Method for cyclically preparing polyether polyol by using DMC catalyst

Abstract

A method for preparing a polyether polyol in a continuous reaction cycle is described. In the method, a low molecular-weight alcohol is polymerized with an alkylene oxide to obtain a low molecular-weight polymer. The low molecular-weight polymer is used as an initiator to react with the alkylene oxide and the low molecular-weight alcohol in the presence of a DMC catalyst and an acid promoter to obtain an intermediate-target polymer. A portion of the intermediate-target polymer is used for producing the target polymer, and the other portion is recycled for reproduction of the intermediate-target polymer. No initiator prepared with a base catalyst is used, and thus the loss of material and the discharge of residue and waste water are reduced. The DMC concentration is kept constant in the target polymer during the production such that the dewatering time and induction time are greatly reduced.

Claims

1. A method of cyclically preparing a polyether polyol as a target polymer, the method comprising: polymerizing a low molecular-weight alcohol with an alkylene oxide to obtain a low molecular-weight polymer; obtaining an intermediate-target polymer by a first process in a reactor, the first process facilitating a first reaction of the low molecular-weight polymer with the alkylene oxide while a first amount of the low molecular-weight alcohol is introduced into the reactor; and obtaining the target polymer by a second process in the reactor using a first portion of the intermediate-target polymer, wherein: a second portion of the intermediate-target polymer is recycled for reproduction of the intermediate-target polymer, a double metal cyanide (DMC) catalyst is used as a catalyst of the first reaction, an acid is used as a promoter of the first reaction, the intermediate-target polymer and the low molecular-weight polymer have a same average molecular weight, the DMC catalyst is a double metal cyanide complex catalyst for ring opening in polymerization of epoxy, the acid is one of a nitric acid, a phosphoric acid, and a sulfuric acid, or a mixture of any two or three thereof, the alkylene oxide is one of a propylene oxide, a butylene oxide, a mixture of ethylene oxide and the propylene oxide, a mixture of an ethylene oxide and a butylene oxide, a mixture of the propylene oxide and the butylene oxide, and a mixture of the ethylene oxide, the propylene oxide and the butylene oxide, the low molecular-weight alcohol is a monohydric alcohol or a polyhydric alcohol, the monohydric alcohol being one of an allyl alcohol or a butanol, the polyhydric alcohol being one of an ethylene glycol, a propylene glycol, a butylene glycol, and a glycerol, and the first process comprises the following steps: 1a) introducing the low molecular-weight polymer into the reactor, the low molecular-weight polymer having been pre-added with the DMC catalyst and the acid; 1b) dewatering by a bubbling nitrogen for at least 10 minutes at a first temperature range of 100-175 C. under vacuum at a first pressure not higher than 0.085 MPa; 1c) turning off the bubbling nitrogen and further vacuuming for at least 10 minutes; 2) introducing into the reactor the alkylene oxide in an amount that is no more than 20% by weight (wt %) of the low molecular-weight polymer; 3a) simultaneously and continuously introducing the alkylene oxide and the first amount of the low molecular-weight alcohol into the reactor, the reactor maintained at a second temperature range of 120-180 C. and at a second pressure not higher than 0.2 MPa; 3b) introducing at least 10 wt % of the alkylene oxide into the reactor after the introducing of the first amount of the low molecular-weight alcohol is completed; 3c) waiting until no substantial pressure drop is observed in the reactor; and 3d) discharging the reactor to obtain the intermediate-target polymer.

2. The method of claim 1, wherein: the second process facilitates a second reaction of the first portion of the intermediate-target polymer with the alkylene oxide while a second amount of the low molecular-weight alcohol is introduced into the reactor, the DMC catalyst is further used as a catalyst of the second reaction, the acid is further used as a promoter of the second reaction, and the second process comprises the following steps: 4a) introducing the first portion of the intermediate-target polymer into the reactor, the first portion of the intermediate-target polymer having been pre-added with the DMC catalyst and the acid; 4b) dewatering by the bubbling nitrogen for at least 10 minutes at the first temperature range of 100-175 C. under vacuum at the first pressure not higher than 0.085 MPa; 4c) turning off the bubbling nitrogen and further vacuuming for at least 10 minutes; 5) introducing into the reactor the alkylene oxide in an amount that is no more than 20 wt % of the first portion of the intermediate-target polymer; 6a) simultaneously and continuously introducing the alkylene oxide and the second amount of the low molecular-weight alcohol into the reactor, the reactor maintained at the second temperature range of 120-180 C. and at the second pressure not higher than 0.2 MPa; 6b) introducing at least 10 wt % of the alkylene oxide into the reactor after the introducing of the second amount of the low molecular-weight alcohol is completed; 6c) waiting until no substantial pressure drop is observed in the reactor; and 6d) discharging the reactor to obtain the target polymer.

3. The method of claim 1, further comprising steps of: 1) adding the low molecular-weight polymer as the first initiator to a reactor, wherein the low molecular-weight polymer is pre-added with the DMC catalyst and the acid; evacuating, heating, and dewatering by bubbling nitrogen for at least 10 minutes at a first temperature range of 100-175 C. under vacuum at a first pressure not higher than 0.085 MPa; and then closing the nitrogen source, and further evacuating for at least 10 minutes; 2) after the dewatering, introducing the alkylene oxide in an amount that is no more than 20% by weight (wt %) of the low molecular-weight polymer in Step 1), such that a significant pressure drop and a significant temperature rise in the reactor is induced; 3) while keeping a second temperature range at 120-180 C. and a second pressure not higher than 0.2 MPa in the reactor, simultaneously and continuously adding metered alkylene oxide and the low molecular-weight alcohol; adding at least 10 wt % of the alkylene oxide after the addition of the low molecular weight alcohol is completed; after the alkylene oxide is completely loaded and no obvious pressure drop in the reactor; evacuating and discharging in the reactor after the temperature in the reactor drops to 70-80 C. to obtain the intermediate-target polymer, wherein the first portion of the intermediate-target polymer is used for preparing the target polymer, and the second portion of the intermediate-target polymer is recycled back to the reactor for preparing the intermediate-target polymer; 4) adding the intermediate-target polymer obtained in Step 4) to the reactor, wherein the intermediate-target polymer is pre-added with the DMC catalyst and the acid; the evacuating, the heating, and the dewatering under vacuum by bubbling nitrogen is carried out for at least 10 minutes at the first temperature range of 100-175 C. under the first pressure not higher than 0.085 MPa; then closing the nitrogen source, and further retaining the evacuating for at least 10 minutes; 5) after the dewatering, terminating the evacuating, and introducing the alkylene oxide in an amount that is no more than 20 wt % of the intermediate-target polymer in Step 4), such that a significant pressure drop and a significant temperature rise in the reactor is induced; 6) while keeping the second temperature range at 120-180 C. and the second pressure not higher than 0.2 MPa, simultaneously and continuously adding metered alkylene oxide and the low molecular-weight alcohol; adding at least 10 wt % of the alkylene oxide after the addition of the low molecular-weight alcohol is completed; after the alkylene oxide is completely loaded and no obvious pressure drop in the reactor; evacuating and discharging the reactor after the temperature in the reactor drops to 70-80 C. to obtain the target polymer; and 7) with the intermediate-target polymer obtained Step 3) as the second initiator, cyclically preparing the intermediate-target polymer and the target polymer following operations in Steps 1-6.

4. The method of claim 1, wherein the target polymer is a polyoxyalkylene ether monol, and wherein an average molecular weight of both the low molecular-weight polymer and the intermediate-target polymer is 300-500.

5. The method of claim 1, wherein the target polymer is a polyoxyalkylene ether diol, and wherein an average molecular weight of both the low molecular-weight polymer and the intermediate-target polymer is 500-700.

6. The method of claim 1, wherein the target polymer is a polyoxyalkylene ether triol, and wherein an average molecular weight of both the low molecular-weight polymer and the intermediate-target polymer is 700-1000.

7. The method of claim 1, wherein the alkylene oxide is a mixture of propylene oxide and ethylene oxide containing no higher than 80% of ethylene oxide in the mixture.

8. The method of claim 3, wherein a content of K.sup.+and a content of Na.sup.+in the low molecular-weight polymer as the first initiator in Step 1) are less than 10 ppm respectively.

9. The method of claim 3, wherein the DMC catalyst is used in Step 1) in an amount of 10-600 ppm based on a weight of the intermediate-target polymer obtained in Step 3).

10. The method of claim 3, wherein the DMC catalyst is used in Step 4) in an amount of 0-500 ppm based on a weight of the target polymer obtained in Step 6).

11. The method of claim 3, wherein the acid in Steps 1), 3), 4) and 6) is the sulfuric acid, the phosphoric acid, or a mixture thereof.

12. The method of claim 3, wherein the low molecular-weight polymer as the first initiator in Steps 1) and 4) contains the acid no more than 200 ppm.

13. The method of claim 3, wherein the low molecular-weight alcohol in Steps 3) and 6) contains the acid no more than 200 ppm.

14. The method of claim 3, wherein the adding of the low molecular-weight alcohol is completed before consuming all the alkylene oxide in Steps 3) and 6), and 20-40 wt % of the alkylene oxide is reserved to be added after the addition of the low molecular-weight alcohol is completed.

15. The method of claim 2, further comprising steps of: 1) adding the low molecular-weight polymer as the first initiator to a reactor, wherein the low molecular-weight polymer is pre-added with the DMC catalyst and the acid; evacuating, heating, and dewatering by bubbling nitrogen for at least 10 minutes at a first temperature range of 100-175 C. under vacuum at a first pressure not higher than 0.085 MPa; and then closing the nitrogen source, and further evacuating for at least 10 minutes; 2) after the dewatering, introducing the alkylene oxide in an amount that is no more than 20% by weight (wt %) of the low molecular-weight polymer in Step 1), such that a significant pressure drop and a significant temperature rise in the reactor is induced; 3) while keeping a second temperature range at 120-180 C. and a second pressure not higher than 0.2 MPa in the reactor, simultaneously and continuously adding metered alkylene oxide and the low molecular-weight alcohol; adding at least 10 wt % of the alkylene oxide after the addition of the low molecular weight alcohol is completed; after the alkylene oxide is completely loaded and no obvious pressure drop in the reactor; evacuating and discharging in the reactor after the temperature in the reactor drops to 70-80 C. to obtain the intermediate-target polymer, wherein the first portion of the intermediate-target polymer is used for preparing the target polymer, and the second portion of the intermediate-target polymer is recycled back to the reactor for preparing the intermediate-target polymer; 4) adding the intermediate-target polymer obtained in Step 4) to the reactor, wherein the intermediate-target polymer is pre-added with the DMC catalyst and the acid; the evacuating, the heating, and the dewatering under vacuum by bubbling nitrogen is carried out for at least 10 minutes at the first temperature range of 100-175 C. under the first pressure not higher than 0.085 MPa; then closing the nitrogen source, and further retaining the evacuating for at least 10 minutes; 5) after the dewatering, terminating the evacuating, and introducing the alkylene oxide in an amount that is no more than 20 wt % of the intermediate-target polymer in Step 4), such that a significant pressure drop and a significant temperature rise in the reactor is induced; 6) while keeping the second temperature range at 120-180 C. and the second pressure not higher than 0.2 MPa, simultaneously and continuously adding metered alkylene oxide and the low molecular-weight alcohol; adding at least 10 wt % of the alkylene oxide after the addition of the low molecular-weight alcohol is completed; after the alkylene oxide is completely loaded and no obvious pressure drop in the reactor; evacuating and discharging the reactor after the temperature in the reactor drops to 70-80 C. to obtain the target polymer; and 7) with the intermediate-target polymer obtained Step 3) as the second initiator, cyclically preparing the intermediate-target polymer and the target polymer following operations in Steps 1-6.

16. The method of claim 15, wherein a content of K.sup.+and a content of Na.sup.+in the low molecular-weight polymer as the first initiator in Step 1) are less than 10 ppm respectively.

17. The method of claim 15, wherein the DMC catalyst is used in Step 1) in an amount of 10-600 ppm based on a weight of the intermediate-target polymer obtained in Step 3), and wherein the DMC catalyst is used in Step 4) in an amount of 0-500 ppm based on a weight of the target polymer obtained in Step 6).

18. The method of claim 15, wherein the acid in Steps 1), 3), 4) and 6) is the sulfuric acid, the phosphoric acid, or a mixture thereof.

19. The method of claim 15, wherein the low molecular-weight polymer as the first initiator in Steps 1) and 4) contains the acid no more than 200 ppm, and wherein the low molecular-weight alcohol in Steps 3) and 6) contains the acid no more than 200 ppm.

20. The method of claim 15, wherein the adding of the low molecular-weight alcohol is completed before consuming all the alkylene oxide in Steps 3) and 6), and 20-40 wt % of the alkylene oxide is reserved to be added after the addition of the low molecular-weight alcohol is completed.

Description

DETAILED DESCRIPTION

(1) The present disclosure is described in further detail with reference to specific embodiments.

(2) It should be noted that the starter compounds used in reaction examples below are merely for illustrative purposes, and the protection scope of the present disclosure is not limited thereto the cited starter compounds.

(3) The DMC catalyst used in the present disclosure is prepared following the method as described in ZL200710019506.7, however the double metal cyanide complex catalysts may be prepared following the method as described in CN201410121198.9, CN03813844.1, and CN200680024203.8.

EXAMPLE 1

Preparation of Intermediate-target Polymer Polyoxypropylene Propylene Glycol Ether (Mn=600) from the Initiator Polyoxypropylene Propylene Glycol Ether (Mn=600) and Propylene Glycol

(4) 1) In a 10 m.sup.3 reactor equipped with an external circulating pump, 2200 kg polyoxypropylene propylene glycol ether (M n=600) initiator (which might be prepared with a conventional KOH catalyst, contained <5 ppm of K+ and Na+ ions, and is premixed with 66 g concentrated sulfuric acid) and 402 g DMC catalyst are added into the reactor to form a mixture. The mixture is stirred, purged with nitrogen, evacuated, and heated. The external circulating pump is activated, and dewatering is performed under vacuum by bubbling nitrogen for 60 minutes at a temperature between 135-145 C. under a pressure below 0.095 MPa. The nitrogen source is turned off, and the reactor is evacuated for an additional 20 minutes.

(5) 2) The vacuum valve connected to the reactor is closed to stop evacuating, and 176 kg propylene oxide is introduced into the reactor. The initiation of reaction is indicated by a significant pressure drop reactor and a significant temperature rise in the reactor.

(6) 3) While the temperature is kept at between 150-160 C., and the pressure is kept below 0.02 MPa, 3395 kg propylene oxide and 740 kg propylene glycol (premixed with 37 g concentrated sulfuric acid) are added into the reactor simultaneously in a continuous-feed manner. 1531 kg propylene oxide is added into the reactor 220 minutes after the addition of propylene oxide and propylene glycol is completed. It may take 80 minutes for the addition of propylene oxide to be completed, and the reaction may proceed until there is no obvious pressure drop in the reactor. The reactor is then evacuated to remove remaining gases, and the vacuum valve is closed once the remaining gases are removed. The material in the reactor is discharged after the temperature of the reactor is cooled to 70-80 C. An intermediate-target polymer polyoxypropylene propylene glycol ether (M n=600) is obtained, a portion of which is used for preparing the target polymer, and the other portion is recycled back to the reactor.

(7) The obtained intermediate-target polymer polyoxypropylene propylene glycol ether (M n=600) is analyzed to have a DMC content of 50 ppm, a hydroxyl value (mg KOH/g) of 188.74, a viscosity (25 C., mPa.Math.s) of 107, and a molecular-weight distribution (either weight average molecular weight or number average molecular weight) D of 1.14.

EXAMPLE 2

Preparation of Polyoxyethylene/Propylene Propylene Glycol Ether (Mn=2000) from Intermediate-Target Polymer Polyoxypropylene Propylene Glycol Ether (Mn=600)

(8) 1) In a 10 m.sup.3 reactor equipped with an external circulating pump, 2400 kg target intermediate polymer polyoxypropylene propylene glycol ether (M n=600) prepared in Example 1 as an initiator, and 120 g DMC catalyst are added into the reactor to form a mixture. The mixture is stirred, purged with nitrogen, evacuated, and heated. The external circulating pump is activated, and the reactor is evacuated for 30 minutes at a temperature between 135-145 C. under a pressure below 0.095 MPa.

(9) 2) The vacuum valve connected to the reactor is closed to stop evacuating, and 192 kg alkylene oxide mixture (in which ethylene oxide/propylene oxide was 2:8) is introduced into the reactor. The initiation of reaction is indicated by a significant temperature rise in the reactor.

(10) 3) While the temperature is kept at 130-135 C., and the pressure is kept below 0.02 MPa, 5408 kg alkylene oxide mixture (in which ethylene oxide to propylene oxide ratio is 2:8) is introduced into the reactor in a continuous-feed manner. It may take 160 minutes for the addition of the alkylene oxide mixture to be completed, and the reaction may proceed until there is no obvious pressure drop in the reactor. The reactor is then evacuated to remove remaining gases, and the vacuum valve is closed once the remaining gases are removed. The material is discharged after the temperature of the reactor is cooled to between 70-80 C., and the target polymer polyoxyethylene/propylene propylene glycol ether (M n=2000) is obtained.

(11) The target polymer polyoxyethylene/propylene propylene glycol ether (M n=2000) is analyzed to have a DMC content of 30 ppm, a hydroxyl value (mg KOH/g) of 55.81, a viscosity (25 C., mPa.Math.s) of 300, and a molecular weight distribution (either weight average molecular weight or number average molecular weight) D of 1.04.

EXAMPLE 3

Preparation of Intermediate-target Polymer Polyoxypropylene Propylene Glycol Ether (Mn=600) from Intermediate-Target Polymer Polyoxypropylene Propylene Glycol Ether (Mn=600) and Propylene Glycol

(12) 1) In a 10 m.sup.3 reactor equipped with an external circulating pump, 1800 kg intermediate-target polymer polyoxypropylene propylene glycol ether (M n=600) prepared in Example 1 as an initiator (premixed with 54 g concentrated sulfuric acid) and 310 g DMC catalyst are added into a reactor to form a mixture. The mixture is stirred, purged with nitrogen, evacuated, and heated. The external circulating pump is activated, and the reactor is evacuated for 30 minutes at a temperature 135-145 C. under a pressure below 0.095 MPa.

(13) 2) The vacuum valve connected to the reactor is closed to stop evacuating, and 144 kg propylene oxide is introduced into the reactor. The initiation of the reaction is indicated by a significant temperature rise in the reactor.

(14) 3) While the temperature is kept at 150-160 C., and the pressure is kept below 0.02 MPa, 3645 kg propylene oxide and 785 kg propylene glycol (premixed with 39 g concentrated sulfuric acid) are added into the reactor in a continuous-feed manner. 1624 kg propylene oxide is further added 200 minutes after the addition of propylene oxide and propylene glycol is completed. It may take 80 minutes for the addition of propylene oxide to be completed, and the reaction may proceed until there was no obvious pressure drop in the reactor. The reactor is then evacuated to remove remaining gases, and the vacuum valve is closed once the remaining gases are removed. The material is discharged after the temperature is cooled to between 70-80 C., and an intermediate-target polymer polyoxypropylene propylene glycol ether (M n=600) is obtained, a portion of which is used for preparing the target polymer, and the other portion is recycled back to the reactor.

(15) The obtained intermediate-target polymer polyoxypropylene propylene glycol ether (M n=600) is analyzed to have a DMC content of 50 ppm, a hydroxyl value (mg KOH/g) of 185.96, a viscosity (25 C., mPa.Math.s) of 112, and a molecular weight distribution (either weight average molecular weight or number average molecular weight) D of 1.17.

COMPARATIVE EXAMPLE 1 (RELATING TO EXAMPLES 1 AND 3)

Preparation of Intermediate-target Polymer Polyoxypropylene Propylene Glycol Ether (Mn=600) from Low Molecular-weight Alcohol Propylene Glycol

(16) 1) In a 10 m.sup.3 reactor equipped with an external circulating pump, 1013 kg propylene glycol as an initiator, and 24 kg KOH as a catalyst are added into a reactor to form a mixture. The mixture is stirred, purged with nitrogen, and evacuated for 5 minutes. Then, the external circulating pump is activated.

(17) 2) The vacuum valve connected to the reactor is closed to stop evacuating, and 100 kg propylene oxide is introduced into the reactor at a temperature ranging from 110 to 120 C. The initiation of the reaction is indicated by a slow temperature rise and a slow pressure drop.

(18) 3) While the temperature is kept at 110-120 C., and the pressure is kept below 0.4 MPa, 6887 kg propylene oxide is added into the reactor in a continuous-feed manner. It may take 300 minutes for the addition of propylene oxide to be completed, and the reaction may proceed until there was no obvious pressure drop in the reactor. The reactor is then evacuated to remove remaining gases, and the vacuum valve is closed once the remaining gases are removed. After the temperature of the reactor is cooled to between 90-100 C., the material is transferred to a post-processing unit.

(19) 4) 400 kg water is added to the post-processing unit and stirred for 30 minutes. 45 kg of 85% phosphoric acid is added and stirred for 60 minutes. 12 kg refining agent and 16 kg clay were added and stirred for 30 minutes. Dewatering is conducted for 4 hours at 110-120 C. under 0.095 MPa. After filtering, cooling, and discharging, the intermediate-target polymer polyoxypropylene propylene glycol ether (M n=600) is obtained, all of which is used for producing the target polymer.

(20) The obtained intermediate-target polymer polyoxypropylene propylene glycol ether (M.sub.n=600) is analyzed to have a hydroxyl value (mg KOH/g) of 185.96, a viscosity of (25 C., mPa.Math.s) 102; a K.sup.+ and Na.sup.+ content less than 5 ppm respectively, and a molecular weight distribution (either weight average molecular weight or number average molecular weight) D of 1.24.

(21) A portion of the intermediate-target polymer prepared with a base catalyst in Example 1 is used to prepare the target polymer in Example 2, and the other portion is recycled to prepare the intermediate-target polymer in the presence of the DMC catalyst in Example 3, so that no intermediate-target polymer prepared with a base catalyst is used in further preparation of the target polymer. However, the total amount of intermediate-target polymer prepared with a base catalyst in Comparative Example 1 is used to prepare the target polymer, so the process for preparing the needed intermediate-target polymer with a base catalyst in Comparative Example 1 needs to be repeated when producing the next batch of the target polymer. Therefore, in the present disclosure, no post-processing is needed once the intermediate-target polymer is recycled for reproduction, thereby reducing the production time, lowering the loss of material and energy consumption, and decreasing the discharge of residue and waste water.

(22) Under the same conditions, the production time, the loss of material per unit of product, the energy consumption, and the amounts of discharged solid waste and waste water resulting from prior art processes and the present method for preparing different products are listed in a table below.

(23) TABLE-US-00001 Loss of Waste Post- material residue water Starter compound of Target processing time Induction Dewatering kg/ton kg/ton kg/ton low molecular-weight polymer Yield min/ton of time time of of of alcohol M.sub.n Process t product min/reactor min/reactor product product product Monohydric Allyl 1500 The 90 6 <2 30 2.5 2.5 4.2 alcohol alcohol present disclosure Prior art 18 16 80 8 8 13 900 The 36 15 <2 30 7 7 11 present disclosure Prior art 45 16 80 20 20 33 Dihydric Ethylene 1600 The 64 8 <2 30 4 4 6 alcohol glycol present disclosure Prior art 25 16 80 12 12 19 Propylene 2000 The 80 7 <2 30 3 3 5 glycol present disclosure Prior art 21 16 80 9 9 15 Butylene 2500 The 100 5 <2 30 2 2 4 glycol present disclosure Prior art 16 17 80 7 7 12 Trihydric Glycerol 3000 The 90 6 <2 30 2.5 2.5 4.2 alcohol present disclosure Prior art 18 16 80 8 8 13 Remark 1. The loss of material, residue, and waste water in the table include exclusively the loss, residue, and waste water resulting from the process itself. With the increase of the yield, that is, with the increase of the cycle number, the intermediate-target polymer used in the present disclosure requires no post-processing, and thus no new post-processing time, residue, and waste water are produced, whereby the post-processing time, residue, and waste water are approximately 0. With the increase of the yield, after the intermediate-target polymer prepared with a base catalyst in the prior art is consumed totally, the intermediate-target polymer prepared with a base catalyst has to be produced and post-processed again, so the post-processing time, residue, and waste water are produced again, whereby the post-processing time, residue, and waste water are approximately a constant value. The loss of material is calculated based on the whole process from the preparation of the intermediate- target polymer from a low molecular-weight alcohol and then to the preparation of the target polymer from the intermediate-target polymer.

EXAMPLE 4

Preparation of Polyoxypropylene Ether (Mn=3000) from Intermediate-target Polymer Polyoxypropylene Glycerol Ether (Mn=800) and Glycerol

(24) 1) In a 10 m.sup.3 reactor equipped with an external circulating pump, 800 kg cyclically prepared intermediate-target polymer polyoxypropylene glycerol ether (M.sub.n=800) as an initiator (premixed with 24 g phosphoric acid) and 182 g DMC catalyst are added into a reactor to form a mixture. The mixture is stirred, purged with nitrogen, evacuated, and heated. The external circulating pump is activated, and the reactor was evacuated for 30 minutes at a temperature 135-145 C. under a pressure below 0.095 MPa.

(25) 2) The vacuum valve connected to the reactor is closed to stop evacuating and 64 kg propylene oxide is introduced into the reactor. The initiation of the reaction is indicated by a significant temperature rise in the reactor.

(26) 3) While the temperature is kept at 130-135 C. and the pressure is kept below 0.02 MPa, 4196 kg propylene oxide and 155 kg glycerol (premixed with 7.8 g phosphoric acid) are added into the reactor in a continuous-feed manner. 2839 kg propylene oxide is further added 150 minutes after the addition of propylene oxide and glycerol is completed. It may take 60 minutes for the addition of propylene oxide to be completed, and the reaction may proceed until there was no obvious pressure drop in the reactor. The reactor is evacuated to remove remaining gases, and then the vacuum valve is closed once the remaining gases are removed. The material is discharged after the temperature is cooled to 70-80 C., and the target polymer polyoxypropylene glycerol ether (M.sub.n=3000) is obtained.

(27) The obtained target polymer polyoxypropylene glycerol ether (M.sub.n=3000) is analyzed to have a DMC content of 30 ppm, a hydroxyl value (mg KOH/g) of 56.93, a viscosity (25 C., mPa.Math.s) of 567, and a molecular weight distribution (either weight average molecular weight or number average molecular weight) D of 1.06.

COMPARATIVE EXAMPLES 2-5 (RELATING TO EXAMPLE 4)

Preparation of Polyoxypropylene Ether (Mn=3000) from Intermediate-target Polymer Polyoxypropylene Glycerol Ether (Mn=800) and Glycerol

(28) Except for the reservation ratio of PO, all the conditions and amounts of materials in Comparative Examples 2-5 are the same as those in Example 4. When the reservation ratio of PO is less than 10%, the molecular weight distribution of the target polymer is wide. When the reservation ratio of PO is larger than 80%, the reaction may fail to proceed.

(29) TABLE-US-00002 Molecular weight distribution weight average molecular Reservation weight/number ratio of Reaction time average PO minutes molecular weight Example 4 40% 210 1.06 Comparative 8% 203 1.58 Example 2 Comparative 10% 215 1.37 Example 3 Comparative 80% 619 1.39 Example 4 Comparative 85% After the introduction Example 5 of glycerol and PO is started, the pressure in the reactor does not decrease any longer, and the reaction is terminated. Remark The reservation ratio of PO refers to the ratio of alkylene oxide introduced after the addition of the low molecular-weight alcohol is completed to the total amount of alkylene oxide, with the provision that the low molecular-weight alcohol and the remaining alkylene oxide are added simultaneously beforehand

EXAMPLE 20

(30) The experiment results obtained in the examples of the present disclosure are summarized, and the comparisons between the target products prepared by the present disclosure and the prior art method are listed in a table below.

(31) TABLE-US-00003 Results of comparison of polyether polyol prepared from various raw materials Low Intermediate molecular- molecular- Target polymer Starter compound of weight weight Molecular Hydroxyl Molecular Induction Dewatering low molecular-weight polymer polymer weight value (mg weight time time alcohol (M.sub.n) (M.sub.n) (M.sub.n) KOH/g) distribution (min) (min) Monohydric Allyl 200 200 1496 37.5 1.22 8 30 alcohol alcohol 600 600 1484 37.8 1.18 <2 30 400 400 1504 37.3 1.06 <2 30 Prior art 1492 37.6 1.24 16 80 Butanol 200 200 889 63.1 1.17 8 30 600 600 904 62.1 1.16 <2 30 400 400 898 62.5 1.08 <2 30 Prior art 893 62.8 1.21 18 80 Dihydric Ethylene 400 400 1617 69.4 1.18 5 30 alcohol glycol 1000 1000 1605 69.9 1.18 <2 30 600 600 1587 70.7 1.07 <2 30 Prior art 1587 70.7 1.21 17 80 Propylene 400 400 2020 55.5 1.19 5 30 glycol 1000 1000 1992 56.3 1.18 <2 30 600 600 2008 55.8 1.07 <2 30 Prior art 2012 55.7 1.20 15 80 Butylene 400 400 2507 44.8 1.19 7 30 glycol 1000 1000 2510 44.7 1.19 <2 30 600 600 2495 45.0 1.06 <2 30 Prior art 2490 45.1 1.20 17 80 Trihydric Glycerol 500 500 3011 55.9 1.20 5 30 alcohol 1200 1200 2997 56.2 1.23 <2 30 800 800 2990 56.3 1.05 <2 30 Prior art 3005 56.0 1.26 18 80

(32) It can be seen from the table above that the target polymer produced through the technical solution of the present disclosure may have a narrow molecular weight distribution compared with the target polymer produced in the prior art, and the induction time and dewatering time are short in the present disclosure. By using the technical solution of the present disclosure, the molecular weight distribution of the target polymer may be wide in the situation that the intermediate-target polymer has a low or high molecular weight distribution.

EXAMPLE 21

(33) The results for the target products prepared under some reaction conditions different from those in the present disclosure by which the intermediate-target polymer (M.sub.n=600) and the target polymer (M.sub.n=2500) are prepared with butylene glycol as a starter compound while the other reaction conditions are kept unchanged, are listed in a table below:

(34) TABLE-US-00004 Comparison of the effect of different reaction conditions in the present disclosure on the target products Weight of Weight of Molecular weight alkylene oxide alkylene oxide distribution initiating the initiating the Acid (weight average reaction in Step reaction in Step content in molecular 2)/weight of low 5)/weight of initiator in Hydroxyl weight/number molecular- intermediate- Steps 1) value average Reaction weight initiator target polymer in and 4) (mg molecular Appearance of condition in Step 1), (%) Step 4), (%) (ppm) KOH/g) weight) product No. 1 20 20 200 44.5 1.21 Light brown No. 2 3 3 80 44.1 1.19 Colorless and clear No. 3 10 10 50 45.1 1.06 Colorless and clear No. 4 3 3 80 44.7 1.18 Colorless and clear No. 5 10 10 50 44.2 1.07 colorless and clear No. 6 25 25 150 44.8 1.29 Light brown No. 7 15 15 250 45.1 The reaction cannot be initiated due to an excessively high acid content. No. 8 22 22 80 44.3 1.21 Dark color No. 9 5 5 30 44.5 1.12 colorless and clear

(35) It can be seen from the table above that during the production of the target polymer through the technical solution of the present disclosure, the target polymer may have a wide molecular weight distribution in the situation that the amounts of alkylene oxide is not optimal (small or large), or the amount of acid is too high. When the acid is introduced in a large amount, the color of the target product is dark. When the acid is introduced in an excessively large amount, the reaction cannot be initiated.

EXAMPLE 22

(36) The results for the target products, prepared under the same conditions in the method of the present disclosure by which the intermediate-target polymer (M.sub.n=600) and the target polymer (M.sub.n=1600) are prepared with ethylene glycol as a starter compound except that different acids and alkylene oxide are used, are listed in a table below:

(37) TABLE-US-00005 Comparison of the effect of different acids and alkylene oxide in the present disclosure on the target products Molecular weight distribution Amount of (weight average DMC Amount of molecular catalyst in DMC catalyst weight/number Reaction Step 1) in Step 4) Hydroxyl value average molecular condition Acid Alkylene oxide (ppm) (ppm) (mg KOH/g) weight) Example 1 Sulfuric Propylene oxide 30 40 70.2 1.04 acid 100% Example 2 Phosphoric Butylene oxide 20 20 70.8 1.28 acid 100% Example 3 Nitric acid Ethylene oxide 10 0 71.1 1.34 80% Propylene oxide 20% Example 4 Sulfuric Ethylene oxide 100 400 The proportion of ethylene oxide acid 90% is relatively high and the reaction Phosphoric Propylene oxide rate is low, the product appears acid 10% cloudy in a later stage of the reaction. Example 5 Sulfuric Ethylene oxide 120 60 70.5 1.05 acid 50% Nitric acid Butylene oxide 50% Example 6 Phosphoric Propylene oxide 400 0 70.0 1.07 acid 50% Nitric acid Butylene oxide 50% Example 7 Sulfuric Ethylene oxide 600 500 69.7 1.32 acid 30% Phosphoric Propylene oxide acid 40% Nitric acid Butylene oxide 40%

(38) It can be seen from the table above that by means of the technical solution of the present disclosure, the species of acids has no obvious effect on the target product under different reaction conditions. When the proportion of ethylene oxide in the alkylene oxide is relatively high and the reaction rate is relatively slow, the product appears cloudy. When the amount of catalyst is relatively low or high, the product may have a wide molecular weight distribution.

(39) It should be noted that the foregoing descriptions are merely preferred examples of the present disclosure, and the protection scope of the present disclosure is not limited thereto. Any combinations or equivalent substitutions made based on the above examples are covered by the protection scope of the present disclosure.