CN220159241U - System for serialization preparation sodium methoxide - Google Patents
System for serialization preparation sodium methoxide Download PDFInfo
- Publication number
- CN220159241U CN220159241U CN202321638642.5U CN202321638642U CN220159241U CN 220159241 U CN220159241 U CN 220159241U CN 202321638642 U CN202321638642 U CN 202321638642U CN 220159241 U CN220159241 U CN 220159241U
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- CN
- China
- Prior art keywords
- sodium methoxide
- tower
- rectifying tower
- compressor
- membrane
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- WQDUMFSSJAZKTM-UHFFFAOYSA-N Sodium methoxide Chemical compound [Na+].[O-]C WQDUMFSSJAZKTM-UHFFFAOYSA-N 0.000 title claims abstract description 68
- 238000002360 preparation method Methods 0.000 title description 4
- 239000012528 membrane Substances 0.000 claims abstract description 45
- 238000006243 chemical reaction Methods 0.000 claims abstract description 44
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 21
- 238000003860 storage Methods 0.000 claims abstract description 10
- 239000012466 permeate Substances 0.000 claims abstract description 5
- 239000012465 retentate Substances 0.000 claims abstract description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 abstract description 89
- 238000005516 engineering process Methods 0.000 abstract description 12
- 238000009833 condensation Methods 0.000 abstract description 8
- 230000005494 condensation Effects 0.000 abstract description 8
- 238000005373 pervaporation Methods 0.000 abstract description 8
- 238000005265 energy consumption Methods 0.000 abstract description 7
- 238000009834 vaporization Methods 0.000 abstract description 7
- 230000008016 vaporization Effects 0.000 abstract description 7
- 230000006835 compression Effects 0.000 abstract description 5
- 238000007906 compression Methods 0.000 abstract description 5
- 230000018044 dehydration Effects 0.000 abstract description 5
- 238000006297 dehydration reaction Methods 0.000 abstract description 5
- 238000011084 recovery Methods 0.000 abstract description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 10
- 239000002994 raw material Substances 0.000 description 9
- 239000007788 liquid Substances 0.000 description 7
- 238000000034 method Methods 0.000 description 7
- 238000000066 reactive distillation Methods 0.000 description 6
- 239000000463 material Substances 0.000 description 5
- 239000012071 phase Substances 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- 239000003513 alkali Substances 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 239000007792 gaseous phase Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 2
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 description 2
- 239000011259 mixed solution Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 1
- 239000013043 chemical agent Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- SUBJHSREKVAVAR-UHFFFAOYSA-N sodium;methanol;methanolate Chemical compound [Na+].OC.[O-]C SUBJHSREKVAVAR-UHFFFAOYSA-N 0.000 description 1
- 230000002269 spontaneous effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a system for continuously preparing sodium methoxide, which comprises a reaction rectifying tower, a heater, a membrane assembly unit, a compressor, a condenser and a water storage tank, wherein the reaction rectifying tower is connected with the heater; the reaction rectifying tower is provided with a feed inlet, a tower top discharge port and a tower bottom discharge port, a reboiler is arranged at the bottom of the reaction rectifying tower, and the tower top discharge port is sequentially connected with a heater and a membrane assembly unit through pipelines; the permeate side outlet of the membrane module unit is connected with the compressor through a pipeline, the compressor is connected with the feed inlet through a pipeline, and the retentate side outlet of the membrane module unit is sequentially connected with the condenser and the water storage tank through pipelines. The utility model combines the continuous reaction rectification technology, the pervaporation membrane dehydration technology and the compression technology, avoids repeated condensation and vaporization of methanol, can effectively reduce the energy consumption of system operation, and further effectively reduces the recovery cost.
Description
Technical Field
The utility model belongs to the technical field of compound preparation, and particularly relates to a system for continuously preparing sodium methoxide.
Background
Sodium methoxide is a dangerous chemical, has corrosiveness and spontaneous combustion, and is mainly used as a condensing agent, a chemical agent and a catalyst for treating practical grease in the pharmaceutical industry and organic synthesis.
In the existing preparation of sodium methoxide, the separation of methanol and water is realized by a rectification mode of the water-containing methanol distilled from the top of the reaction rectifying tower, the gas-phase water-containing methanol at the top of the reaction rectifying tower is required to be totally condensed, the water-containing methanol solution after complete condensation is dehydrated by the rectifying tower, and the dehydrated methanol is heated and vaporized into methanol steam to be returned to the reaction rectifying tower for reaction. In the whole dehydration process of the aqueous methanol, the condensation and vaporization of the gaseous phase of the methanol are involved for a plurality of times, and the vaporization latent heat of the methanol is larger, so that the circulating water consumed in the condensation process of the gaseous methanol and the steam consumed in the vaporization process of the liquid methanol are larger, and the energy consumption in the whole process of preparing the sodium methoxide is extremely large.
Based on the above factors, a new sodium methoxide production system is needed to realize continuous energy-saving production of sodium methoxide.
Disclosure of Invention
In order to solve the technical problems, the utility model provides a system for continuously preparing sodium methoxide, which adopts the following technical scheme:
a system for continuously preparing sodium methoxide comprises a reaction rectifying tower, a heater, a membrane assembly unit, a compressor, a condenser and a water storage tank; the reaction rectifying tower is provided with a feed inlet, a tower top discharge port and a tower bottom discharge port, a reboiler is arranged at the tower bottom of the reaction rectifying tower, and the tower top discharge port is sequentially connected with the heater and the membrane assembly unit through pipelines; the permeate side outlet of the membrane module unit is connected with the compressor through a pipeline, the compressor is connected with the feed inlet through a pipeline, and the retentate side outlet of the membrane module unit is sequentially connected with the condenser and the water storage tank through pipelines.
The technical characteristics of the scheme are adopted, and the scheme has the following technical effects:
according to the technical scheme, the continuous reaction rectification technology, the pervaporation membrane dehydration technology and the compression technology are combined, raw materials react in the reaction rectification tower to generate sodium methoxide and water, gaseous phase water-containing methanol distilled out of the reaction rectification tower further enters the pervaporation membrane of the membrane assembly unit to be dehydrated after passing through the heater in a gaseous state, the dehydrated methanol is still in a gaseous state, and the dehydrated methanol is directly returned to the reaction system after being compressed by the compressor, so that repeated condensation and vaporization of the methanol are avoided, the energy consumption of system operation can be effectively reduced, and the recovery cost is further effectively reduced.
Further, the feed inlet comprises an upper feed inlet and a lower feed inlet.
The raw material of the first alkali liquor for preparing the sodium methoxide can continuously enter from the upper feed inlet of the reaction rectifying tower, and the raw material of the methanol can continuously enter from the lower feed inlet of the reaction rectifying tower, so that the raw material reacts in the reaction rectifying tower, and the first alkali liquor is a mixed solution of methanol and sodium hydroxide.
Further, the reactive distillation column is a plate column, and the number of the plates is 25-55.
Further, the upper feed inlet is positioned at any one of the 5 th to 25 th tower plates, and the lower feed inlet is positioned at any one of the 35 th to 55 th tower plates.
Further, the reactive distillation column is provided with a feed back opening, and the feed back opening is positioned at any column plate from 10 th to 35 th.
The raw materials react in the reactive distillation column, the bottom liquid of the reactive distillation column is sodium methoxide solution containing methanol, a part of the bottom liquid is extracted as a qualified product, and a part of the bottom liquid returns to a reaction section in the reactive distillation column through the feed back opening for re-reaction.
Further, the membrane module unit comprises at least two membrane modules connected in series.
Further, the membrane module unit comprises 5-20 membrane modules connected in series, namely, the series number is 5-20.
Further, the system for continuously preparing sodium methoxide also comprises a material transferring pump which is used for extracting a part of qualified products from the bottom liquid of the reaction rectifying tower.
Further, the operating pressure of the reaction rectifying tower of the system for continuously preparing sodium methoxide is 0.1-0.25 MPaG; the ratio of the tower bottom extract returned to the reactive distillation tower is 0.1-0.9; the feeding temperature of the raw material A alkali liquor is 15-55 ℃, the temperature of the top of the reactive rectifying tower is 65-110 ℃, and the temperature of the bottom of the reactive rectifying tower is 70-125 ℃; the operation pressure of the pervaporation membrane of the membrane component is 0.1-0.25 MPaG, and the side pressure of permeation is-0.095 to-0.1 MPaG; the inlet pressure of the compressor is normal pressure-0.1 MPaG, and the outlet side pressure of the compressor is 0.15-0.3 MPaG; the inlet temperature of the compressor is 65-80 ℃, and the outlet temperature of the compressor is 95-110 ℃.
The utility model provides a system for continuously preparing sodium methoxide, which combines a continuous reaction rectification technology, a pervaporation membrane dehydration technology and a compression technology, wherein gaseous phase water-containing methanol distilled out of a reaction rectification tower directly enters a pervaporation membrane of a membrane assembly unit to be dehydrated after further passing through a heater in a gaseous state, the dehydrated methanol still is in a gaseous state, and the dehydrated methanol directly returns to a reaction system after being compressed by a compressor, so that multiple condensation and vaporization of the methanol are avoided, the energy consumption of the system operation can be effectively reduced, and the recovery cost is further effectively reduced.
Drawings
FIG. 1 is a schematic diagram of a system for continuously preparing sodium methoxide according to the present utility model.
The figure indicates:
1. a reactive rectifying tower; 2. a reboiler; 3. a heater; 4. a membrane module; 5. a compressor; 6. a condenser; 7. a water storage tank; 8. and a material transferring pump.
Detailed Description
The present utility model will be described in further detail with reference to the accompanying drawings for a better understanding of the objects, structures and functions of the present utility model.
Examples:
as shown in fig. 1, the system for continuously preparing sodium methoxide in this embodiment comprises a reactive rectifying tower 1, a heater 3, a membrane module unit, a compressor 5, a condenser 6 and a water storage tank 7; the membrane module unit comprises 8 membrane modules 4 connected in series, namely the series number is 8. The reaction rectifying tower 1 is provided with a feed inlet, a tower top discharge outlet, a tower bottom discharge outlet and a feed back opening, the reaction rectifying tower 1 is a plate rectifying tower, the number of plates is 50, the upper feed inlet is positioned at an 8 th plate, the lower feed inlet is positioned at a 40 th plate, the feed back opening is positioned at a 15 th plate, the reboiler 2 is installed at the tower bottom of the reaction rectifying tower 1, the feed inlet is sequentially connected with the heater 3 and the membrane assembly unit through pipelines, a permeate side outlet of the membrane assembly unit is connected with the compressor 5 through pipelines, the compressor 5 is connected with the feed inlet through pipelines, and a retentate side outlet of the membrane assembly unit is sequentially connected with the condenser 6 and the water storage tank 7 through pipelines.
When the method is used, the methyl lye raw material for preparing the sodium methoxide can continuously enter from the upper feed inlet of the reaction rectifying tower 1, the methyl lye is a mixed solution of methanol and sodium hydroxide, the methanol raw material can continuously enter from the lower feed inlet of the reaction rectifying tower 1, and the raw material reacts in the reaction rectifying tower 1 to generate sodium methoxide and water. The method comprises the steps that excessive methanol and water generated by the reaction are distilled out from the top of a reactive rectifying tower 1 in a gas phase mixture mode, are heated by a heater and continuously enter a membrane assembly 4 connected in series, moisture and a small amount of methanol in the gas phase mixture permeate to a membrane permeation side from the membrane upstream side of the membrane assembly 4, water-free methanol is obtained from the membrane assembly 4 at the last stage, the partial gas phase methanol enters a compressor 5 for compression and pressure boosting, and the boosted gas phase methanol enters a lower feed inlet of the reactive rectifying tower 1 again and participates in the reaction again; the water in the membrane component 4 and a small amount of methanol enter the condenser 6 through the outlet on the seepage side under the suction of a vacuum unit, and are collected in the water storage tank 7 after condensation. The bottom of the reaction rectifying tower 1 is sodium methoxide solution containing methanol, namely sodium methoxide-methanol solution, a part of the bottom liquid of the part of the tower is taken as a qualified product and is extracted by a material transfer pump 8, and a part of the bottom liquid of the part of the tower returns to a reaction section in the reaction rectifying tower 1 through a material return port for re-reaction.
Wherein, the operating pressure of the reactive rectifying tower 1 of the system for continuously preparing sodium methoxide is 0.1-0.25 MPaG; the ratio of the tower bottom extract of the reaction rectifying tower 1 to return to the reaction rectifying tower 1 is 0.1-0.9; the feeding temperature of the first alkali liquor is 15-55 ℃, the temperature of the top of the reactive rectifying tower 1 is 65-110 ℃, and the temperature of the bottom of the reactive rectifying tower is 70-125 ℃; the operation pressure of the pervaporation membrane of the membrane component 4 is 0.1-0.25 MPaG, and the side pressure of permeation is-0.095 to-0.1 MPaG; the inlet pressure of the compressor 5 is normal pressure-0.1 MPaG, and the outlet side pressure of the compressor 5 is 0.15-0.3 MPaG; the inlet temperature of the compressor 5 is 65-80 ℃, and the outlet temperature of the compressor 5 is 95-110 ℃.
The system for continuously preparing sodium methoxide only needs about 0.3 ton of steam per ton of 30wt% sodium methoxide solution, and the energy consumption of the production process of the system is about 10-12% of the energy consumption of the conventional process under the condition that the purity of the prepared product is completely consistent, the energy is saved by 85-90%, the energy saving effect is obvious, and the operation cost is low.
Therefore, the system for continuously preparing sodium methoxide combines the continuous reaction rectification technology, the pervaporation membrane dehydration technology and the compression technology, avoids repeated condensation and vaporization of methanol, can effectively reduce the energy consumption of system operation, and further effectively reduces the recovery cost.
It will be understood that the utility model has been described in terms of several embodiments, and that various changes and equivalents may be made to these features and embodiments by those skilled in the art without departing from the spirit and scope of the utility model. In addition, many modifications may be made to adapt a particular situation or material to the teachings of the utility model without departing from the essential scope thereof. Therefore, it is intended that the utility model not be limited to the particular embodiment disclosed, but that the utility model will include all embodiments falling within the scope of the appended claims.
Claims (8)
1. The system for continuously preparing the sodium methoxide is characterized by comprising a reaction rectifying tower, a heater, a membrane assembly unit, a compressor, a condenser and a water storage tank; the reaction rectifying tower is provided with a feed inlet, a tower top discharge port and a tower bottom discharge port, a reboiler is arranged at the tower bottom of the reaction rectifying tower, and the tower top discharge port is sequentially connected with the heater and the membrane assembly unit through pipelines; the permeate side outlet of the membrane module unit is connected with the compressor through a pipeline, the compressor is connected with the feed inlet through a pipeline, and the retentate side outlet of the membrane module unit is sequentially connected with the condenser and the water storage tank through pipelines.
2. The system for continuously preparing sodium methoxide of claim 1, wherein the feed inlet comprises an upper feed inlet and a lower feed inlet.
3. The system for continuously preparing sodium methoxide according to claim 2, wherein the reactive rectifying tower is a plate tower, and the number of plates is 25-55.
4. A system for continuously preparing sodium methoxide according to claim 3, wherein the upper inlet is located at any of the 5 th to 25 th trays and the lower inlet is located at any of the 35 th to 55 th trays.
5. A system for continuously preparing sodium methoxide according to claim 3, wherein the reactive rectifying tower is provided with a feed back opening, and the feed back opening is positioned at any tray of 10 th to 35 th.
6. The system for continuously producing sodium methoxide according to claim 1, wherein the membrane module unit comprises at least two membrane modules connected in series.
7. The system for continuously preparing sodium methoxide according to claim 6, wherein the membrane module unit comprises 5 to 20 membrane modules connected in series.
8. The system for continuously preparing sodium methoxide as claimed in claim 1, further comprising a transfer pump.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321638642.5U CN220159241U (en) | 2023-06-27 | 2023-06-27 | System for serialization preparation sodium methoxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321638642.5U CN220159241U (en) | 2023-06-27 | 2023-06-27 | System for serialization preparation sodium methoxide |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220159241U true CN220159241U (en) | 2023-12-12 |
Family
ID=89062556
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321638642.5U Active CN220159241U (en) | 2023-06-27 | 2023-06-27 | System for serialization preparation sodium methoxide |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220159241U (en) |
-
2023
- 2023-06-27 CN CN202321638642.5U patent/CN220159241U/en active Active
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