CN114307214A - Rectification recovery device and method for rectifying and recovering acetone in acetone aqueous solution - Google Patents
Rectification recovery device and method for rectifying and recovering acetone in acetone aqueous solution Download PDFInfo
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Abstract
The invention provides a rectification recovery device and a method for rectifying and recovering acetone in an acetone aqueous solution, wherein the rectification recovery device comprises a rectification tower, a gas-liquid distributor, a reflux tank and a condensation cooler; the rectifying tower comprises a tower top, a tower kettle and a packing layer, the packing layer is positioned between the tower top and the tower kettle, the condensing cooler is communicated with the tower top and a reflux tank, and the reflux tank is communicated with the rectifying tower through a reflux pump; the height of the filler layer is 5.5 m-6 m, the filler layer comprises three sections of filler sections, the height of the first section of filler section is 1.0 m-1.25 m, the height of the second section of filler section is 1.0 m-1.25 m, and the height of the third section of filler section is 3.0 m-3.5 m; by adopting the structure, the liquid is collected and redistributed in sections, so that the gas-liquid mass and heat transfer can be enhanced, the impact of gas on internal parts of the tower can be reduced, and the energy consumption can be reduced by 10-20%, and the maintenance frequency of the equipment can be reduced.
Description
Technical Field
The invention relates to the field of chemical separation and recovery, in particular to a rectification recovery device and a method for rectifying and recovering acetone in an acetone aqueous solution.
Background
In recent years, with the vigorous development of fine chemical industry, petrochemical industry, chemical fertilizer and other industries, the research work of various novel tower fillers has attracted the attention of professionals. The structured packing has the advantages of large specific surface area, regular structure, high porosity, high flow rate, low pressure drop, high operation elasticity and the like, and is concerned.
Rectification is an energy-consuming large household in a chemical operation unit, the infrastructure cost is high, a large amount of energy is consumed, and simultaneously, a large amount of greenhouse gases such as carbon dioxide are indirectly emitted, so that the rectification process has important significance in energy conservation. How to reduce energy consumption, save cost and reduce environmental pollution by improving the separation efficiency is an urgent problem to be solved.
In the production process of the acetate fiber tows, the recovery of acetone is mainly completed through an activated carbon adsorption process or a water absorption process, in both processes, an acetone-water mixed solution is formed, and then the acetone is recovered through the operation of a rectification unit. At present, a rectifying tower used for separating the acetone-water solution in the industry adopts a traditional plate tower, and plate tower internals such as a float valve and the like are used in the traditional plate tower; however, the operating pressure and temperature of the plate rectifier are relatively high, so that the cooling medium required at the top of the column to achieve the desired temperature is increased, and likewise, the heating steam required to achieve the same separation requirement is increased, thereby increasing the operating cost of the process. If improper operation causes the airflow in the tower to be suddenly small, the airflow strongly impacts internal parts of the tower, such as tower plates, float valves and the like, the internal parts of the tower are damaged, such as collapse of the tower tray, falling of the float valves and the like, the operation of the rectifying tower is unstable, and regular maintenance is needed. Meanwhile, after acetone circulates in the system for a long time, chemical reaction can occur to generate impurities, the impurities are discharged irregularly, the quality of the circulating acetone in the system is reduced, and the production of acetate fiber tows is seriously influenced.
Disclosure of Invention
The first purpose of the invention is to provide an energy-saving rectification recovery device.
The second purpose of the invention is to provide a method for recovering acetone in the acetone aqueous solution by rectification by utilizing the rectification recovery device.
In order to achieve the first purpose, the rectification recovery device provided by the invention comprises a rectification tower, a plurality of gas-liquid distributors, a reflux tank and a condensation cooler, wherein the rectification tower comprises a tower top, a tower kettle and a packing layer, the packing layer is positioned between the tower top and the tower kettle, the condensation cooler is communicated with the tower top through a first delivery pipe, the condensation cooler is communicated with the reflux tank through a discharge pipe, the reflux tank is communicated with the tower top of a discharge hole through a reflux pipe, and the tower kettle is connected with a gas inlet pipe; the height of the filler layer is 5.5 m-6 m, the filler layer comprises a first section of filler section, a second section of filler section and a third section of filler section, and fillers are respectively arranged in the first section of filler section, the second section of filler section and the third section of filler section; along the height direction of the rectifying tower, from top to bottom, a first section of packing section, a second section of packing section and a third section of packing section are sequentially arranged, and gas-liquid distributors are respectively arranged between the first section of packing section and the second section of packing section and between the second section of packing section and the third section of packing section; the height of the first section of the filling section is 1.0-1.25 m, the height of the second section of the filling section is 1.0-1.25 m, and the height of the third section of the filling section is 3.0-3.5 m; a feed inlet is also arranged between the second section of the packing section and the third section of the packing section.
According to the scheme, the regular packing is adopted to replace the original plate-type tower internal parts, so that the advantages of high flux and low pressure drop of the regular packing are fully exerted; in the process of rectification separation, the packing is treated in a segmented manner, a gas-liquid distributor is arranged between every two adjacent packing segments along the height direction of a rectification tower, so that the middle collection and redistribution of liquid phases are realized, the full contact of gas and liquid phases is facilitated, particularly, the liquid phase part is collected and redistributed in a segmented manner, the enhanced mass transfer and heat transfer are facilitated, the occurrence of mass transfer circuit breaking phenomena such as wall flow and the like is avoided, and the energy consumption is reduced by 10-20%; and because the packing is integral and stable, the permeability of the rectifying tower during the operation is high, all processes are continuous and stable, the frequency of equipment maintenance is greatly reduced, and the service life of the equipment is prolonged.
The further scheme is that a side-draw device is respectively connected to a gas-liquid distributor between the first section of the packing section and the second section of the packing section and a gas-liquid distributor between the second section of the packing section and the third section of the packing section, the side-draw device is connected with a chromatography tank, and the chromatography tank is communicated with a side-draw return pipe and a rectifying tower through a side-draw reflux pump.
Therefore, the side-draw technology is beneficial to discharging trace impurities from the tower body in time, the reflux ratio of the rectifying tower can be reduced by about 0.1 under the condition of achieving the same product quality index, and the steam consumption in the rectifying process is reduced.
The further scheme is that a feeding preheater is arranged at the feeding port and communicated with the feeding port through a feeding pipe.
Therefore, the acetone aqueous solution is preheated by the feed preheater before entering the rectifying tower, so that the heat of the high-temperature kettle liquid is recycled, and the efficiency is improved.
In a further embodiment, the filler is a Walsh Mellapak 500Y filler.
Therefore, the structured packing has the advantages of large specific surface area, small pressure drop, uniform fluid distribution, high mass and heat transfer efficiency and the like, and can obviously improve the gas-liquid contact condition under a certain filling height.
In order to achieve the second object, the present invention provides a method for recovering acetone from an acetone aqueous solution by distillation, which uses the distillation recovery device as described above to recover acetone from an acetone aqueous solution, and comprises: heating steam is introduced into the tower kettle through the air inlet pipe, acetone aqueous solution with the acetone mass concentration of 2% -30% is injected into the rectifying tower through the feeding hole and rectified, gas-phase materials at the top of the tower flow into the reflux tank after entering the condenser for condensation, part of distillates in the reflux tank are extracted as acetone products, and the rest distillates flow back into the rectifying tower, wherein the reflux ratio is 2.0-3.0.
The further scheme is that the temperature of the heating steam is 175-180 ℃, the heating steam enters the tower kettle under 0.15MPa, and the temperature of the tower kettle is controlled at 99-102 ℃.
Further, the operation pressure control of the tower topIs-220 mmH2O～10mmH2O。
The further proposal is that the temperature of the acetone aqueous solution at the feed inlet is controlled between 90 ℃ and 97 ℃.
The further proposal is that the side draw amount on the gas-liquid distributor between the first section of the packing section and the second section of the packing section and the gas-liquid distributor between the second section of the packing section and the third section of the packing section is controlled between 150kg/hr and 450 kg/hr.
According to the scheme, the method has the advantages that acetone in the acetone aqueous solution is recovered by using the rectifying tower with multiple sections of packing sections, and the pressure drop of the packed rectifying tower with the structure is reduced by 8 to 10 times and the energy consumption is reduced by 10 to 20 percent compared with that of the traditional plate-type rectifying tower on the premise of the same product purity and separation requirement by controlling all process coefficients.
Drawings
FIG. 1 is a schematic diagram of an embodiment of a rectification and recovery apparatus according to the present invention.
The invention is further explained with reference to the drawings and the embodiments.
Detailed Description
The rectification recovery device can be applied to an acetone recovery process in an acetone aqueous solution in the production process of acetate fiber tows, a plurality of sections of packing sections with different heights are arranged in a rectification tower, a gas-liquid distributor is arranged between adjacent packing sections, and the advantages of high flux and low pressure drop of regular packing are fully exerted by utilizing the packing sections with different heights; the gas-liquid distributor is arranged between every two adjacent filler sections, so that the collection and redistribution among liquid phases are realized, the full contact of gas and liquid phases is facilitated, particularly, the liquid phase part is collected and redistributed in a segmented manner, the mass transfer and heat transfer are facilitated to be enhanced, the occurrence of mass transfer disconnection phenomena such as wall flow and the like is avoided, and the energy consumption is reduced by 10-20%.
Referring to fig. 1, the rectification recovery device comprises a rectification tower 1, a gas-liquid distributor 3, a reflux tank 4, a reflux pump 5, a condensation cooler 6, a chromatography tank 7, a side reflux pump 8, a kettle liquid pump 9 and a feed preheater 10. The rectifying tower 1 comprises a tower top 11, a tower bottom 12 and a packing layer 13, wherein the packing layer 13 is positioned between the tower top 11 and the tower bottom 12. The condenser 6 communicates with the column top 11 via a first lead-out pipe 61, and the condensate cooler 6 communicates with the reflux drum 4 via a lead-out pipe 62. The reflux tank 4 is communicated with the discharge hole and the tower top 11 through a reflux pipe 41 and a reflux pump 5, and the specific work flow is as follows: the reflux tank 4 is connected with the reflux pump 5 through a first reflux pipe 41, the reflux pump 5 is communicated with a discharge hole of the rectifying tower 1 and the tower top 11 through a second reflux pipe 42, so that part of the distillate is conveniently extracted as an acetone product, and the rest of the distillate flows back into the rectifying tower 1.
The height of the packing layer 13 is 5.5 m-6 m, and the plurality of gas-liquid distributors 3 are respectively arranged in the packing layer 13. Packing layer 13 includes a first section of packing 131, a second section of packing 132, and a third section of packing 133.
The first section packing section 131, the second section packing section 132 and the third section packing section 133 are respectively provided with packing therein, the first section packing section 131, the second section packing section 132 and the third section packing section 133 are sequentially arranged from top to bottom along the height direction of the packed tower 1, a gas-liquid distributor 3 is arranged between the first section packing section 131 and the second section packing section 132, and a gas-liquid distributor 3 is arranged between the second section packing section 132 and the third section packing section 133. The height of the first section of the packing section 131 is 1.0m to 1.25m, the height of the second section of the packing section 132 is 1.0m to 1.25m, and the height of the third section of the packing section 133 is 3.0m to 3.5 m. In this embodiment, the packing is a Walsh Mellapak 500Y-type packing, and the heights of the first section packing section 131 and the second section packing section 132 are 1.25m and the third section packing section 133 is 3.5m, respectively.
The gas-liquid distributor 3 between the first section packing section 131 and the second section packing section 132, and the gas-liquid distributor 3 between the second section packing section 132 and the third section packing section 133 are respectively connected with a side-draw device, the side-draw device is connected with the chromatographic tank 7, and the chromatographic tank 7 is communicated with the rectifying tower 1 through a side-draw reflux pump 8 and a side-draw reflux pipe. The plurality of side-draw devices are connected with the chromatography tank 7 through the guide pipe 71, liquid drawn by the side-draw devices is layered in the chromatography tank 7, and impurities on the upper layer of the chromatography tank 7 are periodically discharged; the lower layer liquid of the chromatographic tank 7 flows to the side reflux pump 8 through the first side reflux pipe 72, and then the side reflux pump 8 conveys the liquid to the interior of the rectifying tower 1 through the second side reflux pipe 81. The side draw amount of the plurality of side draw devices is controlled to be 150 kg/hr-450 kg/hr.
The tower kettle 12 is connected with an air inlet pipe 121, and the air inlet pipe 121 is used for conveying heating steam with the temperature of 175-180 ℃ to the bottom of the rectifying tower 1 under 0.15 MPa. While the temperature in the tower kettle 12 is controlled at 99-102 ℃.
The autoclave liquid of the tower kettle 12 is communicated with the kettle liquid pump 9 through a second leading-out pipe 91, the kettle liquid pump 9 is connected with the feeding preheater 10 through a third leading-out pipe 92, and the autoclave liquid is discharged through the feeding preheater 10. A feed inlet 14 is also arranged between the second section packing section 132 and the third section packing section 133, the dilute acetone aqueous solution to be rectified passes through the feed preheater 10, and the feed preheater 10 is communicated with the feed inlet 14 through the feed pipe 101.
When a rectification recovery device is used for recovering acetone in an acetone aqueous solution, the acetone aqueous solution with the acetone mass concentration of 2-30% is preheated by a feed preheater 10 and then enters a rectification tower 1 from a feed port between a second section of packing section 13 and a third section of packing section 13; heating steam of 175-180 ℃ under 0.15MPa enters the bottom of the rectifying tower 1 through an air inlet pipe. The kettle high-temperature kettle liquid is pumped into the feeding preheater 2 through the kettle liquid pump 93 to exchange heat with the acetone-water solution, the temperature of the acetone-water solution at the feeding port is controlled to be 90-97 ℃, and the liquid at the feeding port is uniformly distributed through the gas-liquid distributor 3 between the second section filling section 132 and the third section filling section 133. The gas phase material at the tower top 11 enters a condensing cooler 6 to be condensed and then flows into a reflux tank 4, and the operation pressure of the tower top 11 is controlled to be 220mmH2O～10mmH2O; the purity of acetone distillate at the tower top 11 is controlled to be more than 99%, and the temperature is controlled to be 54-56 ℃; and part of distillate in the reflux tank 4 is extracted as an acetone product, and the rest of distillate flows back into the rectifying tower 1, wherein the reflux ratio is 2.0-3.0.
The invention will be better understood with reference to the following specific examples.
Example 1
The specific process for recovering the acetone by the rectification recovery device comprises the following steps: introducing dilute acetone with mass concentration of 10% (temperature of 96.5 deg.C, pressure of 0.15MPa, vaporization enthalpy r of 14356.2kJ/kg) into the rectification column at a feed flow rate of 45000kg/hA tower; introducing water vapor (at 178 ℃ and 0.15MPa) into the bottom of the rectifying tower from an air inlet pipeline, wherein the feeding amount is 2545 kg/h; in the rectification process, the operation pressure at the top of the tower is-30 mmH2O (G) and the operating pressure of the tower bottom is 2mmH2O (G); the product flow rate after condensation of the overhead condenser is 4497.4 kg/h; after the overhead distillate (the mass concentration of acetone is 99.1%) is cooled to 29 ℃ by a full condenser, part of the overhead distillate is collected as a product, and the other part of the overhead distillate is taken as reflux, wherein the reflux ratio is 2.36. The mass concentration of acetone in the column bottom stream was 1000 ppm.
Comparative example 1
The specific process of acetone recovery by adopting the existing plate-type rectifying tower is as follows: introducing dilute acetone with the mass concentration of 10% (the temperature is 96.5 ℃, the pressure is 0.15MPa, the vaporization enthalpy r is 14356.2kJ/kg) into a rectifying tower according to the feeding flow of 45000 kg/h; introducing water vapor (at 178 ℃ and 0.15MPa) into the bottom of the rectifying tower from an air inlet pipeline, wherein the feeding amount is 2956 kg/h; in the rectification process, the operation pressure at the top of the tower is-30 mmH2O (G) tower bottom operating pressure of 2470mmH2O (G); the product flow rate after condensation of the overhead condenser is 4497.0 kg/h; after the overhead distillate (the mass concentration of acetone is 99.1%) is cooled to 29 ℃ by a full condenser, part of the overhead distillate is collected as a product, and the other part of the overhead distillate is taken as reflux, wherein the reflux ratio is 2.38. The mass concentration of acetone in the column bottom stream was 1000 ppm.
Example 2
The specific process for recovering the acetone by the rectification recovery device comprises the following steps: introducing dilute acetone with the mass concentration of 15% (the temperature is 96.5 ℃, the pressure is 0.15MPa, the vaporization enthalpy r is 13698.6kJ/kg) into a rectifying tower according to the feeding flow of 28000 kg/h; introducing water vapor (at 178 deg.C and 0.15MPa) into the bottom of the rectifying tower from an inlet pipe, wherein the feeding amount is 1548 kg/h; in the rectification process, the operation pressure at the top of the tower is-30 mmH2O (G) and the operating pressure of the tower bottom is 2mmH2O (G); the product flow rate after condensation of the overhead condenser is 4212.57 kg/h; after the overhead distillate (the mass concentration of acetone is 99.1%) is cooled to 29 ℃ by a full condenser, part of the overhead distillate is taken out as a product, and the other part of the overhead distillate is taken as reflux, wherein the reflux ratio is 2.29. The mass concentration of acetone in the column bottom stream was 1000 ppm.
Comparative example 2
The specific process of acetone recovery by adopting the existing plate-type rectifying tower is as follows: dilute acetone with the mass concentration of 15% (the temperature is 96.5 ℃, the pressure is 0.15MPa, the vaporization enthalpy r is 13698.6kJ/kg) is introduced into the rectifying tower according to the feeding flow rate of 28000 kg/h; introducing water vapor (at 178 deg.C and 0.15MPa) into the bottom of the rectifying tower from the gas inlet pipe, wherein the feeding amount is 1874 kg/h; during the rectification and extraction process, the operation pressure at the top of the tower is-30 mmH2O (G) tower bottom operating pressure of 2470mmH2O (G); the product flow rate after condensation of the overhead condenser is 4212.24 kg/h; after the overhead distillate (the mass concentration of acetone is 99.1%) is cooled to 29 ℃ by a full condenser, part of the overhead distillate is taken out as a product, and the other part of the overhead distillate is taken as reflux, wherein the reflux ratio is 2.34. The mass concentration of acetone in the column bottom stream was 1000 ppm.
Example 3
The specific process for recovering the acetone by the rectification recovery device comprises the following steps: introducing dilute acetone with mass concentration of 20% (temperature of 96.5 ℃, pressure of 0.15MPa, vaporization enthalpy r of 13040.9kJ/kg) into a rectifying tower according to feed flow of 20000 kg/h; introducing water vapor (at 178 ℃ and 0.15MPa) into the bottom of the rectifying tower from an air inlet pipeline, wherein the feeding amount is 1096 kg/h; in the rectification process, the operation pressure at the top of the tower is-30 mmH2O (G) and the operating pressure of the tower bottom is 2mmH2O (G); the product flow rate after condensation of the overhead condenser is 4019.11 kg/h; and cooling the overhead distillate (the mass concentration of acetone is 99.1%) to 29 ℃ through a full condenser, and collecting part of the overhead distillate as a product and collecting part of the overhead distillate as reflux, wherein the reflux ratio is 2.24. The acetone mass concentration in the column bottoms stream was 998.9 ppm.
Comparative example 3
The specific process of acetone recovery by adopting the existing plate-type rectifying tower is as follows: introducing dilute acetone with mass concentration of 20% (temperature of 96.5 ℃, pressure of 0.15MPa, vaporization enthalpy r of 13040.9kJ/kg) into a rectifying tower according to feed flow of 20000 kg/h; introducing water vapor (with the temperature of 178 ℃ and the pressure of 0.15MPa) into the bottom of the rectifying tower from a gas inlet pipeline, wherein the feeding amount is 1357 kg/h; in the rectification process, the operation pressure at the top of the tower is-30 mmH2O (G) tower bottom operating pressure of 2470mmH2O (G); the product flow rate after condensation of the overhead condenser is 4018.82 kg/h; after the overhead distillate (the mass concentration of acetone is 99.1%) is cooled to 29 ℃ by a full condenser, part of the overhead distillate is taken out as a product, and the other part of the overhead distillate is taken as reflux, wherein the reflux ratio is 2.32. The mass concentration of acetone in the column bottom stream was 1000 ppm.
A comparison of the process and performance parameters of examples 1-3 and comparative examples 1-3 is shown in Table 1.
TABLE 1 comparison of the operation of plate-type rectification and packed rectification
As can be seen from Table 1, in the production process of the acetate fiber tows, compared with the traditional plate-type tower rectification process, the acetone-water novel packed tower rectification process adopted by the invention can reduce the steam consumption by 12-20% under the condition of meeting the same product purity and separation requirements, so that the efficient packed rectification has obvious energy-saving effect and greatly reduces the operation cost of the rectification tower.
Finally, it should be emphasized that the above-described preferred embodiments of the present invention are merely examples of implementations, rather than limitations, and that many variations and modifications of the invention are possible to those skilled in the art, without departing from the spirit and scope of the invention.
Claims (9)
1. Rectification recovery unit, its characterized in that: the rectifying tower comprises a tower top, a tower kettle and a packing layer, the packing layer is positioned between the tower top and the tower kettle, the condensing cooler is communicated with the tower top through a first guide pipe, the condensing cooler is communicated with the reflux tank through a discharge pipe, the reflux tank is communicated with the tower top through a reflux pipe and a discharge hole, and the tower kettle is connected with an air inlet pipe;
the height of the filler layer is 5.5-6 m, the filler layer comprises a first section of filler section, a second section of filler section and a third section of filler section, and fillers are respectively arranged in the first section of filler section, the second section of filler section and the third section of filler section; the first section of packing section, the second section of packing section and the third section of packing section are sequentially arranged from top to bottom along the height direction of the rectifying tower, and the gas-liquid distributors are respectively arranged between the first section of packing section and the second section of packing section and between the second section of packing section and the third section of packing section; the height of the first section of the packing section is 1.0-1.25 m, the height of the second section of the packing section is 1.0-1.25 m, and the height of the third section of the packing section is 3.0-3.5 m;
and a feed inlet is also arranged between the second section of filling section and the third section of filling section.
2. The rectification recovery device according to claim 1, wherein:
the gas-liquid distributor between the first section of packing section and the second section of packing section and the gas-liquid distributor between the second section of packing section and the third section of packing section are respectively connected with a lateral line extraction device, the lateral line extraction device is connected with a chromatography tank, and the chromatography tank is communicated with the rectifying tower through a lateral line reflux pump and a lateral line reflux pipe.
3. The rectification recovery device according to claim 1, wherein:
the feed inlet department is provided with the feeding pre-heater, the feeding pre-heater pass through the inlet pipe with the feed inlet intercommunication.
4. The rectification recovery apparatus according to any one of claims 1 to 3, characterized in that:
the filler is Sil's Mel lapak 500Y type filler.
5. A method for recovering acetone in an acetone aqueous solution by rectification is characterized by comprising the following steps:
the use of the rectification recovery apparatus as claimed in any one of claims 1 to 4 for recovering acetone in an aqueous acetone solution, the method comprising:
heating steam is introduced into the tower kettle through the air inlet pipe, acetone aqueous solution with the acetone mass concentration of 2% -30% is injected into the rectifying tower through the feeding port and rectified, gas-phase materials at the top of the tower enter the condensing cooler and flow into the reflux tank after being condensed, part of distillates in the reflux tank are extracted as acetone products, and the rest distillates flow back into the rectifying tower, wherein the reflux ratio is 2.0-3.0.
6. The method for rectifying and recovering acetone in the acetone aqueous solution according to claim 5 is characterized in that:
the temperature of the heating steam is 175-180 ℃, the heating steam enters the tower kettle under 0.15MPa, and the temperature of the tower kettle is controlled at 99-102 ℃.
7. The method for rectifying and recovering acetone in the acetone aqueous solution according to claim 6, is characterized in that:
the operation pressure of the tower top is controlled to be-220 mmH2O～10mmH2O。
8. The method for rectifying and recovering acetone in the acetone aqueous solution according to claim 5 is characterized in that:
the temperature of the acetone aqueous solution at the feed inlet is controlled to be 90-97 ℃.
9. The method for rectifying and recovering acetone in the acetone aqueous solution according to claim 5 is characterized in that:
the gas-liquid distributors between the first section of packing section and the second section of packing section and the side draws on the gas-liquid distributors between the second section of packing section and the third section of packing section are controlled to be 150 kg/hr-450 kg/hr.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114906823A (en) * | 2022-05-07 | 2022-08-16 | 南通星球石墨股份有限公司 | Method for removing fluorine and chlorine by sulfuric acid |
| CN115155093A (en) * | 2022-08-09 | 2022-10-11 | 山东蓝湾新材料有限公司 | Distillation column is used in production of dimethylamino ethyl acrylate |
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2021
- 2021-12-15 CN CN202111538478.6A patent/CN114307214A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114906823A (en) * | 2022-05-07 | 2022-08-16 | 南通星球石墨股份有限公司 | Method for removing fluorine and chlorine by sulfuric acid |
| CN115155093A (en) * | 2022-08-09 | 2022-10-11 | 山东蓝湾新材料有限公司 | Distillation column is used in production of dimethylamino ethyl acrylate |
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