CN119463088A - A kind of synthesis process of waterborne polyurethane - Google Patents
A kind of synthesis process of waterborne polyurethane Download PDFInfo
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- CN119463088A CN119463088A CN202411684496.9A CN202411684496A CN119463088A CN 119463088 A CN119463088 A CN 119463088A CN 202411684496 A CN202411684496 A CN 202411684496A CN 119463088 A CN119463088 A CN 119463088A
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- waterborne polyurethane
- chain extender
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- polyol
- diisocyanate
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- 238000000034 method Methods 0.000 title claims abstract description 40
- 239000004814 polyurethane Substances 0.000 title claims abstract description 36
- 229920002635 polyurethane Polymers 0.000 title claims abstract description 36
- 230000008569 process Effects 0.000 title claims abstract description 31
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 17
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 17
- 238000006243 chemical reaction Methods 0.000 claims abstract description 54
- 239000004970 Chain extender Substances 0.000 claims abstract description 39
- 239000000839 emulsion Substances 0.000 claims abstract description 25
- 150000003077 polyols Chemical class 0.000 claims abstract description 20
- 229920005862 polyol Polymers 0.000 claims abstract description 18
- 239000012948 isocyanate Substances 0.000 claims abstract description 14
- 150000002513 isocyanates Chemical class 0.000 claims abstract description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 33
- 238000001816 cooling Methods 0.000 claims description 32
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 20
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 claims description 18
- 239000007788 liquid Substances 0.000 claims description 13
- 229910052757 nitrogen Inorganic materials 0.000 claims description 10
- RRAMGCGOFNQTLD-UHFFFAOYSA-N hexamethylene diisocyanate Chemical compound O=C=NCCCCCCN=C=O RRAMGCGOFNQTLD-UHFFFAOYSA-N 0.000 claims description 7
- 230000002194 synthesizing effect Effects 0.000 claims description 7
- 239000005057 Hexamethylene diisocyanate Substances 0.000 claims description 6
- 239000006185 dispersion Substances 0.000 claims description 4
- 229920005906 polyester polyol Polymers 0.000 claims description 4
- UPMLOUAZCHDJJD-UHFFFAOYSA-N 4,4'-Diphenylmethane Diisocyanate Chemical compound C1=CC(N=C=O)=CC=C1CC1=CC=C(N=C=O)C=C1 UPMLOUAZCHDJJD-UHFFFAOYSA-N 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- DVKJHBMWWAPEIU-UHFFFAOYSA-N toluene 2,4-diisocyanate Chemical compound CC1=CC=C(N=C=O)C=C1N=C=O DVKJHBMWWAPEIU-UHFFFAOYSA-N 0.000 claims description 3
- CDMDQYCEEKCBGR-UHFFFAOYSA-N 1,4-diisocyanatocyclohexane Chemical compound O=C=NC1CCC(N=C=O)CC1 CDMDQYCEEKCBGR-UHFFFAOYSA-N 0.000 claims description 2
- 239000004721 Polyphenylene oxide Substances 0.000 claims description 2
- 150000001412 amines Chemical group 0.000 claims description 2
- XXKOQQBKBHUATC-UHFFFAOYSA-N cyclohexylmethylcyclohexane Chemical compound C1CCCCC1CC1CCCCC1 XXKOQQBKBHUATC-UHFFFAOYSA-N 0.000 claims description 2
- NIMLQBUJDJZYEJ-UHFFFAOYSA-N isophorone diisocyanate Chemical compound CC1(C)CC(N=C=O)CC(C)(CN=C=O)C1 NIMLQBUJDJZYEJ-UHFFFAOYSA-N 0.000 claims description 2
- PSGAAPLEWMOORI-PEINSRQWSA-N medroxyprogesterone acetate Chemical compound C([C@@]12C)CC(=O)C=C1[C@@H](C)C[C@@H]1[C@@H]2CC[C@]2(C)[C@@](OC(C)=O)(C(C)=O)CC[C@H]21 PSGAAPLEWMOORI-PEINSRQWSA-N 0.000 claims description 2
- 229920000515 polycarbonate Polymers 0.000 claims description 2
- 239000004417 polycarbonate Substances 0.000 claims description 2
- 229920000570 polyether Polymers 0.000 claims description 2
- 238000012797 qualification Methods 0.000 claims description 2
- 239000007787 solid Substances 0.000 claims description 2
- 239000005058 Isophorone diisocyanate Substances 0.000 claims 1
- 239000002826 coolant Substances 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 abstract description 5
- 238000002156 mixing Methods 0.000 abstract description 2
- 239000002861 polymer material Substances 0.000 abstract description 2
- 230000000052 comparative effect Effects 0.000 description 7
- 238000007086 side reaction Methods 0.000 description 4
- 230000017525 heat dissipation Effects 0.000 description 3
- 238000009776 industrial production Methods 0.000 description 3
- 238000006116 polymerization reaction Methods 0.000 description 3
- 206010024769 Local reaction Diseases 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000009472 formulation Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 230000002035 prolonged effect Effects 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- PIICEJLVQHRZGT-UHFFFAOYSA-N Ethylenediamine Chemical compound NCCN PIICEJLVQHRZGT-UHFFFAOYSA-N 0.000 description 1
- 230000002159 abnormal effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000032798 delamination Effects 0.000 description 1
- 230000003111 delayed effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000001788 irregular Effects 0.000 description 1
- 238000013021 overheating Methods 0.000 description 1
- 238000011056 performance test Methods 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
- B01J19/0013—Controlling the temperature of the process
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G18/00—Polymeric products of isocyanates or isothiocyanates
- C08G18/06—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen
- C08G18/08—Processes
- C08G18/10—Prepolymer processes involving reaction of isocyanates or isothiocyanates with compounds having active hydrogen in a first reaction step
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G18/00—Polymeric products of isocyanates or isothiocyanates
- C08G18/06—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen
- C08G18/28—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen characterised by the compounds used containing active hydrogen
- C08G18/30—Low-molecular-weight compounds
- C08G18/32—Polyhydroxy compounds; Polyamines; Hydroxyamines
- C08G18/3203—Polyhydroxy compounds
- C08G18/3206—Polyhydroxy compounds aliphatic
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G18/00—Polymeric products of isocyanates or isothiocyanates
- C08G18/06—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen
- C08G18/28—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen characterised by the compounds used containing active hydrogen
- C08G18/30—Low-molecular-weight compounds
- C08G18/32—Polyhydroxy compounds; Polyamines; Hydroxyamines
- C08G18/3225—Polyamines
- C08G18/3228—Polyamines acyclic
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G18/00—Polymeric products of isocyanates or isothiocyanates
- C08G18/06—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen
- C08G18/28—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen characterised by the compounds used containing active hydrogen
- C08G18/65—Low-molecular-weight compounds having active hydrogen with high-molecular-weight compounds having active hydrogen
- C08G18/66—Compounds of groups C08G18/42, C08G18/48, or C08G18/52
- C08G18/6633—Compounds of group C08G18/42
- C08G18/6637—Compounds of group C08G18/42 with compounds of group C08G18/32 or polyamines of C08G18/38
- C08G18/6648—Compounds of group C08G18/42 with compounds of group C08G18/32 or polyamines of C08G18/38 with compounds of group C08G18/3225 or C08G18/3271 and/or polyamines of C08G18/38
- C08G18/6651—Compounds of group C08G18/42 with compounds of group C08G18/32 or polyamines of C08G18/38 with compounds of group C08G18/3225 or C08G18/3271 and/or polyamines of C08G18/38 with compounds of group C08G18/3225 or polyamines of C08G18/38
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Polyurethanes Or Polyureas (AREA)
Abstract
本发明属于高分子材料领域，提供了一种水性聚氨酯的合成工艺，包括：将异氰酸酯和多元醇混合，在80‑90℃下反应2‑5h；在70‑90℃下，采用连续补加的方式向反应体系中加入扩链剂，在1‑3h内完成投料，投料完成后继续反应1‑3h，即得。本发明的聚氨酯乳液合成工艺可以生产出更为均一、稳定的水性聚氨酯产品，明显提升了生产效率和批次间乳液性能的稳定性。The invention belongs to the field of polymer materials, and provides a synthesis process of waterborne polyurethane, comprising: mixing isocyanate and polyol, reacting at 80-90°C for 2-5h; adding a chain extender to the reaction system at 70-90°C in a continuous addition manner, completing the feeding within 1-3h, and continuing the reaction for 1-3h after the feeding is completed, to obtain the product. The polyurethane emulsion synthesis process of the invention can produce a more uniform and stable waterborne polyurethane product, and significantly improves the production efficiency and the stability of the emulsion performance between batches.
Description
Technical Field
The invention belongs to the field of high polymer materials, and particularly relates to a synthesis process of waterborne polyurethane.
Background
The disclosure of this background section is only intended to increase the understanding of the general background of the invention and is not necessarily to be construed as an admission or any form of suggestion that this information forms the prior art already known to those of ordinary skill in the art.
The synthesis of the aqueous polyurethane adopts kettle reaction, firstly, raw materials (isocyanate, chain extender, polyol and the like) are added into a reaction kettle to perform prepolymerization reaction, then acetone is added to perform viscosity adjustment and pre-chain extension treatment, finally water is added to perform phase inversion, so that the emulsion is converted from a W/O (water in oil) state to an O/W (oil in water) state, and acetone is removed, thus obtaining the polyurethane emulsion. In the emulsion synthesis process, the pre-polymerization reaction is critical, the currently common process is that three-component raw materials are subjected to one-time feeding reaction or polyol and isocyanate are subjected to preferential reaction, and then chain extender is added for reaction, and the two reaction modes have the advantages of ensuring the reaction efficiency, but have the disadvantages that the pre-polymerization reaction cannot be stably controlled, the obvious difference of polyurethane molecular chain structures can be caused by slight change of process operation, the obvious performance difference of the emulsion synthesized by the same formula can be caused by light weight, the emulsion performance is insufficient in controllability, demulsification, sedimentation and delamination are caused by heavy weight, even a condensation kettle are caused, and the yield and the production progress are seriously influenced.
The paper "influence of chain extension on the structure and performance of waterborne polyurethane" discloses the preparation of waterborne polyurethane by adopting a step-by-step chain extension method. But belongs to laboratory pilot experiments, and cannot meet the tonnage level industrial production requirements. Meanwhile, in industrial production, the method has high probability of risk of a condensation kettle when acetone is added for viscosity adjustment.
On the other hand, the purpose of the traditional step-by-step feeding method is to prevent the reaction failure or side reaction caused by rapid reaction and severe heat release, but the risk of overheating and excessive viscosity of the reaction still exists in the step-by-step feeding in the industrial production process of the aqueous polyurethane.
Disclosure of Invention
In order to solve the problems, the invention provides a synthesis process of waterborne polyurethane. The continuous adding mode is used, the reaction heat release is slower by prolonging the adding time of the chain extender, the temperature in the reaction kettle is controlled by matching with the cooling mode, the smooth proceeding of the main reaction is ensured, and the yield, the production efficiency and the stability of the emulsion performance among batches are improved.
In order to achieve the above purpose, the present invention adopts the following technical scheme:
in a first aspect of the invention, a synthesis process of aqueous polyurethane is provided, comprising:
mixing isocyanate and polyol, and reacting for 2-5h at 80-90 ℃;
adding a chain extender into the reaction system in a continuous adding mode at 70-90 ℃, completing feeding within 1-3h, and continuing to react for 1-3h after feeding is completed;
Adding acetone for viscosity adjustment, adding a pre-chain extender for chain extension reaction, adding water for dispersion, removing acetone, and adjusting to proper emulsion solid content and viscosity.
At present, the emulsion stability of the domestic aqueous polyurethane emulsion is biased, and the invention adjusts the synthesis process with low cost, thereby improving the reaction success rate of the aqueous polyurethane emulsion.
Unlike the traditional chain extender replenishing process in 5min, the present invention has continuous chain extender replenishing process with prolonged chain extender replenishing time (completed in 1-3 hr), controlled heat release, normal main reaction, raised emulsion performance stability and film forming strength.
In some embodiments, the isocyanate is selected from at least one of Hexamethylene Diisocyanate (HDI), toluene Diisocyanate (TDI), diphenylmethane diisocyanate (MDI), isophorone diisocyanate (IPDI), dicyclohexylmethane 4, 4-diisocyanate (HMDI), 1, 4-cyclohexane diisocyanate (CHDI).
In some embodiments, the polyol is a polyether polyol, a polyester polyol, or a polycarbonate polyol.
In some embodiments, the chain extender is a polyol chain extender.
Preferably, the chain extender is at least one of BDO, EDO, PDO, CDO, DMPA.
In some embodiments, the front chain extender is an amine chain extender.
The present invention is not limited to the specific amounts of isocyanate, polyol and chain extender, and may be applied to any formulation capable of synthesizing an aqueous polyurethane emulsion.
In some embodiments, the temperature is controlled by a combination of at least two of water cooling, liquid nitrogen cooling and chilled water cooling.
In some embodiments, a double coil or a triple coil is used for temperature control, and different cooling liquids are independently circulated to form a closed loop;
in some embodiments, the double coil adopts two coil modes of common water cooling and chilled water cooling, common water cooling and liquid nitrogen cooling;
in some embodiments, the three coils are in the form of normal water cooling, chilled water, liquid nitrogen three coils.
In a second aspect of the invention, there is provided an aqueous polyurethane prepared by the above method.
In a third aspect, the invention provides the use of a continuous addition of a chain extender to improve the yield and performance stability of an aqueous polyurethane product.
The beneficial effects of the invention are that
(1) The synthesis process of the invention realizes more effective control of polyurethane molecular chains, improves the yield in the synthesis process of the aqueous polyurethane, and improves the quality of the aqueous polyurethane synthesis under the condition of low cost input.
(2) The preparation method is simple, has strong practicability and is easy to popularize.
Detailed Description
It should be noted that the following detailed description is exemplary and is intended to provide further explanation of the invention. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
As described in the background art, isocyanate, polyol and chain extender are put into a reaction kettle for prepolymerization reaction at one time, so that local severe reaction is easy to cause, the more severe the local reaction is, the more the reaction releases heat, the obvious difference of the distribution of reactive molecular chains is caused by the temperature difference of different areas in the kettle, and the problems of unstable performance among emulsion batches, gel even the like are caused;
Isocyanate and polyol are put into a reaction kettle to be subjected to pre-polymerization reaction preferentially, and irregular distribution of molecular chains is restrained to a certain extent, but after a chain extender is put into the reaction kettle, free isocyanate and the chain extender react extremely rapidly, if rapid dispersion of the chain extender cannot be realized, the problem of severe local reaction is easily caused, and the occurrence of side reaction is aggravated by rising reaction heat.
In order to solve the problems, the invention provides a synthesis process of aqueous polyurethane, comprising the following steps:
(1) The isocyanate and the polyol are preferentially reacted for a period of time (2-5 h), and the temperature in the kettle is controlled at 80-90 ℃;
(2) Adding chain extender in the kettle, controlling the adding flow according to the specific adding amount by adopting a continuous adding mode, completing feeding within 1-3h, continuing to react for 1-3h after finishing feeding, and controlling the temperature in the kettle at 70-90 ℃;
(3) The cooling mode of the reaction kettle adopts a mode of combining water cooling and liquid nitrogen cooling (and/or frozen water cooling) to control the temperature, and double-coil pipes or three-coil pipes are used for controlling the temperature (the double-coil pipes are a common water cooling and frozen water cooling mode, a common water cooling and liquid nitrogen cooling mode, different cooling liquids are independently circulated to form a closed loop, and the three-coil pipes are a common water cooling mode, a frozen water mode and a liquid nitrogen mode, and different cooling liquids are independently circulated to form a closed loop.)
The principle is described as follows:
The process (1) aims to ensure that the polyol is preferentially reacted with isocyanate, the reaction is complete, the temperature is too low, the reaction degree can be influenced, or the reaction time can be delayed, the production efficiency is influenced, the side reaction is easy to occur due to the too high temperature, and the reaction cannot be reimbursed, so that the reaction of the process (1) needs to strictly control the reaction temperature, the conventional water heating or heat dissipation mode can realize heating and heat preservation, but the heat dissipation and the temperature reduction are slower, and the abnormal problem of local overheat reaction is easy to occur;
The process (2) is the key point of the invention, namely, the feeding amount and the feeding period of the chain extender are controlled in a flow metering and time setting mode, so that the overreaction problem (local overheat and side reaction) caused by one-time feeding is avoided, the feeding period of the chain extender is prolonged, the heat dissipation efficiency in a kettle is improved, the local overheat problem is avoided, and the smooth proceeding of the main reaction is ensured to the greatest extent;
The process (3) is to optimize and reform the reaction kettle equipment, and the heat exchange and cooling efficiency of the reaction kettle is improved by introducing frozen water and/or liquid nitrogen, so that the temperature in the reaction kettle is effectively controlled.
The invention prolongs the synthesis time of the emulsion to a certain extent, but greatly improves the qualification rate and the performance stability of the finished product of the emulsion.
The invention will now be described in further detail with reference to the following specific examples, which should be construed as illustrative rather than limiting.
In the examples below, the amounts of HDI, polyester polyol, chain extender, acetone, pre-chain extender were determined according to the formulation of commercial aqueous polyurethane.
Example 1
(1) The cooling mode of the reaction kettle adopts a mode of combining water cooling and frozen water cooling to control the temperature, double-coil pipe temperature control is carried out, the HDI and the polyester polyol with the molecular weight of 2000 are fed according to the formula proportioning requirement and react for 2 hours preferentially, the temperature in the kettle is controlled at 85 ℃, and in the production process, the temperature of the reaction kettle is 85+/-2 ℃, and the temperature stability is good;
(2) Adding chain extender (BDO) in the kettle in a continuous adding mode, controlling the adding flow according to the specific adding amount, completing feeding within 1h, continuing to react for 2h after the feeding is completed, controlling the temperature in the kettle at 80 ℃ and controlling the actual temperature at about 80+/-2 ℃;
(3) After the reaction is finished, adding acetone for viscosity reduction, adding a front chain extender (ethylenediamine) for chain extension reaction, adding water for dispersion, and desolventizing to obtain a finished emulsion;
(4) 2 batches of product (4 tons per batch, the same applies below) were continuously produced according to the above process, each batch being sampled for performance.
Example 2
The reaction kettle is cooled by normal water cooling and temperature control, the temperature is raised to 95 ℃ at most in the reaction process of HDI and polyol according to the method of the embodiment 1, the cooling is slow, the same formula is added with an equal amount of chain extender, the feeding is completed within 1h by adopting a continuous addition method, the reaction is continued for 2h after the feeding is completed, the temperature in the kettle is controlled at 80 ℃ and the actual temperature is up to 100 ℃, other processes are the same as the embodiment 1,2 batches of products are normally produced, and each batch is sampled and tested for performance.
Comparative example 1
In the cooling method of reference example 1, however, in the step (1), isocyanate, a chain extender and polyol are added into a reaction kettle at one time, the reaction temperature is controlled to be 80 ℃, the actual maximum temperature is 100 ℃, the reaction heat release is more, obvious residues exist in the finished emulsion, and the emulsion stability is poor.
Comparative example 2
Referring to the process of example 1, but in step (2), the chain extender is fed into the reaction kettle in a one-time feeding manner (the chain extender is fed in 5 minutes), the reaction temperature is controlled to 80 ℃, the actual maximum temperature is 90 ℃, the finished emulsion has residues, 2 batches of products are produced, and each batch is sampled for testing performance.
Comparative example 3
Referring to the procedure of example 1, but in step (2), the chain extender was added to the reaction vessel in 3 portions, each of which was completed within 1/3 of 5min, each at 20min intervals. The reaction temperature is controlled to be 80 ℃, the actual highest temperature is 86 ℃,2 batches of products are produced, the finished emulsion has slight residues, the filling is slightly better than that of comparative example 2, and each batch is sampled to test the performance.
TABLE 1 results of Water-based polyurethane Performance test
As shown in table 1, example 1 had the best performance, the best batch-to-batch stability, the most stable temperature control according to the process record, and the other examples and comparative examples all had the deviation in effect, especially comparative example 1, with poor emulsion stability, significant sedimentation, and the emulsion could not be used.
As is clear from a comparison of example 1 and comparative example 3, the continuous addition of the present invention can better improve the performance stability and film forming strength of the aqueous polyurethane than the "step-feed method".
The above description is only of the preferred embodiments of the present invention and is not intended to limit the present invention, but various modifications and variations can be made to the present invention by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
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| CN202411684496.9A CN119463088A (en) | 2024-11-22 | 2024-11-22 | A kind of synthesis process of waterborne polyurethane |
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