
| The overhead product product | ??＜10 | ??0.10 | ????0.20 | ??97.50 | ??0.50 | ??1.70 |
| Raffinate | ??/ | ??0.05 | ????0.02 | ??68.36 | ??18.50 | ??13.07 |
In embodiment 4, in conjunction with adopting two thin-film evaporators and a reduction film evaporator, Hydroxyethyl acrylate is purified, can obtain low colourity, low moisture and highly purified Hydroxyethyl acrylate product.
Annotate: the HEA Hydroxyethyl acrylate
Embodiment 7
In the presence of the composite catalyst of methacrylic acid iron, protonic acid and ZJ-705 stopper, methacrylic acid and oxyethane react under 75 ℃.After the transformation efficiency for the treatment of methacrylic acid reaches 99.0%, remove excessive oxyethane and obtain the thick liquid of hydroxyethyl methylacrylate (comprising dibasic acid esters and other impurity), use two thin-film evaporators and a falling-film evaporator that the thick liquid of hydroxyethyl methylacrylate is purified.Operational condition is identical with embodiment 1.
The thick liquid of above-mentioned hydroxyethyl methylacrylate, the colourity that distillates product and waste liquid, moisture, hydroxyethyl methylacrylate and other foreign matter content are listed in the table 9.
Above technological process is moved three months continuously, polymerism does not take place, and said process can be operated stably.
Table 9
| The colourity of hydroxyethyl methylacrylate, moisture, purity situation | ||||||
| Colourity APHA | ??H 2O ??wt％ | ????AA ????Wt％ | ??HMEA ??wt％ | Dibasic acid esters wt% | Other impurity wt% | |
| Infeed solution | ??/ | ??0.35 | ????0.50 | ??93.50 | ??4.50 | ??1.15 |
| The overhead product product | ??＜10 | ??0.10 | ????0.20 | ??98.50 | ??0.50 | ??0.70 |
| Raffinate | ??/ | ??0.05 | ????0.02 | ??68.16 | ??20.50 | ??11.27 |
Annotate: HMEA: hydroxyethyl methylacrylate
In the presence of the composite catalyst of methacrylic acid iron, protonic acid and ZJ-705 stopper, methacrylic acid and propylene oxide react under 75 ℃.After the transformation efficiency for the treatment of methacrylic acid reaches 99.0%, remove excessive propylene oxide and obtain the thick liquid of Rocryl 410 (comprising dibasic acid esters and other impurity), use two thin-film evaporators and a falling-film evaporator that the thick liquid of Rocryl 410 is purified.Operational condition is identical with embodiment 1.
The thick liquid of above-mentioned Rocryl 410, the colourity that distillates product and waste liquid, moisture, Rocryl 410 and other foreign matter content are listed in the table 10.
Above technological process is moved three months continuously, polymerism does not take place, and said process can be operated stably.
Table 10
| The colourity of Rocryl 410, moisture, purity situation | ||||||
| Colourity APHA | ??H 2O ??wt％ | ????AA ????Wt％ | ??HMPA ??wt％ | Dibasic acid esters wt% | Other impurity wt% | |
| Infeed solution | ??/ | ??0.35 | ????0.50 | ??94.80 | ??2.50 | ??1.85 |
| The overhead product product | ??＜10 | ??0.05 | ????0.20 | ??98.70 | ??0.20 | ??0.85 |
| Raffinate | ??/ | ??0.05 | ????0.02 | ??78.46 | ??10.50 | ??10.88 |
Annotate: HMPA: Rocryl 410
Comparative example 3
Use the thick liquid of Propylene glycol monoacrylate of embodiment 1, adopt the void column in the U.S. Pat 4365081 that it is purified.The quality product situation that obtains sees Table 11.
This purifying technique process is moved 20 days continuously, and polymerism just takes place.And product purity is lower by 1.40% than embodiment 1, and the moisture of product and acidity are all higher.
Table 11
| The colourity of Propylene glycol monoacrylate, moisture, purity situation | ||||||
| Colourity APHA | ??H 2O ??wt％ | ????AA ????Wt％ | ????HPA ????wt％ | Dibasic acid esters wt% | Other impurity wt% | |
| Infeed solution | ??/ | ??0.35 | ????0.20 | ????94.50 | ??2.90 | ??2.05 |
| The overhead product product | ??＜10 | ??0.45 | ????0.35 | ????97.10 | ??0.20 | ??1.90 |
| Raffinate | ??/ | ??0.05 | ????0.10 | ????76.26 | ??14.54 | ??9.05 |
Comparative example 4
Use the thick liquid of Hydroxyethyl acrylate of embodiment 2, adopt the void column in the U.S. Pat 4365081 that it is purified equally.The quality product situation that obtains sees Table 12.
This purifying technique process is moved 10 days continuously, and polymerism just takes place.And product purity is lower by 1.0% than embodiment 2, and the moisture of product and acidity are all higher.
Table 12
| The colourity of Hydroxyethyl acrylate, moisture, purity situation | ||||||
| Colourity APHA | ??H 2O ??wt％ | ????AA ????Wt％ | ??HEA ??wt％ | Dibasic acid esters wt% | Other impurity wt% | |
| Infeed solution | ??/ | ??0.35 | ????0.50 | ??90.50 | ??5.80 | ??2.85 |
| The overhead product product | ??＜10 | ??0.50 | ????0.65 | ??95.20 | ??2.50 | ??1.15 |
| Raffinate | ??/ | ??0.05 | ????0.02 | ??78.36 | ??10.58 | ??10.99 |
The present invention can comprise that other does not depart from the specific form of the present invention's spirit or its essential characteristic.Therefore, some embodiments at this only are used for explanation, be not construed as limiting the invention the scope of the invention of determining by the description of claims rather than front and all be included in claims in meaning of claims and all changes in the full scope of equivalents.
Claims (9)
1. the method for purification of (methyl) acrylic acid hydroxy alkyl ester, this method comprises: (1) makes the thick liquid of (methyl) acrylic acid hydroxy alkyl ester separate by at least one thin-film evaporator, (2) material that distillates of described thin-film evaporator is separated through at least one falling-film evaporator, (3) overhead product of described reduction film evaporator is separated again through at least one thin-film evaporator, (methyl) acrylic acid hydroxy alkyl ester that obtains purifying, the working pressure of described thin-film evaporator is respectively 200Pa～1500Pa, the working pressure of described falling-film evaporator is 50Pa～1200Pa, the temperature of falling film evaporation device internal heating medium is 40 ℃～100 ℃, the evaporation area of described falling-film evaporator be the thin-film evaporator before it the total evaporation area 0.1-1 doubly.
2. the method for purification of (methyl) as claimed in claim 1 acrylic acid hydroxy alkyl ester, the evaporation area that it is characterized in that described falling-film evaporator is 0.5 times of the total evaporation area of the thin-film evaporator before it.
3. the method for purification of (methyl) as claimed in claim 2 acrylic acid hydroxy alkyl ester, it is characterized in that described overhead product introducing falling-film evaporator with a thin-film evaporator, material that then will be after falling liquid film is handled, infeed another thin-film evaporator again, overhead product is (methyl) acrylic acid hydroxy alkyl ester product after purifying.
4. the method for purification of (methyl) as claimed in claim 1 acrylic acid hydroxy alkyl ester is characterized in that described thin-film evaporator is horizontal film evaporator or vertical film vaporizer.
5. the method for purification of (methyl) as claimed in claim 4 acrylic acid hydroxy alkyl ester is characterized in that described thin-film evaporator is the vertical film vaporizer.
6. as the method for purification of the arbitrary claim among the claim 1-5 described (methyl) acrylic acid hydroxy alkyl ester, the working pressure that it is characterized in that described thin-film evaporator is 200Pa～800Pa.
7. according to the method for purification of arbitrary claim among the claim 1-5 described (methyl) acrylic acid hydroxy alkyl ester, the working pressure that it is characterized in that described falling film evaporation device is 200Pa～600Pa, and the temperature of falling film evaporation device internal heating medium is 60 ℃～75 ℃.
8. the purifying plant of (methyl) acrylic acid hydroxy alkyl ester, this device comprises thin-film evaporator and at least one falling-film evaporator between thin-film evaporator at least, the evaporation area of described falling-film evaporator be the thin-film evaporator before it the total evaporation area 0.1-1 doubly.
9. the purifying plant of (methyl) as claimed in claim 8 acrylic acid hydroxy alkyl ester, the evaporation area that it is characterized in that described falling-film evaporator is 0.5 times of the total evaporation area of the thin-film evaporator before it.
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| CN 02145374 CN1220672C (en) | 2002-11-25 | 2002-11-25 | Method for purifying hydroxyalkyl ester acrylate (methacrylate) |
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| CN 02145374 CN1220672C (en) | 2002-11-25 | 2002-11-25 | Method for purifying hydroxyalkyl ester acrylate (methacrylate) |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102007056926A1 (en) | 2007-11-23 | 2009-05-28 | Evonik Röhm Gmbh | Process and installation for the purification of unsaturated compounds |
| CN101080259B (en) * | 2004-12-15 | 2012-03-28 | 旭化成化学株式会社 | Industrial evaporator |
| CN101080260B (en) * | 2004-12-20 | 2012-03-28 | 旭化成化学株式会社 | Industrial evaporator |
| CN104640835A (en) * | 2012-09-24 | 2015-05-20 | 株式会社日本触媒 | Hydroxyalkyl acrylate and method for producing same |
| CN110935188A (en) * | 2019-12-18 | 2020-03-31 | 万华化学集团股份有限公司 | Continuous rectification separation method and device for hydroxyethyl (meth) acrylate crude product |
| WO2023169863A1 (en) * | 2022-03-08 | 2023-09-14 | Röhm Gmbh | Process for preparing high purity (meth)acrylates |
-
2002
- 2002-11-25 CN CN 02145374 patent/CN1220672C/en not_active Expired - Lifetime
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101080259B (en) * | 2004-12-15 | 2012-03-28 | 旭化成化学株式会社 | Industrial evaporator |
| CN101080260B (en) * | 2004-12-20 | 2012-03-28 | 旭化成化学株式会社 | Industrial evaporator |
| DE102007056926A1 (en) | 2007-11-23 | 2009-05-28 | Evonik Röhm Gmbh | Process and installation for the purification of unsaturated compounds |
| RU2492162C2 (en) * | 2007-11-23 | 2013-09-10 | Эвоник Рем ГмбХ | Methods and apparatus for purifying unsaturated compounds |
| US9259664B2 (en) | 2007-11-23 | 2016-02-16 | Evonik Roehm Gmbh | Method and plant for purifying unsaturated compounds |
| CN104640835A (en) * | 2012-09-24 | 2015-05-20 | 株式会社日本触媒 | Hydroxyalkyl acrylate and method for producing same |
| CN104640835B (en) * | 2012-09-24 | 2016-07-06 | 株式会社日本触媒 | Acrylic acid hydroxy alkyl ester and preparation method thereof |
| US10023522B2 (en) | 2012-09-24 | 2018-07-17 | Nippon Shokubai Co., Ltd. | Hydroxyalkyl acrylate and method for producing same |
| CN110935188A (en) * | 2019-12-18 | 2020-03-31 | 万华化学集团股份有限公司 | Continuous rectification separation method and device for hydroxyethyl (meth) acrylate crude product |
| WO2023169863A1 (en) * | 2022-03-08 | 2023-09-14 | Röhm Gmbh | Process for preparing high purity (meth)acrylates |
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|---|---|
| CN1220672C (en) | 2005-09-28 |
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