CN110724252B - Polyester resin synthesis device and synthesis method thereof - Google Patents
Polyester resin synthesis device and synthesis method thereof Download PDFInfo
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- CN110724252B CN110724252B CN201910949459.9A CN201910949459A CN110724252B CN 110724252 B CN110724252 B CN 110724252B CN 201910949459 A CN201910949459 A CN 201910949459A CN 110724252 B CN110724252 B CN 110724252B
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- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 18
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 18
- 229920001225 polyester resin Polymers 0.000 title claims abstract description 17
- 239000004645 polyester resin Substances 0.000 title claims abstract description 17
- 238000001308 synthesis method Methods 0.000 title claims abstract description 9
- 238000006243 chemical reaction Methods 0.000 claims abstract description 34
- 230000007246 mechanism Effects 0.000 claims abstract description 30
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 22
- 238000009833 condensation Methods 0.000 claims abstract description 22
- 230000005494 condensation Effects 0.000 claims abstract description 22
- 238000000034 method Methods 0.000 claims abstract description 16
- 230000008569 process Effects 0.000 claims abstract description 11
- 238000010992 reflux Methods 0.000 claims abstract description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 30
- 238000001816 cooling Methods 0.000 claims description 23
- 239000007788 liquid Substances 0.000 claims description 23
- 238000012856 packing Methods 0.000 claims description 15
- 238000010438 heat treatment Methods 0.000 claims description 13
- 239000002253 acid Substances 0.000 claims description 10
- 239000002351 wastewater Substances 0.000 claims description 10
- 239000000376 reactant Substances 0.000 claims description 9
- 239000002184 metal Substances 0.000 claims description 8
- 238000009529 body temperature measurement Methods 0.000 claims description 7
- 238000001802 infusion Methods 0.000 claims description 5
- 238000003860 storage Methods 0.000 claims description 4
- 239000002699 waste material Substances 0.000 claims description 4
- 150000001875 compounds Chemical class 0.000 claims description 3
- 239000002826 coolant Substances 0.000 claims description 3
- 239000000110 cooling liquid Substances 0.000 claims description 3
- 239000006185 dispersion Substances 0.000 claims description 3
- 238000012546 transfer Methods 0.000 claims description 2
- 230000002194 synthesizing effect Effects 0.000 claims 4
- 239000002994 raw material Substances 0.000 abstract description 12
- 238000005265 energy consumption Methods 0.000 abstract description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-O ammonium group Chemical group [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 6
- 238000005070 sampling Methods 0.000 description 5
- 239000003054 catalyst Substances 0.000 description 4
- 230000008859 change Effects 0.000 description 4
- 238000001514 detection method Methods 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- 239000003963 antioxidant agent Substances 0.000 description 2
- 230000003078 antioxidant effect Effects 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000005886 esterification reaction Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000006068 polycondensation reaction Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 229920005989 resin Polymers 0.000 description 2
- 239000011347 resin Substances 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 238000009835 boiling Methods 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 238000009795 derivation Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000002861 polymer material Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000004886 process control Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
- C08G63/78—Preparation processes
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
- C08G63/78—Preparation processes
- C08G63/785—Preparation processes characterised by the apparatus used
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- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
- Polyesters Or Polycarbonates (AREA)
Abstract
The invention discloses a polyester resin synthesis device and a synthesis method thereof, wherein the synthesis device comprises a reaction kettle, a packed tower, a condensing device and a vacuumizing device, the condensing device comprises a first condensing mechanism for carrying out primary condensation on a derived product at the top end of the packed tower and a second condensing mechanism for carrying out secondary condensation on a derived product of the first condensing mechanism, and a step-by-step temperature measuring structure is arranged on the packed tower. The method of automatic control in advance is adopted, the fluctuation of the top temperature is avoided, the loss of alcohol in the raw materials is small, the product stability is high, the reflux is not needed in the temperature rise process, and the energy consumption is obviously reduced.
Description
Technical Field
The invention belongs to the technical field of high polymer material synthesis, and particularly relates to a polyester resin synthesis device and a synthesis method thereof.
Background
At present, the known polyester resin synthesis device has large loss of raw material alcohol, unstable temperature rise control and poor stability among batches. In the known polyester resin process, in order to reduce the loss of alcohol in raw materials, when the temperature is over, the loss is reduced by adopting a full reflux mode, but the hysteresis of the mode is larger, and the energy is wasted by adopting the full reflux mode.
Disclosure of Invention
The invention aims to solve the technical problems in the prior art. Therefore, the invention provides a polyester resin synthesis device and a synthesis method thereof, aiming at reducing the loss of alcohol in raw materials.
In order to achieve the purpose, the invention adopts the technical scheme that:
the utility model provides a polyester resin synthesizer, includes reation kettle, packed tower, condensing equipment and evacuating device, condensing equipment is including being used for carrying out the first condensation mechanism of once condensation and being used for carrying out the second condensation mechanism of secondary condensation to the thing of leading out of first condensation mechanism to packed tower top, be equipped with temperature measurement structure step by step on the packed tower.
The device comprises a packed tower, a temperature measurement structure and a temperature measurement structure, wherein a metal ammonium ring area, a first wire mesh corrugated packing area, a second wire mesh corrugated packing area and an overflow groove are sequentially arranged in the packed tower from bottom to top, and the temperature measurement structure comprises a first thermometer for detecting the temperature of the metal ammonium ring area, a second thermometer for detecting the temperature of the first wire mesh corrugated packing area and a third thermometer for detecting the temperature of the second wire mesh corrugated packing area.
First condensation mechanism includes first condenser and is used for carrying out the first circulative cooling mechanism of condensation to first condenser circulating transport coolant liquid, and first circulative cooling mechanism includes circulation transfusion pipeline, locates EG storage tank, pump and heat exchanger on the circulation transfusion pipeline in proper order, the feed liquor end of circulation transfusion pipeline is connected with the bottom inlet of first condenser, and the play liquid end of circulation transfusion pipeline is connected with the top liquid outlet of first condenser.
The second condensing mechanism comprises a second condenser and a second circulating cooling mechanism for cooling the second condenser through circulating conveying water, the second circulating cooling mechanism comprises a circulating water conveying pipeline, the water inlet end of the circulating water conveying pipeline is connected with the bottom water inlet of the second condenser, the liquid outlet end of the circulating water conveying pipeline is connected with the top water outlet of the second condenser, and the second condenser is connected with the first condenser through a first conveying pipeline.
The synthesis device also comprises a waste water collecting tank, and the waste water collecting tank is connected with an outlet of the second condenser through a second conveying pipeline.
The synthesis device further comprises a tail gas collecting device, and the tail gas collecting device is connected with a gas outlet at the top end of the wastewater collecting tank through a third conveying pipeline.
The vacuumizing device comprises a vacuum pump set, and the vacuum pump set is connected with a third conveying pipeline through a vacuum pipe.
The synthesis method of the polyester resin synthesis device comprises the following steps:
step one, putting reactants into a reaction kettle for heating reaction,
and step two, controlling a first condenser at the upper part of the packed tower to condense part of vaporized reactants and then reflux the condensed reactants into the reaction kettle for continuous reaction, condensing part of vaporized compounds through a second condenser under the condition of vacuumizing, and then collecting waste liquid and tail gas.
The synthesis method comprises the steps of putting dihydric alcohol and dibasic acid into a reaction kettle, wherein the reaction parameters are as follows; before 185 ℃, the temperature rise speed is more than 5 ℃/15 min; the temperature range is 185-210 ℃, and the heating speed is 1-2 ℃/15 min; the temperature range is 210 ℃ and 240 ℃, and the heating speed is 2-4 ℃/15 min; the temperature rise control is controlled by a distributed control system, the temperature rise process controls the temperature of the lower part of the tower column of the packed tower to be between 130 and 180 ℃, the temperature of the middle part of the tower column to be between 110 and 150 ℃, and the temperature of the upper part of the tower column to be between 99 and 101 ℃.
And the dispersion control system automatically controls the EG cooling liquid to be introduced into the first condenser for condensation and cooling according to the temperature of the first conveying pipeline and the temperatures of the upper part, the middle part and the lower part of the packed tower. According to the three thermometers and the change of the top temperature (the temperature in the first conveying pipeline), the opening degree of the EG cooling regulating valve is automatically controlled by combining a Distributed Control System (DCS), and the whole temperature rising process does not need to be subjected to full reflux.
The invention has the beneficial effects that: the device realizes indirect detection of the proportion of raw material alcohol and reaction synthetic water in the tower column in the whole esterification reaction process by the improved packed tower structure and the auxiliary thermometers on the upper part, the middle part and the lower part of the tower column, reduces the loss of the raw material alcohol to the maximum extent and is beneficial to the discharge of the reaction synthetic water. The method of automatic control in advance is adopted, the fluctuation of the top temperature is avoided, the loss of alcohol in the raw materials is small, the product stability is high, the reflux is not needed in the temperature rise process, and the energy consumption is obviously reduced.
Drawings
The description includes the following figures, the contents shown are respectively:
fig. 1 is a schematic structural view of the present invention.
Labeled as:
1. the system comprises a reaction kettle, 2, a packed tower, 3, a feed port, 4, a stirrer, 5, a first condenser, 6, a circulating infusion pipeline, 7, an EG storage tank, 8, a pump, 9, a heat exchanger, 10, a second condenser, 11, a first conveying pipeline, 12, a waste water collecting tank, 13, a second conveying pipeline, 14, a tail gas collecting device, 15, a third conveying pipeline, 16, a control valve, 17, a vacuum pump set, 18, a vacuum pipe, 21, a metal ammonium ring area, 22, a first wire mesh corrugated packing area, 23 and a second wire mesh corrugated packing area.
Detailed Description
The following detailed description of the embodiments of the present invention will be given with reference to the accompanying drawings for a purpose of helping those skilled in the art to more fully, accurately and deeply understand the concept and technical solution of the present invention and to facilitate its implementation. It should be noted that the terms "upper", "lower", "front", "rear", "left", "right", "vertical", "inner", "outer", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of describing the present invention and simplifying the description, but do not indicate or imply that the referred devices or elements must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention. In the following embodiments, the terms "first", "second" and "third" do not denote absolute differences in structure and/or function, nor do they denote a sequential order of execution, but rather are used for descriptive convenience only.
As shown in figure 1, a polyester resin synthesizer, including reation kettle 1, packed tower 2, condensing equipment and evacuating device, last dog-house 3 and the agitator 4 of being equipped with of reation kettle, condensing equipment is including being used for carrying out the first condensation mechanism of once condensation and the second condensation mechanism that is used for carrying out the secondary condensation to the first condensation mechanism derivation thing to 2 tops of packed tower, is equipped with temperature measurement structure step by step on the packed tower 2. The step-by-step temperature measurement structure is convenient for detecting the temperatures of different areas of the packed tower, because the boiling point of the alcohol is higher than that of water, after the alcohol and the water are vaporized, if the alcohol is relatively less in the mixing proportion of the alcohol and the water, the temperature of the area is relatively lower, and if the alcohol is relatively more in the mixing proportion of the alcohol and the water, the temperature of the area is relatively higher. The structure of reasonable setting packed tower, through the condensation of condenser, during the reation kettle was gone into in the backward flow of packed tower after the alcohol in the raw materials can condense, the loss of alcohol in the reduction raw materials.
A metal ammonium ring area 21, a first wire mesh corrugated packing area 22, a second wire mesh corrugated packing area 23 and an overflow groove are sequentially arranged in the packed tower 2 from bottom to top, and the step-by-step temperature measuring structure comprises a first thermometer for detecting the temperature of the metal ammonium ring area, a second thermometer for detecting the temperature of the first wire mesh corrugated packing area and a third thermometer for detecting the temperature of the second wire mesh corrugated packing area. The metal ammonium ring has the advantages of uniform liquid distribution, small gas flow resistance and large fluid flow. The screen corrugated packing has the advantages that the sheets are arranged orderly, the gaps between peaks and valleys are large, and the airflow resistance is small; the direction of the channel between the corrugations is frequently changed, and the airflow turbulence is intensified; the interleaving of the net strips among the sheets and among the discs promotes the liquid to be continuously redistributed; the screen mesh is fine, liquid can form a stable film on the screen face, and even if the spraying density of the liquid is low, the liquid is easy to completely wet.
First condensation mechanism includes first condenser 5 and is used for carrying out the first circulative cooling mechanism of condensation to 5 circulative transport coolants of first condenser, and first circulative cooling mechanism includes circulation transfusion pipeline 6, locates EG storage tank 7, pump 8 and heat exchanger 9 on the circulation transfusion pipeline in proper order, and the inlet fluid end of circulation transfusion pipeline 6 is connected with the bottom inlet of first condenser 5, and the play liquid end of circulation transfusion pipeline 6 is connected with the top liquid outlet of first condenser 5. The heat exchanger is preferably a plate filter.
The second condensing mechanism comprises a second condenser 10 and a second circulating cooling mechanism for cooling the second condenser through circulating conveying water, the second circulating cooling mechanism comprises a circulating water conveying pipeline, the water inlet end of the circulating water conveying pipeline is connected with the water inlet at the bottom end of the second condenser 10, the liquid outlet end of the circulating water conveying pipeline is connected with the water outlet at the top end of the second condenser, and the second condenser is connected with the first condenser 5 through a first conveying pipeline 11.
In order to collect the liquid condensed by the second condenser, the synthesis device further comprises a waste water collecting tank 12, and the waste water collecting tank 12 is connected with the outlet of the second condenser 10 through a second conveying pipeline 13. The waste water collecting tank can be used for subsequent recovery and other centralized treatment after collecting waste liquid.
In order to collect tail gas, the synthesis device further comprises a tail gas collecting device 14, and the tail gas collecting device 14 is connected with the gas outlet at the top end of the waste water collecting tank 12 through a third conveying pipeline 15. Specifically, the third transfer line is provided with a control valve 16, and whether or not the exhaust gas is collected is controlled by opening and closing the control valve.
The vacuum pumping device comprises a vacuum pump unit 17, and the vacuum pump unit 17 is connected with the third conveying pipeline 15 through a vacuum pipe 18. Specifically, a control valve is provided in the vacuum tube, and whether or not the entire apparatus is evacuated is controlled by opening and closing the control valve.
The synthesis method adopting the polyester resin synthesis device comprises the following steps:
step one, putting reactants into a reaction kettle for heating reaction,
and step two, controlling a first condenser at the upper part of the packed tower to condense part of vaporized reactants and then reflux the condensed reactants into the reaction kettle for continuous reaction, condensing part of vaporized compounds through a second condenser under the condition of vacuumizing, and then collecting waste liquid and tail gas.
The device realizes indirect detection of the proportion of raw material alcohol and reaction synthetic water in the tower column in the whole esterification reaction process by the improved packed tower structure and the auxiliary thermometers arranged on the upper part, the middle part and the lower part of the tower column, reduces the loss of the raw material alcohol to the maximum extent and is beneficial to discharge of the reaction synthetic water. For temperature detection, the temperature of the reaction kettle is T1, the temperature of the lower part of the column of the packed column is T2, the temperature of the middle part of the column is T3, the temperature of the upper part of the column is T4, and the top temperature (the temperature in the first conveying pipeline connected to the outlet end of the first condenser) is T5.
In actual production, according to the changes of the three thermometers and the top temperature T5, the opening degree of the EG cooling regulating valve is automatically controlled by combining a Distributed Control System (DCS), and the whole temperature rising process does not need to be subjected to full reflux.
The synthesis device can prejudge the change of the top temperature in advance, adopts a method of automatic control in advance, avoids the fluctuation of the top temperature, has small alcohol loss in raw materials, high product stability, does not need backflow in the temperature rise process, and obviously reduces the energy consumption.
The following is detailed by specific preferred examples:
example 1
Adding the dihydric alcohol and the dibasic acid into a reaction kettle according to the proportion of 1.2:1 and a proper amount of catalyst (the adding amount of the catalyst is 1 thousandth of the total materials), wherein the reaction parameters are as follows; before 185 ℃, the heating speed is more than 5 ℃/15min, 185 ℃ plus 210 ℃, the heating speed is 1-2 ℃/15min, 210 ℃ plus 240 ℃, and the heating speed is 2-4 ℃/15 min. The temperature rise control is controlled by a Distributed Control System (DCS). The temperature raising process requires the lower temperature T2 of the column to be between 130 ℃ and 180 ℃, the middle temperature T3 of the column to be between 110 ℃ and 150 ℃, and the upper temperature T4 of the column to be between 99 ℃ and 101 ℃. According to the three thermometers and the change of the top temperature T5, the opening degree of the EG cooling adjusting valve is automatically controlled by combining a Distributed Control System (DCS).
Keeping the sampling acid value to be 4-10 (unit mgKOH/g resin, the same below) at 240 ℃, cooling, and adding dibasic acid accounting for 15% of the total mass ratio of the reaction kettle to perform end capping reaction. The reaction parameters are as follows: 200 ℃ and 235 ℃, 5 ℃/15min, a Distributed Control System (DCS) is used.
Keeping the sampling acid value at 235 ℃ to 47, and carrying out vacuum polycondensation reaction under the vacuum degree of-0.095 Mpa for about 4 hours. Adding antioxidant and promoter after vacuum, maintaining for 30-60 min, and discharging. The vacuum operation uses a Distributed Control System (DCS).
Example 2
Adding the dihydric alcohol and the dibasic acid into a reaction kettle according to the proportion of 1.1:1 and a proper amount of catalyst (the adding amount of the catalyst is 0.5 thousandth of the total materials), wherein the reaction parameters are as follows; before 185 ℃, the heating speed is more than 5 ℃/15min, 185-210 ℃, the heating speed is 1-2 ℃/15min, 210-235 ℃, and the heating speed is 2-4 ℃/15 min. The temperature rise control is controlled by a Distributed Control System (DCS). The temperature raising process requires the temperature T1 at the lower part of the column to be between 130 ℃ and 180 ℃, the temperature T2 at the middle part of the column to be between 110 ℃ and 150 ℃, and the temperature at the upper part of the column to be between 99 ℃ and 101 ℃. According to the three thermometers and the change of the top temperature T5, the opening degree of the EG cooling adjusting valve is automatically controlled by combining a Distributed Control System (DCS).
Keeping the sampling acid value to 10-15 (unit mgKOH/g resin, the same below) at 235 ℃, cooling, and adding 12% of dibasic acid by mass of the total reaction kettle for end capping reaction. The reaction parameters are 200 ℃ and 235 ℃, 5 ℃/15min, and a Distributed Control System (DCS) is used.
Keeping the sampling acid value at 235 ℃ to 44, and carrying out vacuum polycondensation reaction with the vacuum degree of-0.099 Mpa for about 6 hours. Adding antioxidant and promoter after vacuum, maintaining for 30-60 min, and discharging. The vacuum operation uses a Distributed Control System (DCS).
After the polyester resins prepared in examples 1 and 2 are prepared into powder coating and sprayed into a film, the performance of the film is detected, and the results are as follows:
the esterified water from the production processes of examples 1 and 2 was sampled and examined, and the results were as follows:
| sampling phase | Examples COD test values | COD detection value of former device |
| 185℃ | 6500-6800 | 8800-9200 |
| 200℃ | 7500-8000 | 10300-10700 |
| 215℃ | 9200-9600 | 12000-12500 |
| 225℃ | 10000-10500 | 13300-13600 |
| 240℃ | 11200-11600 | 13800-14200 |
The invention is described above with reference to the accompanying drawings. It is to be understood that the specific implementations of the invention are not limited in this respect. Various insubstantial improvements are made by adopting the method conception and the technical scheme of the invention; the present invention is not limited to the above embodiments, and can be modified in various ways.
Claims (5)
1. A polyester resin synthesis device comprises a reaction kettle, a packed tower, a condensing device, a vacuumizing device and a dispersion control system, and is characterized in that the condensing device comprises a first condensing mechanism for performing primary condensation on a derived product at the top end of the packed tower and a second condensing mechanism for performing secondary condensation on a derived product of the first condensing mechanism, and a step-by-step temperature measurement structure is arranged on the packed tower;
a metal saddle ring area, a first wire mesh corrugated packing area, a second wire mesh corrugated packing area and an overflow groove are sequentially arranged in the packed tower from bottom to top, and the step-by-step temperature measuring structure comprises a first thermometer for detecting the temperature of the metal saddle ring area, a second thermometer for detecting the temperature of the first wire mesh corrugated packing area and a third thermometer for detecting the temperature of the second wire mesh corrugated packing area;
the first condensation mechanism comprises a first condenser and a first circulating cooling mechanism for condensing cooling liquid conveyed by the first condenser in a circulating manner, the first circulating cooling mechanism comprises a circulating infusion pipeline, an EG storage tank, a pump and a heat exchanger which are sequentially arranged on the circulating infusion pipeline, the liquid inlet end of the circulating infusion pipeline is connected with the liquid inlet at the bottom end of the first condenser, and the liquid outlet end of the circulating infusion pipeline is connected with the liquid outlet at the top end of the first condenser;
the second condensation mechanism comprises a second condenser and a second circulating cooling mechanism for cooling the second condenser through circulating conveying water, the second circulating cooling mechanism comprises a circulating water conveying pipeline, the water inlet end of the circulating water conveying pipeline is connected with the water inlet at the bottom end of the second condenser, the liquid outlet end of the circulating water conveying pipeline is connected with the water outlet at the top end of the second condenser, and the second condenser is connected with the first condenser through a first conveying pipeline;
set up the thermometer in the first conveying line and measure a temperature, according to first thermometer, second thermometer, third thermometer and top temperature variation, combine distributed control system, the aperture of automatic control EG cooling governing valve lets in the EG coolant liquid and cools down first condenser.
2. The polyester resin synthesizing apparatus according to claim 1, wherein the synthesizing apparatus further comprises a waste water collecting tank connected to an outlet of the second condenser through a second transfer line.
3. The polyester resin synthesis device according to claim 2, further comprising a tail gas collection device, wherein the tail gas collection device is connected with the outlet of the top end of the waste water collection tank through a third conveying pipeline.
4. The polyester resin synthesis device according to claim 3, wherein the exhaust gas collection device comprises a vacuum pump set, and the vacuum pump set is connected with the third conveying pipeline through a vacuum pipe.
5. The method for synthesizing a polyester resin synthesizing apparatus according to any one of claims 1 to 4, characterized by comprising the steps of:
step one, putting reactants into a reaction kettle for heating reaction: the synthesis method comprises the steps of putting dihydric alcohol and dibasic acid into a reaction kettle, wherein the reaction parameters are as follows: before 185 ℃, the temperature rise speed is more than 5 ℃/15 min; the temperature range is 185-210 ℃, and the heating speed is 1-2 ℃/15 min; the temperature range is 210 ℃ and 240 ℃, and the heating speed is 2-4 ℃/15 min; the temperature rise control adopts a distributed control system to control the temperature rise process, the temperature of the lower part of the tower column of the packed tower is controlled to be between 130 and 180 ℃, the temperature of the middle part of the tower column is controlled to be between 110 and 150 ℃, and the temperature of the upper part of the tower column is controlled to be between 99 and 101 ℃; the dispersion control system automatically controls the introduction of EG cooling liquid to condense and cool the first condenser according to the temperature of the first conveying pipeline and the temperatures of the upper part, the middle part and the lower part of the packed tower;
and step two, controlling a first condenser at the upper part of the packed tower to condense part of vaporized reactants and then reflux the condensed reactants into the reaction kettle for continuous reaction, condensing part of vaporized compounds through a second condenser under the condition of vacuumizing, and then collecting waste liquid and tail gas.
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| CN116478379A (en) * | 2023-05-22 | 2023-07-25 | 广东科云诚新材料有限公司 | Hyperbranched high-performance environment-friendly polyphenylene polyester plasticizer, PVC products, preparation method and application thereof |
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| JPS6464694A (en) * | 1987-09-07 | 1989-03-10 | Mitsubishi Heavy Ind Ltd | Dry cleaning machine |
| CN100418940C (en) * | 2006-09-28 | 2008-09-17 | 天津大学 | Method for separating isopropanol from n-propanol by theoretical plate-assisted dual-temperature controlled batch distillation |
| CN202390351U (en) * | 2012-01-13 | 2012-08-22 | 青岛新宇田化工有限公司 | Device for automatically regulating and controlling tower top temperature during reaction of polyester polyol |
| CN202829903U (en) * | 2012-08-10 | 2013-03-27 | 黄山市向荣新材料有限公司 | Polyester resin production system |
| CN203609914U (en) * | 2013-11-06 | 2014-05-28 | 江苏盈天化学有限公司 | Condensation backflow device for polyester polyol synthesis |
| WO2015095879A1 (en) * | 2013-12-18 | 2015-06-25 | Invista Technologies S.A.R.L. | Method of manufacturing 2-methyl-1, 3-dioxolane in a solid state polycondensation process |
| CN109535399A (en) * | 2018-12-14 | 2019-03-29 | 浙江古纤道绿色纤维有限公司 | A kind of filling reactor |
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