CN220091424U - Potassium and sodium ion removing device for high-activity high-molecular-weight polyether - Google Patents
Potassium and sodium ion removing device for high-activity high-molecular-weight polyether Download PDFInfo
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- CN220091424U CN220091424U CN202321616120.5U CN202321616120U CN220091424U CN 220091424 U CN220091424 U CN 220091424U CN 202321616120 U CN202321616120 U CN 202321616120U CN 220091424 U CN220091424 U CN 220091424U
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- tower
- polyether
- potassium
- sodium ion
- desalting
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- 239000004721 Polyphenylene oxide Substances 0.000 title claims abstract description 86
- 229920000570 polyether Polymers 0.000 title claims abstract description 86
- 230000000694 effects Effects 0.000 title claims abstract description 28
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 title claims abstract description 18
- 239000011591 potassium Substances 0.000 title claims abstract description 18
- FKNQFGJONOIPTF-UHFFFAOYSA-N Sodium cation Chemical compound [Na+] FKNQFGJONOIPTF-UHFFFAOYSA-N 0.000 title claims abstract description 17
- 229910001414 potassium ion Inorganic materials 0.000 title claims abstract description 17
- 229910001415 sodium ion Inorganic materials 0.000 title claims abstract description 17
- 238000010612 desalination reaction Methods 0.000 claims abstract description 51
- 238000011033 desalting Methods 0.000 claims abstract description 48
- 239000000463 material Substances 0.000 claims abstract description 26
- 238000006386 neutralization reaction Methods 0.000 claims abstract description 20
- 239000012266 salt solution Substances 0.000 claims abstract description 20
- 229920005862 polyol Polymers 0.000 claims abstract description 18
- 150000003077 polyols Chemical class 0.000 claims abstract description 18
- 238000003860 storage Methods 0.000 claims abstract description 10
- 238000007599 discharging Methods 0.000 claims description 9
- 230000007704 transition Effects 0.000 claims description 6
- 238000007701 flash-distillation Methods 0.000 claims 3
- 230000008676 import Effects 0.000 claims 1
- 238000007670 refining Methods 0.000 abstract description 7
- 230000018044 dehydration Effects 0.000 abstract description 5
- 238000006297 dehydration reaction Methods 0.000 abstract description 5
- 230000005484 gravity Effects 0.000 abstract description 5
- 238000001914 filtration Methods 0.000 abstract description 3
- 238000001179 sorption measurement Methods 0.000 abstract description 3
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 abstract description 2
- 230000009286 beneficial effect Effects 0.000 abstract description 2
- 239000000243 solution Substances 0.000 description 9
- 238000000034 method Methods 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- 238000003491 array Methods 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 230000009471 action Effects 0.000 description 3
- 239000012267 brine Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 3
- 238000004065 wastewater treatment Methods 0.000 description 3
- 238000010923 batch production Methods 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000010924 continuous production Methods 0.000 description 2
- 229920002635 polyurethane Polymers 0.000 description 2
- 239000004814 polyurethane Substances 0.000 description 2
- BITYAPCSNKJESK-UHFFFAOYSA-N potassiosodium Chemical compound [Na].[K] BITYAPCSNKJESK-UHFFFAOYSA-N 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 238000006467 substitution reaction Methods 0.000 description 2
- IAYPIBMASNFSPL-UHFFFAOYSA-N Ethylene oxide Chemical compound C1CO1 IAYPIBMASNFSPL-UHFFFAOYSA-N 0.000 description 1
- GOOHAUXETOMSMM-UHFFFAOYSA-N Propylene oxide Chemical compound CC1CO1 GOOHAUXETOMSMM-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000003999 initiator Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229910021645 metal ion Inorganic materials 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007151 ring opening polymerisation reaction Methods 0.000 description 1
Landscapes
- Polyethers (AREA)
Abstract
The utility model relates to a refining device of polyether polyol, in particular to a potassium and sodium ion removing device of high-activity high-molecular-weight polyether, which comprises the following components: the high-activity high-molecular polyether polyol produced by the neutralization kettle is pumped into the neutralization kettle from a material inlet arranged in the middle of the desalination tower by the metering pump, a polyether overflow outlet is arranged at the top end of the desalination tower, a polyether clean-out opening is arranged at the middle lower part of the desalination tower, a salt solution discharge outlet is arranged at the bottom end of the desalination tower, the polyether overflow outlet and the polyether clean-out opening are connected with the flash kettle through pipelines, and the bottom end of the flash kettle is connected with the finished product storage tank through pipelines. The beneficial effects are that: the desalting tower adopts gravity layering to replace long-time vacuum dehydration, so that the energy loss is reduced; in addition, silicate is not needed to participate in adsorption treatment and filtration, so that material loss caused by filter residues and consumption of filter residue treatment are avoided.
Description
Technical Field
The utility model relates to a refining device of polyether polyol, in particular to a potassium and sodium ion removing device of high-activity high-molecular-weight polyether.
Background
Polyurethane materials have wide application in the fields of automobiles, building materials, furniture and the like, and polyether polyol is also increasingly valued as an important raw material of polyurethane.
The traditional polyether polyol is synthesized by using micromolecular polyol or amine as an initiator, catalyzing propylene oxide or ethylene oxide to carry out ring-opening polymerization by using an alkali metal catalyst to form a macromolecular polymer, wherein the polymerized polyether polyol contains catalyst metal ions, unreacted monomers and oligomers, so that the impurities are removed by a refining process. The most widely used refining process is adsorption filtration treatment by adding acid for neutralization and then using adsorbent.
After the neutralization reaction of the polyether polyol in the neutralization tank, it is necessary to carry out vacuum dehydration for a long time, and it is also necessary to add polyether concentrates or other filter aids at the same time. The long-time vacuum dehydration brings about no small energy loss; the use of the refining agent and the filter aid also brings about material loss and filter residue treatment consumption, so that the manufacturing cost of the polyether is higher.
Disclosure of Invention
Aiming at the defects of the prior art, the utility model provides a potassium and sodium ion removing device for high-activity high-molecular-weight polyether, which solves the problem of higher cost of a water removing process of polyether polyol.
In order to achieve the above purpose, the present utility model provides the following technical solutions: a potassium and sodium ion removal device for a high activity high molecular weight polyether comprising: the high-activity high-molecular polyether polyol produced by the neutralization kettle is pumped into the neutralization kettle from a material inlet arranged in the middle of the desalination tower by the metering pump, a polyether overflow outlet is arranged at the top end of the desalination tower, a polyether clean-out opening is arranged at the middle lower part of the desalination tower, a salt solution discharge outlet is arranged at the bottom end of the desalination tower, the polyether overflow outlet and the polyether clean-out opening are connected with the flash kettle through pipelines, and the bottom end of the flash kettle is connected with the finished product storage tank through pipelines.
Further, the desalination tower is of a hollow tower structure with different diameters from top to bottom, the upper part of the desalination tower is a large-diameter section, the lower part of the desalination tower is a small-diameter section, and an excessive section is arranged between the large-diameter section and the small-diameter section.
Further, the height of the small diameter section is 20% -35% of the total height of the desalting tower.
Further, the height of the large diameter section is 50% -70% of the total height of the desalting tower.
Further, the height of the transition section is 5% -20% of the total height of the desalination tower.
Further, the diameter ratio of the large diameter section to the small diameter section is 2-4:1.
Further, the distance between the position of the material inlet and the bottom end of the desalting tower is 35% -50% of the height of the desalting tower, and the distance between the position of the polyether clean-out port and the bottom end of the desalting tower is 30% -45% of the height of the desalting tower.
Further, a plurality of tubes are arranged in the desalting tower.
Further, the tube array is U-shaped, and two ends of the upper part of the tube array are fixedly connected with the desalting towers respectively.
Further, the bottom ends of the tubes are lower than the material inlet of the desalting tower and higher than the small-diameter section.
Compared with the prior art, the utility model has the following beneficial effects: the desalting tower adopts gravity layering to replace long-time vacuum dehydration, so that the energy loss is reduced; in addition, silicate is not needed to participate in adsorption treatment and filtration, so that material loss caused by filter residues and consumption of filter residue treatment are avoided.
Drawings
FIG. 1 is a flow chart of the operation of the present utility model;
FIG. 2 is a schematic structural view of a desalination tower of the present utility model;
FIG. 3 is a cross-sectional view of a desalination column of the utility model.
In the figure: 1. a neutralization kettle; 2. a metering pump; 3. a desalination tower; 31. a large diameter section; 32. a small diameter section; 33. a transition section; 4. a flash evaporation kettle; 5. a finished product storage tank; 6. a material inlet; 7. a polyether overflow port; 8. polyether discharging port; 9. a salt solution discharge port; 10. and (5) arranging a tube.
Detailed Description
In order to make the objects, technical solutions and advantages of the present utility model more apparent, the present utility model will be clearly and completely described in connection with the following specific embodiments.
A potassium and sodium ion removal device for a high activity high molecular weight polyether comprising: the high-activity high-molecular-weight polyether polyol produced by the neutralization kettle 1 is pumped into the neutralization kettle 1 by the metering pump 2 from a material inlet 6 arranged in the middle of the desalination tower 3, the distance between the position of the material inlet 6 and the bottom end of the desalination tower 3 is 35% -50% of the height of the desalination tower 3, polyether and potassium sodium salt solution are spontaneously layered under the action of gravity, the potassium sodium salt solution leaves the desalination tower 3 from the bottom to enter a crystallizer at a flow rate of 3% -10% of the total material mass flow entering the desalination tower 3, polyether overflows from the top to enter the flash evaporation kettle 4 and finally enters the finished product storage tank 5 for storage.
The desalting tower 3 utilizes the density difference between polyether and potassium nano-salt water to separate the two solutions spontaneously, so that the polyether solution in the mixed solution is extracted, and compared with the existing vacuum dehydration process, the energy consumption is reduced.
The desalination tower 3 is a hollow tower structure with different diameters from top to bottom, the upper part of the desalination tower 3 is a large-diameter section 31, the lower part of the desalination tower 3 is a small-diameter section 32, and an excessive section 33 is arranged between the large-diameter section 31 and the small-diameter section 32.
The height of the small diameter section 32 is 20% -35% of the total height of the desalination tower 3.
The height of the large diameter section 31 is 50% -70% of the total height of the desalination tower 3.
The height of the transition section 33 is 5% to 20% of the total height of the desalination tower 3.
The diameter ratio of the large diameter section 31 to the small diameter section 32 is 2-4:1.
The top of the desalination tower 3 is provided with a polyether overflow port 7, the middle lower part of the desalination tower 3 is provided with a polyether clean-out port 8, the distance between the position of the polyether clean-out port 8 and the bottom end of the desalination tower 3 is 30% -45% of the height of the desalination tower 3, the bottom end of the desalination tower 3 is provided with a salt solution discharge port 9, the polyether overflow port 7 and the polyether clean-out port 8 are connected with a flash evaporation kettle 4 through pipelines, and the bottom end of the flash evaporation kettle 4 is connected with a finished product storage tank 5 through pipelines.
The inside of the desalting tower 3 is provided with a plurality of U-shaped tube arrays 10, two ends of the upper part of the U-shaped tube arrays 10 are respectively welded with the desalting tower 3, the bottom ends of the tube arrays 10 are lower than a material inlet 6 of the desalting tower 3 and higher than a small-diameter section 32, and a heating medium is introduced into the tube arrays 10, so that the inside of the desalting tower 3 can be heated or insulated, and the temperature in the desalting tower 3 is suitable for the desalting reaction of the high-molecular-weight polyether polyol with high activity.
Example 1
A batch process polyether refining process.
After the neutralization of the raw materials in the neutralization kettle 1 is finished, high-activity high-molecular-weight polyether polyol is produced, and the salt water content is 5.8%; to accommodate the brine content of the solution and to ensure desalination efficiency, the diameter of the large diameter section 31 of the desalination tower 3 is 2m, the diameter of the small diameter section 32 is 0.5m, the height of the desalination tower 3 is 15m, the height of the large diameter section 31 is 60% (9 m) of the height of the desalination tower 3, the height of the small diameter section 32 is 30% (4.5 m) of the height of the desalination tower 3, and the height of the transition section 33 is 10% (1.5 m) of the height of the desalination tower 3.
The distance between the polyether material inlet 6 and the bottom end of the desalting tower 3 is 40% of the total tower height, and the distance between the polyether clean-up opening 8 and the bottom end of the desalting tower 3 is 30% of the total tower height; the internal temperature of the desalting tower 3 is kept between 120 and 130 ℃ by a tube array 10.
After the temperature of the neutralized high-activity high-molecular-weight polyether polyol is raised to 120 ℃, the neutralized high-activity high-molecular-weight polyether polyol is sent into a desalting tower 3 by a metering pump 2, and the flow is 65t/h; the total material flow rate into the desalting column 3 is 65 t/h/2 m 2 ×3.14÷4）=20.7t/m 2 /h, flow rate of 20.7t/m 2 /h÷（1t/m 3 ) =20.7m/h (the density of the high activity high molecular weight polyether polyol liquid formed after polyether neutralization was 1t/m 3 Meter), the residence time of the material in the desalination column 3 was 15 m/20.7 m/h=0.725 h=43.5 min.
After entering the desalting tower 3, polyether and salt solution are automatically layered under the action of gravity, polyether leaves the desalting tower 3 from a polyether overflow port 7 at the top, and enters a finished product storage tank 5 after further subsequent treatment; the salt solution leaves the desalination tower 3 from the bottom salt solution outlet 9 and enters the wastewater treatment link.
After the materials in the neutralization kettle 1 are completely transferred, closing a valve of a salt solution outlet 9, standing for 30 minutes, opening a valve of a polyether discharging port 8, discharging upper polyether, and closing the valve of the polyether discharging port 8; and opening a valve of the salt solution outlet 9, discharging the residual materials in the desalting tower 3, and closing the valve of the salt solution outlet 9. To this end, the purification of the high molecular weight high activity polyether of the single batch is completed.
The total material has less salt and water, when the solution in the desalting tower 3 is desalted, the dividing line of polyether and salt solution is lower than the polyether discharging opening 8, so that after the material in the neutralization kettle 1 is transported into the desalting tower 3 and is kept stand for 30 minutes, the polyether is discharged from the polyether discharging opening 8, the salt solution and a part of polyether are discharged from the salt solution discharging opening 9, and the polyether discharged together with the salt solution is separated by the wastewater treatment ring and is sent into the neutralization kettle 1 for recycling.
Example 2
A continuous polyether refining process.
After the neutralization of the raw materials in the neutralization kettle 1 is finished, high-activity high-molecular-weight polyether polyol is produced, and the brine content is 6.4%; to accommodate the brine content of the solution and to ensure desalination efficiency, the desalination tower 3 has a large diameter section 31 with a diameter of 1.5m, a small diameter section 32 with a diameter of 0.5m, a tower height of 20m, a large diameter section 31 with a height of 70% (10.5 m) of the desalination tower 3, a small diameter section 32 with a height of 20% (3 m) of the desalination tower 3, and a transition section 33 with a height of 10% (1.5 m) of the desalination tower 3.
The distance between the polyether material inlet 6 and the bottom end of the desalting tower 3 is 40% of the height of the desalting tower 3, and the distance between the polyether clean-out port 8 and the bottom end of the desalting tower 3 is 30% of the total tower height; the internal temperature of the desalination tower 3 is kept between 130 and 140 ℃ by the tube array 10.
After the temperature of the neutralized polyether is raised to 125 ℃, the neutralized polyether is sent into a desalting tower 3 by a metering pump 2, and the flow is 50t/h; the total material flow rate into the desalting column 3 was 50 t/h/((1.5 m)） 2 ×3.14÷4）=28.4t/m 2 /h, flow rate of 28.4t/m 2 /h÷（1t/m 3 ) The residence time of the material in the whole column was 20 m/h (28.4 m/h) =0.7h=42 min.
After entering the desalting tower 3, polyether and salt solution are automatically layered under the action of gravity, polyether leaves the desalting tower 3 from a polyether overflow port 7 at the top, and enters a finished product storage tank 5 after further subsequent treatment; the salt solution leaves the desalination tower 3 from the bottom salt solution outlet 9 and enters the wastewater treatment link.
In general, the continuous process does not need to be suspended, and the continuous process is operated according to the batch process when equipment is stopped and overhauled.
Although the utility model has been described in detail with reference to the foregoing embodiments, those skilled in the art may modify the technical solutions described in the foregoing embodiments or make equivalent substitutions for some technical features thereof; such modifications and substitutions do not depart from the spirit and scope of the technical solutions of the embodiments of the present utility model.
Claims (10)
1. A potassium and sodium ion removing device for high-activity high-molecular-weight polyether, comprising: neutralization cauldron (1), measuring pump (2), desalination tower (3), flash distillation cauldron (4), finished product storage tank (5), high activity high molecular weight polyether polyol that neutralization cauldron (1) produced is followed to measuring pump (2) material import (6) pump wherein that the middle part of desalination tower (3) was equipped with, the top of desalination tower (3) is equipped with polyether overflow mouth (7), the well lower part of desalination tower (3) is equipped with polyether and puts clean mouth (8), the bottom of desalination tower (3) is equipped with salt solution discharge port (9), polyether overflow mouth (7) with polyether is put clean mouth (8) all through the pipeline with flash distillation cauldron (4) are connected, flash distillation cauldron (4) bottom pass through the pipeline with finished product storage tank (5) are connected.
2. The potassium and sodium ion removing device for high-activity high-molecular-weight polyether according to claim 1, wherein the desalting tower (3) is of a hollow tower structure with different diameters from top to bottom, the upper part of the desalting tower (3) is a large-diameter section (31), the lower part of the desalting tower (3) is a small-diameter section (32), and an excessive section (33) is arranged between the large-diameter section (31) and the small-diameter section (32).
3. The potassium and sodium ion removing apparatus of a high activity high molecular weight polyether according to claim 2, wherein the height of said small diameter section (32) is 20% to 35% of the total height of said desalting tower (3).
4. The potassium and sodium ion removing apparatus of high activity high molecular weight polyether as claimed in claim 2, wherein the height of said large diameter section (31) is 50 to 70% of the total height of said desalting tower (3).
5. The potassium and sodium ion removing apparatus of a high activity high molecular weight polyether according to claim 2, wherein the height of the transition section (33) is 5% to 20% of the total height of the desalting tower (3).
6. The potassium and sodium ion removing apparatus of a high activity high molecular weight polyether according to claim 2, wherein a diameter ratio of said large diameter section (31) to said small diameter section (32) is 2 to 4:1.
7. The potassium and sodium ion removing device for high-activity high-molecular-weight polyether according to claim 1, wherein the distance between the material inlet (6) and the bottom end of the desalting tower (3) is 35% -50% of the height of the desalting tower (3), and the distance between the polyether discharging opening (8) and the bottom end of the desalting tower (3) is 30% -45% of the height of the desalting tower (3).
8. The potassium and sodium ion removing device for high-activity high-molecular weight polyether according to claim 2, wherein a plurality of tubes (10) are arranged inside the desalting tower (3).
9. The potassium and sodium ion removing device for high-activity high-molecular weight polyether according to claim 8, wherein the tube array (10) is U-shaped, and two ends of the upper part of the tube array are fixedly connected with the desalting tower (3).
10. The potassium and sodium ion removing apparatus of a high activity high molecular weight polyether according to claim 9, wherein the bottom end of said tube array (10) is lower than the material inlet (6) of said desalting column (3) and higher than said small diameter section (32).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321616120.5U CN220091424U (en) | 2023-06-25 | 2023-06-25 | Potassium and sodium ion removing device for high-activity high-molecular-weight polyether |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321616120.5U CN220091424U (en) | 2023-06-25 | 2023-06-25 | Potassium and sodium ion removing device for high-activity high-molecular-weight polyether |
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| Publication Number | Publication Date |
|---|---|
| CN220091424U true CN220091424U (en) | 2023-11-28 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321616120.5U Active CN220091424U (en) | 2023-06-25 | 2023-06-25 | Potassium and sodium ion removing device for high-activity high-molecular-weight polyether |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220091424U (en) |
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2023
- 2023-06-25 CN CN202321616120.5U patent/CN220091424U/en active Active
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