CN115181259B - Method for continuously preparing polyether - Google Patents
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- CN115181259B CN115181259B CN202210966793.7A CN202210966793A CN115181259B CN 115181259 B CN115181259 B CN 115181259B CN 202210966793 A CN202210966793 A CN 202210966793A CN 115181259 B CN115181259 B CN 115181259B
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- 229920000570 polyether Polymers 0.000 title claims abstract description 78
- 239000004721 Polyphenylene oxide Substances 0.000 title claims abstract description 75
- 238000000034 method Methods 0.000 title claims abstract description 34
- 239000003054 catalyst Substances 0.000 claims abstract description 75
- 238000006243 chemical reaction Methods 0.000 claims abstract description 73
- 229920005862 polyol Polymers 0.000 claims abstract description 41
- 150000003077 polyols Chemical class 0.000 claims abstract description 40
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 37
- 230000008569 process Effects 0.000 claims abstract description 25
- 239000000047 product Substances 0.000 claims abstract description 20
- 230000032683 aging Effects 0.000 claims abstract description 19
- 239000003999 initiator Substances 0.000 claims abstract description 16
- 230000006698 induction Effects 0.000 claims abstract description 13
- 239000000203 mixture Substances 0.000 claims abstract description 12
- 239000007858 starting material Substances 0.000 claims abstract description 8
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 5
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 3
- 238000010438 heat treatment Methods 0.000 claims abstract description 3
- 125000002887 hydroxy group Chemical group [H]O* 0.000 claims description 31
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims description 20
- DNIAPMSPPWPWGF-UHFFFAOYSA-N Propylene glycol Chemical compound CC(O)CO DNIAPMSPPWPWGF-UHFFFAOYSA-N 0.000 claims description 15
- GOOHAUXETOMSMM-UHFFFAOYSA-N Propylene oxide Chemical compound CC1CO1 GOOHAUXETOMSMM-UHFFFAOYSA-N 0.000 claims description 15
- MTHSVFCYNBDYFN-UHFFFAOYSA-N diethylene glycol Chemical compound OCCOCCO MTHSVFCYNBDYFN-UHFFFAOYSA-N 0.000 claims description 15
- 238000009826 distribution Methods 0.000 claims description 13
- 150000002924 oxiranes Chemical class 0.000 claims description 12
- IAYPIBMASNFSPL-UHFFFAOYSA-N Ethylene oxide Chemical group C1CO1 IAYPIBMASNFSPL-UHFFFAOYSA-N 0.000 claims description 9
- 238000002360 preparation method Methods 0.000 claims description 9
- SZXQTJUDPRGNJN-UHFFFAOYSA-N dipropylene glycol Chemical compound OCCCOCCCO SZXQTJUDPRGNJN-UHFFFAOYSA-N 0.000 claims description 3
- 230000000630 rising effect Effects 0.000 claims description 2
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 abstract description 10
- 239000002994 raw material Substances 0.000 abstract description 7
- 150000002118 epoxides Chemical class 0.000 abstract 2
- 239000002002 slurry Substances 0.000 description 27
- 239000006185 dispersion Substances 0.000 description 10
- 230000000052 comparative effect Effects 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 230000002431 foraging effect Effects 0.000 description 5
- 238000006116 polymerization reaction Methods 0.000 description 5
- 229920002635 polyurethane Polymers 0.000 description 5
- 238000003860 storage Methods 0.000 description 5
- 239000000463 material Substances 0.000 description 4
- 238000010998 test method Methods 0.000 description 3
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 description 2
- 238000005227 gel permeation chromatography Methods 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 229920005830 Polyurethane Foam Polymers 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000004806 packaging method and process Methods 0.000 description 1
- 239000011496 polyurethane foam Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
Classifications
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- 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
- C08G65/00—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule
- C08G65/02—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring
- C08G65/26—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds
- C08G65/2603—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds the other compounds containing oxygen
- C08G65/2606—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds the other compounds containing oxygen containing hydroxyl groups
- C08G65/2609—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds the other compounds containing oxygen containing hydroxyl groups containing aliphatic hydroxyl groups
-
- 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
- C08G65/00—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule
- C08G65/02—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring
- C08G65/26—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds
- C08G65/2603—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds the other compounds containing oxygen
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- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
- Polyethers (AREA)
Abstract
The invention provides a method for continuously preparing polyether, which comprises the following steps: 1) Adding polyether polyol and DMC catalyst into a reaction kettle in advance, heating, and introducing epoxide for induction reaction; 2) After the induction reaction of the catalyst is successful, continuously introducing epoxide, DMC catalyst and starter into a reaction kettle for reaction, and allowing a reaction product to flow out from the top of the kettle and enter an aging kettle to obtain polyether after the aging is completed; wherein the initiator is water or a mixture of water and dihydric alcohol, and the addition amount of the initiator is controlled so that the average water content in the reaction system is not less than 0.01wt% and not more than 1.15wt%. The invention can greatly reduce the raw material cost in the production process of polyether polyol by replacing all or part of the initiator with water, and can keep various indexes of the product consistent with those of the polyether in the conventional process.
Description
Technical Field
The invention belongs to the technical field of polyether polyol preparation, and particularly relates to a method for continuously preparing polyether, which can reduce production cost.
Background
Polyether polyol is an important chemical raw material, and polyurethane foam produced by using the polyether polyol is widely applied to the fields of furniture home appliances, automobiles, aerospace, buildings, clothing, packaging and the like. The method is characterized by the polyether polyol industry, and the polyether polyol productivity in the market is excessive, so that the polyether price is mainly influenced by the raw material price, and the overall profit margin is very low, so that the reduction of the raw material cost becomes the development direction of improving profits of various polyether manufacturers.
The continuous production process is generally catalyzed by Double Metal Cyanide (DMC) catalyst, has the advantages of high productivity, small occupied area, low cost and the like, has been adopted by a plurality of companies in the world, and has gradually expanded productivity and yield. During polyether production, it is generally believed that moisture in the feedstock reduces the activity of the DMC catalyst and even results in complete deactivation of the catalyst, and thus the moisture content of the feedstock is strictly controlled during either batch or continuous polyether production. Chinese patent publication CN113087892a also reports that the catalyst activity is protected by inhibiting the catalyst fall-off effect of water by adding an acid. However, in the actual production process, trace moisture in the raw materials can react with epoxide to generate polyether, and water is used as a difunctional initiator, so that the cost is low compared with that of small molecular dihydric alcohol commonly used in polyether production, and the raw material cost can be greatly saved if water is used as the initiator for producing polyether polyol.
Disclosure of Invention
The present invention addresses the problems of the prior art by providing a process for the continuous preparation of polyether polyols at low cost.
In order to achieve the above purpose, the present invention adopts the following technical scheme.
A process for the continuous preparation of polyethers comprising the steps of:
1) Polyether polyol and Double Metal Cyanide (DMC) catalyst are added into a reaction kettle in advance, epoxide is introduced into the reaction kettle for induction reaction after heating and temperature rising,
2) After the induction reaction of the catalyst is successful, continuously introducing epoxide, DMC catalyst and starter into a reaction kettle for reaction, and allowing a reaction product to flow out from the top of the kettle and enter an aging kettle to obtain polyether after the aging is completed;
the initiator is water or a mixture of water and dihydric alcohol, and the addition amount of the initiator is controlled so that the average water content of a reaction system is more than or equal to 0.01wt% and less than or equal to 1.15wt% under the continuous operation condition, wherein the average water content of the reaction system is the weight percentage of the water in the initiator converted to the total feeding amount according to the feeding proportion.
More preferably, the average water content in the reaction system is controlled within the following range in accordance with the concentration of the catalyst in the reaction system:
| catalyst concentration c, unit: ppm of | Water content, wt% |
| c≤15 | 0.01～0.15 |
| 15≤c＜30 | 0.15～0.30 |
| 30≤c＜60 | 0.30～0.45 |
| 60≤c＜100 | 0.45～0.65 |
| 100≤c＜200 | 0.65～0.85 |
| c≥200 | 0.85～1.15。 |
The average water content in the reaction system is the concentration of the moisture in the initiator, which is converted to the total feeding amount according to the feeding proportion, and is not the moisture value in the polyether product actually obtained.
Preferably, in the process, in step 1), the hydroxyl number of the polyether polyol added beforehand is from 20 to 280mg KOH/g, preferably from 40 to 120mg KOH/g.
Preferably, in step 1), the amount of catalyst added is greater, and the DMC catalyst concentration in the pre-feed is 20 to 5000ppm, preferably 60 to 1000ppm.
Preferably, the reactor temperature is raised to 130 to 190 ℃, preferably 145 to 160 ℃.
Preferably, the epoxide is ethylene oxide, propylene oxide or a mixture of the two in any proportion.
Preferably, the epoxide is added in the induction reaction of step 1) in an amount of 1% to 5% by mass of the polyether polyol added in advance.
The DMC catalyst is a conventional commercial catalyst.
Preferably, in the method, in step 2), the dihydric alcohol is one or a mixture of more selected from ethylene glycol, propylene glycol, diethylene glycol and dipropylene glycol.
Preferably, in step 2), the ratio of epoxide and initiator added is controlled according to the hydroxyl value of the product of 20 to 168mgKOH/g.
The catalyst concentration (c) of the reaction kettle refers to the catalyst concentration in the reaction system.
The epoxide, DMC catalyst, and small molecule starter can be fed in a manner conventional in the art.
After the system is stable, the temperature of the reaction kettle and the aging kettle is 130-190 ℃ and the pressure is 0-1 MPa.
Preferably, the polyethers prepared in accordance with the process of the present invention have a hydroxyl number of from 20 to 168mg KOH/g.
Preferably, the polyether prepared according to the process of the present invention has a viscosity of 100 to 10000cp@25 ℃, more preferably 100 to 2000cp@25 ℃.
Preferably, the polyether prepared according to the process of the present invention has a molecular weight distribution of from 1.00 to 2.00.
The invention has the following advantages:
by replacing all or part of the difunctional initiator with water, the raw material cost in the production process of the polyether polyol can be greatly reduced, and various indexes of the product can be kept consistent with those of the polyether in the conventional process. In addition, the activity of the catalyst can be fully ensured by controlling the water content under different conditions, and the safe and stable operation of production equipment is ensured.
Detailed Description
The method provided by the invention is further illustrated by the following examples, but the invention includes but is not limited to the examples listed and any other known modifications within the scope of the claims of the invention.
The product performance testing method comprises the following steps:
the polyether polyol hydroxyl value test method is referred to as follows: GB/T12008.3-2009
Polyether polyol viscosity test method reference: GB/T12008.7-2009
The molecular weight distribution test method of the polyether polyol uses gel chromatography (GPC).
Example 1
(1) Preparation of catalyst slurry: a catalyst slurry was prepared by previously dispersing 0.3g of DMC catalyst (Huai' an Maillard polyurethane Co., ltd.) into 1.5kg of polyether polyol (polyether base, hydroxyl value 56 mgKOH/g), and was added to a catalyst slurry tank.
(2) Induction reaction: 0.06g of DMC catalyst was dispersed in 1.5kg of polyether polyol (polyether base material, hydroxyl value: 56mg KOH/g) to obtain a dispersion, and the dispersion was charged into a 5L reactor, heated to 150℃and induced by adding 50g of propylene oxide.
(3) Polymerization reaction: when the pressure of the reaction kettle drops rapidly and the temperature rises rapidly, the catalyst is activated successfully, then the mixture of propylene glycol and water (the water content is 10wt percent and is converted to the concentration of the reaction system to be 0.247wt percent), the mixture of ethylene oxide, propylene oxide and catalyst slurry (the mass ratio of propylene glycol to water to propylene oxide to ethylene oxide to catalyst slurry is=9:1: 304.7:33.9:56.7) is continuously fed, after the reaction kettle is full, polyether polyol overflows from the top of the reaction kettle to an aging kettle for aging reaction, and after the reaction kettle is full, the polyether polyol overflows from the top of the aging kettle to a product storage tank. The reactor temperature was controlled at 150℃and the reactor pressure was controlled at 0.4MPa, the catalyst concentration was 28ppm and the residence time was 2 hours during continuous and steady operation, and the hydroxyl value of the product was 56.12mgKOH/g, the viscosity was 360cP (25 ℃) and the molecular weight distribution was 1.20.
Comparative example 1
Based on example 1, and under otherwise identical conditions, propylene glycol was used as initiator and the desired ratio was fed, the resulting product having a hydroxyl value of 56.03mgKOH/g, a viscosity of 355cP (25 ℃ C.) and a molecular weight distribution of 1.21.
Example 2
(1) Preparation of catalyst slurry: a catalyst slurry was prepared by previously dispersing 0.75g of DMC catalyst (Huai' an Maillard polyurethane Co., ltd.) into 1.5kg of polyether polyol (polyether base, hydroxyl value: 112 mgKOH/g), and was added to the catalyst slurry tank.
(2) Induction reaction: 0.25g of DMC catalyst was dispersed in 2.5kg of polyether polyol (polyether base material, hydroxyl value: 112 mgKOH/g) to obtain a dispersion, and the dispersion was charged into a 5L reactor, heated to 150℃and induced by adding 50g of propylene oxide.
(3) Polymerization reaction: when the pressure of the reaction kettle drops rapidly and the temperature rises rapidly, the catalyst is activated successfully, then a mixture of ethylene glycol and water (the water content is 17wt percent, the concentration of the reaction system is 0.63wt percent) is continuously fed (the target hydroxyl value is 112 mgKOH/g), propylene oxide and catalyst slurry (the mass ratio of ethylene glycol to water to propylene oxide to catalyst slurry is=83:17: 2187.2: 403.6), polyether polyol overflows from the top of the reaction kettle to an aging kettle for aging reaction after the reaction kettle is full, and the polyether polyol overflows from the top of the aging kettle to a product storage tank after the reaction kettle is full. The reactor temperature was controlled at 180℃and the reactor pressure was controlled at 0.5MPa, the catalyst concentration was 75ppm and the residence time was 4 hours during continuous steady operation, to finally obtain a hydroxyl value 111.45mgKOH/g, a viscosity 160cP (25 ℃) and a molecular weight distribution of 1.25.
Comparative example 2
Based on example 2, the starter was fed in the desired ratio using ethylene glycol under otherwise identical conditions, the resulting product having a hydroxyl value of 111.87mgKOH/g, a viscosity of 162cP (25 ℃ C.) and a molecular weight distribution of 1.24.
Example 3
(1) Preparation of catalyst slurry: a catalyst slurry was prepared by previously dispersing 0.45g of DMC catalyst (Huai' an Maillard polyurethane Co., ltd.) in 1.5kg of polyether polyol (polyether base, hydroxyl value: 28 mgKOH/g), and was added to a catalyst slurry tank.
(2) Induction reaction: 0.25g of DMC catalyst was dispersed in 2.5kg of a polyether polyol (polyether base, hydroxyl value: 28 mgKOH/g) to obtain a dispersion, and the dispersion was charged into a 5L reactor, heated to 170℃and induced by adding 30g of propylene oxide.
(3) Polymerization reaction: when the pressure of the reaction kettle drops rapidly and the temperature rises rapidly, the catalyst is activated successfully, water (the concentration of the target hydroxyl value is 28 mgKOH/g) is fed continuously (converted to 0.394wt percent of the concentration of the reaction system), propylene oxide and catalyst slurry (the mass ratio of water to propylene oxide to catalyst slurry=1:221.6:30.9) are added, polyether polyol overflows from the top of the reaction kettle to an aging kettle for aging reaction after the reaction kettle is full, and the polyether polyol overflows from the top of the aging kettle to a product storage tank after the reaction kettle is full. The temperature of the reaction kettle is controlled to be 180 ℃ during continuous and stable operation, the pressure of the reaction kettle is controlled to be 0.5MPa, the catalyst concentration is controlled to be 36.6ppm, the residence time is 6h, and the final product has a hydroxyl value of 28.23mgKOH/g, the viscosity is 950cP (25 ℃), and the molecular weight distribution is 1.16.
Comparative example 3
Based on example 3, the starter was diethylene glycol, fed in the desired ratio, and the resulting product had a hydroxyl value of 28.05mgKOH/g, a viscosity of 940cP (25 ℃) and a molecular weight distribution of 1.24, under otherwise identical conditions.
Example 4
(1) Preparation of catalyst slurry: 3g of DMC catalyst (Huai' an Maillard polyurethane Co., ltd.) was dispersed in 1.5kg of polyether polyol (polyether base, hydroxyl value 47 mgKOH/g) to prepare a catalyst slurry in advance, and the catalyst slurry was fed into a catalyst slurry tank.
(2) Induction reaction: 1.5g of DMC catalyst was dispersed in 2.5kg of polyether polyol (polyether base material, hydroxyl value: 47 mgKOH/g) to obtain a dispersion, and the dispersion was charged into a 5L reaction vessel, heated to 140℃and induced by adding 60g of propylene oxide.
(3) Polymerization reaction: after the reaction kettle is rapidly reduced in pressure and rapidly increased in temperature, the catalyst is successfully activated, diethylene glycol and water (converted to the concentration of a reaction system of 1.14 wt%) are continuously fed according to the required proportion (target hydroxyl value of 47 mgKOH/g), a mixture of propylene oxide and ethylene oxide (ethylene oxide accounts for 20 wt%) and a catalyst slurry (diethylene glycol: water: propylene oxide: ethylene oxide: catalyst slurry mass ratio=2:1:57.2:14.3:13.1), after the reaction kettle is full, polyether polyol overflows from the top of the reaction kettle to an aging kettle for aging reaction, and after the reaction kettle is full, polyether polyol overflows from the top of the aging kettle to a product storage tank. The reactor temperature was controlled at 140℃and the reactor pressure was controlled at 0.3MPa, the catalyst concentration was 299ppm, the residence time was 8 hours during the continuous and steady operation, and the hydroxyl value of the product was 112.20mgKOH/g, the viscosity was 180cP (25 ℃) and the molecular weight distribution was 1.19.
Comparative example 4
Based on example 4, the starter was supplied with dipropylene glycol in the desired ratio under the same conditions, and the resulting product had a hydroxyl value of 112.11mgKOH/g, a viscosity of 184cP (25 ℃ C.) and a molecular weight distribution of 1.20.
Example 5
(1) Preparation of catalyst slurry: 1.5g of DMC catalyst (Huai' an Maillard polyurethane Co., ltd.) was dispersed in 1.5kg of polyether polyol (polyether base, hydroxyl value 23 mgKOH/g) to prepare a catalyst slurry in advance, and the catalyst slurry was fed into a catalyst slurry tank.
(2) Induction reaction: 2.5g of DMC catalyst was dispersed in 2.5kg of polyether polyol (polyether base material, hydroxyl value: 23 mgKOH/g) to obtain a dispersion, and the dispersion was charged into a 5L reaction vessel, heated to 160℃and induced by adding 40g of propylene oxide.
(3) Polymerization reaction: when the pressure of the reaction kettle drops rapidly and the temperature rises rapidly, the catalyst is activated successfully, water (converted to the concentration of the reaction system of 0.35 wt%), ethylene oxide and catalyst slurry (the mass ratio of water to ethylene oxide to catalyst slurry=1:270.0:12.9) are fed continuously according to the required proportion (the target hydroxyl value of 23 mgKOH/g), polyether polyol overflows from the top of the aging kettle to the aging kettle for aging reaction after the reaction kettle is full, and the polyether polyol overflows from the top of the aging kettle to a product storage tank after the reaction kettle is full. The temperature of the reaction kettle is controlled to 160 ℃ during continuous and stable operation, the pressure of the reaction kettle is controlled to 0.4MPa, the catalyst concentration is 45ppm, the residence time is 6h, and finally the hydroxyl value of the product is 22.86mgKOH/g, the viscosity is 205cP (60 ℃), and the molecular weight distribution is 1.26.
Comparative example 5
Based on example 5, and under otherwise identical conditions, ethylene glycol was used as initiator and fed in the desired ratio, the resulting product had a hydroxyl value of 22.99mgKOH/g, a viscosity of 215cP (25 ℃ C.) and a molecular weight distribution of 1.26.
In the invention, by using water or a mixture thereof, the raw material cost of the polyether polyol production process can be greatly reduced under the condition that various indexes of the product are consistent with those of the conventional process polyether. In addition, the activity of the catalyst can be fully ensured by controlling the water content under different conditions, and the safe and stable operation of production equipment is ensured.
Claims (14)
1. A process for the continuous preparation of polyethers comprising the steps of:
1) Polyether polyol and DMC catalyst are added into a reaction kettle in advance, epoxide is introduced into the reaction kettle for induction reaction after heating and temperature rising,
2) After the induction reaction of the catalyst is successful, continuously introducing epoxide, DMC catalyst and starter into a reaction kettle for reaction, and allowing a reaction product to flow out from the top of the kettle and enter an aging kettle to obtain polyether after the aging is completed;
wherein the initiator is water or a mixture of water and dihydric alcohol, the addition amount of the initiator is controlled to ensure that the average water content in a reaction system is more than or equal to 0.01wt% and less than or equal to 1.15wt% under the continuous operation condition, the average water content in the reaction system is the weight percentage of the water in the initiator converted into the total feeding amount according to the feeding proportion,
the average water content in the reaction system is controlled within the following range according to the concentration of the catalyst in the reaction system:
wherein the addition amount of epoxide in the induction reaction of the step 1) is 1 to 5 percent of the mass of polyether polyol added in advance,
the molecular weight distribution of the polyether is 1.00-1.26.
2. The process according to claim 1, wherein the pre-added polyether polyol has a hydroxyl number of 20 to 280mg KOH/g.
3. The process according to claim 2, wherein the pre-added polyether polyol has a hydroxyl number of 40 to 120mg KOH/g.
4. A process according to any one of claims 1 to 3, wherein the DMC catalyst is added in step 1) in a concentration of 20 to 5000ppm.
5. The process of claim 4, wherein the DMC catalyst is added in step 1) at a concentration of 60 to 1000ppm.
6. A process according to any one of claims 1 to 3, wherein in step 1) the reactor temperature is raised to 130 to 190 ℃.
7. The process according to claim 4, wherein in step 1), the reactor temperature is increased to 145 to 160 ℃.
8. A process according to any one of claims 1 to 3 wherein the epoxide is ethylene oxide, propylene oxide or a mixture of the two in any proportion.
9. A process according to any one of claims 1 to 3, wherein the glycol is a mixture of one or more selected from ethylene glycol, propylene glycol, diethylene glycol and dipropylene glycol.
10. A process according to any one of claims 1 to 3, wherein the ratio of epoxide to starter is controlled according to the hydroxyl value of the polyether product obtained, from 20 to 168mgKOH/g.
11. A process according to any one of claims 1 to 3, wherein the reaction vessel and ageing vessel in step 2) are at a temperature of 130 to 190 ℃ and a pressure of 0 to 1MPa.
12. A method according to any one of claim 1 to 3, wherein,
the polyether prepared according to the method has a hydroxyl value of 20 to 168mgKOH/g.
13. A process according to any one of claims 1 to 3, wherein the polyether prepared according to the process has a viscosity of 100 to 10000cp @25 ℃.
14. A process according to any one of claims 1 to 3, wherein the polyether prepared according to the process has a viscosity of 100 to 2000cp@25 ℃.
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