CN218834038U - Novel acrylic acid reaction gas separation system - Google Patents
Novel acrylic acid reaction gas separation system Download PDFInfo
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- CN218834038U CN218834038U CN202223014595.5U CN202223014595U CN218834038U CN 218834038 U CN218834038 U CN 218834038U CN 202223014595 U CN202223014595 U CN 202223014595U CN 218834038 U CN218834038 U CN 218834038U
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Abstract
The utility model relates to a novel acrylic acid reaction gas separation system, the utility model discloses a product gas at first cools off through the primary cooling system, gets into the primary tower afterwards and separates, and the primary tower top uses raw materials propylene as the cold source, and most acrylic acid in the product gas gets into the azeotropic tower from the tower bottom after condensing in the primary tower, and the remaining product gas in the primary tower top gets into the absorption tower, utilizes the desalinized water to wash and absorb, and acrylic acid absorption liquid gets into the azeotropic tower from the tower bottom; the utility model adopts the product gas primary cooling system to efficiently recover the heat in the acrylic acid product gas, thereby not only improving the preheating temperature of fresh air, but also greatly improving the energy utilization rate of the device; the condenser at the top of the primary separation tower adopts the raw material propylene as a cold source to further condense and separate the product gas, the propylene provides a lower temperature level, and most of acrylic acid products are condensed and recovered in the primary separation tower, so that the gas amount in the subsequent absorption tower and the waste gas treatment device is greatly reduced, and the waste water amount is reduced.
Description
Technical Field
The utility model relates to an acrylic acid production technical field specifically indicates a novel acrylic acid reaction gas piece-rate system.
Background
Acrylic acid is used as an important organic chemical raw material, is widely applied to the production of adhesives and water-soluble coatings, plays an important role in the fields of chemical fibers, papermaking, leather, building materials, plastic modification, synthetic rubber, radiation curing water treatment agents and the like, and can also be further processed into butyl acrylate and the like.
Acrylic acid has undergone an era of coexistence of various preparation methods, acrylonitrile hydrolysis method, high pressure Rapu method (high pressure oxo synthesis method), modified Rapu method (low pressure oxo synthesis method), cyanoethanol method, ketene method and the like have been used as main methods for producing acrylic acid and esters, but all of these methods have been substantially eliminated due to serious corrosion of equipment, high energy consumption, low yield and high cost, and the most common acrylic acid production method at present is the propylene oxidation method. In the process of preparing acrylic acid by propylene oxidation, the product gas of an acrylic acid device is directly introduced into a quenching tower after by-product low-pressure steam, a kettle liquid circulating cooling quenching absorption system is arranged at the bottom of the quenching tower, circulating acetic acid wastewater or fresh desalted water is used as an acrylic acid product gas absorbent to absorb and separate acrylic acid products, acrylic acid crude liquid at the bottom of the quenching tower enters an azeotropic tower to carry out azeotropic separation, and tail gas at the top of the tower is partially circulated back to a reaction system after oxidation treatment, and is partially discharged. For example, chinese patents CN103193618B and CN10260036B are different in waste gas treatment, but both use fresh desalted water to quench and absorb the primarily cooled acrylic acid product gas, and part of the absorbed tail gas is recycled and part of the tail gas is disposed to an incineration system; both of them use fresh desalted water for reabsorption in order to reduce the organic content in the chilled acrylic acid tail gas, and then part of the tail gas is pressurized and circulated, which has the problems of high fresh water consumption and large amount of waste water in the subsequent separation process. In patent CN105001072B, a three-in-one absorption tower is adopted, circulating acetic acid-containing wastewater is taken as a quenching absorbent, tail gas at the top of the tower is treated by catalytic oxidation waste gas, part of the tail gas is compressed and then returns to a reaction system, and part of the tail gas is discharged; acetic acid wastewater is circularly used as a quenching absorbent of acrylic acid product gas, tail gas at the top of a quenching tower is completely sent to a waste gas treatment system, a large amount of waste gas treatment catalysts are consumed, and carbon emission is high.
In the mainstream acrylic acid product gas separation technology, the temperature of acrylic acid product gas is high when the acrylic acid product gas enters the quenching tower, and medium-low temperature waste heat in the product gas is not efficiently recovered by adopting a quenching way of circulating quench tower bottom liquid. Meanwhile, in the technology, the amount of product gas in the quenching tower is large, the separation temperature is high, and more fresh desalted water is consumed for ensuring the recovery rate of the product acrylic acid and reducing the content of organic matters in the acrylic acid tail gas after quenching. Therefore, the mainstream acrylic acid product gas separation technology at present has the problems of large treatment capacity of waste water and waste gas, low energy utilization efficiency and the like.
Therefore, the current separation system of acrylic acid reaction gas is to be further optimized.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the technical problem to prior art's current situation, thereby provide one kind can be through the high-efficient recovery of acrylic acid product gas heat improve energy utilization, reduce fresh desalination water yield, exhaust-gas treatment catalyst consumption and waste water volume, thereby accomplish the novel acrylic acid reaction gas piece-rate system that the raw materials vaporization process reduces the steam consumption through absorption product gas heat through product gas low-temperature condensation separation.
The utility model provides a technical scheme that above-mentioned technical problem adopted does:
a novel acrylic acid reaction gas separation system comprising:
a reaction system for producing acrylic acid gas;
the primary cooling system is arranged at the downstream of the reaction system and is used for recovering energy of the acrylic acid gas generated by the reaction system and preheating air; the primary cooling system is provided with a first outlet for returning gas-phase propylene obtained after energy recovery to the reaction system and a second outlet for outputting the obtained product gas;
the primary separation tower is arranged at the downstream of the primary cooling system and is used for condensing and separating the product gas, the bottom of the primary separation tower is provided with an inlet for inputting the product gas at a second outlet of the primary cooling system and a first output port for outputting a liquid phase, and the top of the primary separation tower is provided with a second output port for outputting a gas phase;
the azeotropic tower is arranged at the downstream of the primary separation tower, is communicated with a first output port of the primary separation tower, is used for carrying out azeotropic rectification separation on the acrylic acid solution, and is provided with an output port for inputting the obtained crude acrylic acid liquid at the bottom;
the acrylic acid refining system is arranged at the downstream of the azeotropic tower, is communicated with an output port at the bottom of the azeotropic tower and is used for refining propylene to obtain an acrylic acid product; and
and the absorption tower is arranged at the downstream of the primary separation tower, is communicated with a second output port of the primary separation tower, is used for washing and absorbing residual gas after condensation and separation of the primary separation tower, and is provided with a conveying pipeline for conveying part of the obtained purified circulating tail gas to the reaction system as circulating gas on the tower top. The proportion of the acrylic acid tail gas recycled as the recycle gas is 0.5 to 60.0 percent.
Preferably, the upper part of the primary separation tower is provided with a condensation structure which adopts raw material propylene as a cold source. The primary tower is a rectifying tower with a condenser, the top of the rectifying tower is provided with a condensation section, and the condensation structure is arranged in the condensation section. The operating pressure of the primary separation tower is 0.01-0.2 MPaG; the number of theoretical plates of the primary separation tower is 5-20.
Preferably, the primary cooling system comprises an air preheater, a warm water heat exchanger, a propylene superheater and a circulating water cooler which are connected in series in sequence, wherein one inlet of the air preheater is connected with an acrylic acid gas output port of the reaction system, and an outlet of the circulating water cooler forms a second outlet of the primary cooling system and is communicated with the primary separation tower.
Preferably, one side of the air preheater is provided with an inlet for inputting fresh raw material air, and the other side of the air preheater is provided with an outlet for inputting preheated fresh raw material air to the reaction system. The operation temperature of the product gas side outlet in the air preheater is 140-220 ℃.
Preferably, one side of the propylene superheater is communicated with the top of the primary separation tower and is provided with an opening for inputting vaporized propylene, and the other side of the propylene superheater is provided with a first outlet of the primary cooling system. The operating temperature of the product gas side outlet in the propylene superheater is 50-90 ℃.
Preferably, a circulating gas compressor for pressurizing the circulating gas is arranged on the conveying pipeline of the circulating gas.
Preferably, the top of the absorption tower is provided with a gas supply pipeline for supplying another part of the purified circulating tail gas to an exhaust gas treatment system, and a pipeline downstream of the exhaust gas treatment system is optionally provided with a pipeline crossing the pipeline for supplying part of the purified gas to the circulating gas. The flow proportion of the cross-line pipeline is controlled to be 0.5-60.0% (the flow of the cross-line pipeline accounts for 0.5-60.0% of the total flow of the tail gas after passing through the waste gas treatment system) so as to control the content of organic matters in the circulating gas.
Preferably, the device also comprises a condenser and a reflux tank which are connected in series with the top of the azeotropic tower and are used for carrying out non-uniform separation on the materials at the top of the azeotropic tower so as to return the separated entrainer to the azeotropic tower, discharge acetic acid-containing wastewater and discharge gas torch-removing system.
Preferably, the bottom of the azeotropic column is provided with a reboiler.
Preferably, the air preheater takes compressed fresh raw material air as a heat exchange medium, the warm water heat exchanger takes warm water as the heat exchange medium, the propylene superheater takes raw material vaporized propylene as the heat exchange medium, and the circulating water cooler takes circulating water as the heat exchange medium to sequentially recover energy of the acrylic acid product gas.
Preferably, the warm water heat exchanger is used for recovering energy of heat in a medium-temperature section of product gas, and the preheated warm water is used for heat preservation and heat tracing of the device. The operation temperature of the product gas side outlet in the warm water heat exchanger is 60-100 ℃. The operating temperature of the product gas side outlet in the circulating water cooler is 30-50 ℃.
Preferably, fresh desalted water is used as an absorbent in the absorption tower to wash and absorb the primary tower top gas, and the liquid-gas ratio of the fresh desalted water to the circulating tail gas in the absorption tower is 0.01-0.1; the operating pressure of the absorption tower is 0.01-0.2 MPaG.
Compared with the prior art, the utility model has the advantages of: the product gas of the utility model is firstly cooled by the primary cooling system and then enters the primary tower for separation, the primary tower top takes the raw material propylene as a cold source, most acrylic acid in the product gas is condensed in the primary tower and then enters the azeotropic tower from the tower bottom, the residual product gas in the primary tower top enters the absorption tower, desalted water is utilized for washing and absorption, and the acrylic acid absorption liquid enters the azeotropic tower from the tower bottom; specifically, the method comprises the following steps:
the utility model adopts the product gas primary cooling system to efficiently recover the heat in the acrylic acid product gas, thereby not only improving the preheating temperature of fresh air, but also supplying the production operation of a warm water system by the waste heat of the product gas, and greatly improving the energy utilization rate of the device; the condenser at the top of the primary separation tower adopts raw material propylene as a cold source, further condenses and separates product gas, the lower temperature level is provided for the propylene, the absorption of acrylic acid and organic matters is facilitated as the temperature is lower, most acrylic acid products are condensed and recovered in the primary separation tower, so that the gas amount in a subsequent absorption tower and a waste gas treatment device is greatly reduced, the consumption of fresh desalted water and a waste gas treatment catalyst is reduced, and the waste water amount is reduced; the raw material liquid phase propylene absorbs the heat of product gas in the primary tower condenser to complete the vaporization process, so that the original propylene evaporator is replaced, the steam consumption is reduced, and the economical efficiency of a production device is greatly improved;
the utility model discloses well adoption product gas is cold system and division tower just, adopts different heat transfer medium to carry out heat recovery to it according to the temperature position of the different sections of product gas, has improved the energy utilization efficiency of product gas waste heat. In the primary separation tower, raw material propylene is used as a cold source of the condenser, so that the condensation temperature of product gas is reduced, the recovery rate of product acrylic acid is improved, and the gas amounts in the absorption tower and the waste gas treatment system are effectively reduced. Therefore, the consumption of fresh desalted water and the exhaust gas treatment catalyst is effectively reduced, and the economic benefit and the environmental benefit of the device are greatly improved.
Drawings
FIG. 1 is a process flow diagram of example 1 of the present invention;
FIG. 2 is a process flow diagram of example 2 of the present invention;
FIG. 3 is a process flow diagram of example 3 of the present invention;
fig. 4 is a process flow diagram of embodiment 4 of the present invention.
Detailed Description
The present invention will be described in further detail with reference to the following embodiments.
Example 1:
as shown in fig. 1, the novel acrylic acid reaction gas separation system of the present example comprises:
the reaction system 1 is used for generating acrylic acid gas;
the primary cooling system 2 is arranged at the downstream of the reaction system 1 and is used for recovering energy of the acrylic acid gas generated by the reaction system 1 and preheating air; the primary cooling system 2 is provided with a first outlet for returning gas-phase propylene obtained after energy recovery to the reaction system 1 and a second outlet for outputting the obtained product gas;
the primary separation tower 3 is arranged at the downstream of the primary cooling system 2 and is used for condensing and separating the product gas, the bottom of the primary separation tower is provided with an inlet for inputting the product gas at a second outlet of the primary cooling system and a first output port for outputting the liquid phase, and the top of the primary separation tower is provided with a second output port for outputting the gas phase;
the azeotropic tower 7 is arranged at the downstream of the primary separation tower 3, is communicated with the first output port of the primary separation tower 3, is used for carrying out azeotropic rectification separation on the acrylic acid solution, and is provided with an output port for inputting the obtained crude acrylic acid liquid at the bottom of the tower;
the acrylic acid refining system 12 is arranged at the downstream of the azeotropic tower 7, is communicated with an output port at the bottom of the azeotropic tower and is used for refining propylene to obtain an acrylic acid product; and
and the absorption tower 4 is arranged at the downstream of the primary separation tower 3, is communicated with a second output port of the primary separation tower 3, is used for washing and absorbing residual gas after condensation and separation of the primary separation tower 3, and is provided with a conveying pipeline for conveying part of the obtained purified circulating tail gas to the reaction system as circulating gas. The proportion of the acrylic acid tail gas recycled as the recycle gas is 0.5 to 60.0 percent.
In this embodiment, the upper part of the preliminary separation column 3 is provided with a condensation structure using propylene as a raw material as a cooling source. The primary tower 3 is a rectifying tower with a condenser, the top of the rectifying tower is provided with a condensation section, and a condensation structure is arranged in the condensation section. The operation pressure of the primary tower 3 is 0.01-0.2 MPaG; the number of theoretical plates of the preliminary separation column is 5 to 20, and 10 plates are used in this example.
The primary cooling system 2 of this embodiment includes air heater 2.1, warm water heat exchanger 2.2, propylene over heater 2.3, circulating water cooler 2.4 that concatenate in proper order, and an import of air heater 2.1 is connected with the acrylic acid gas delivery outlet of reaction system 1, and the export of circulating water cooler 2.4 constitutes the second export of primary cooling system 2, is linked together with primary tower 3. One side of the air preheater 2.1 is provided with an inlet for inputting fresh raw material air, and the other side is provided with an outlet for inputting preheated fresh raw material air to the reaction system. The operating temperature of the product gas side outlet in the air preheater 2.1 is 140-220 ℃. One side of the propylene superheater 2.3 is communicated with the top of the primary separation tower 3 and is provided with an opening for inputting vaporized propylene, and the other side is provided with a first outlet of the primary cooling system 2. The operating temperature of the product gas side outlet in the propylene superheater 2.3 is 50-90 ℃. The air preheater 2.1 takes the compressed fresh raw material air as a heat exchange medium, the warm water heat exchanger 2.2 takes the warm water as the heat exchange medium, the propylene superheater 2.3 takes the raw material vaporized propylene as the heat exchange medium, and the circulating water cooler 2.4 takes the circulating water as the heat exchange medium to sequentially recover the energy of the acrylic acid product gas. The warm water heat exchanger 2.2 recovers energy of heat in the medium-temperature section of the product gas, and the preheated warm water is used for heat preservation and heat tracing of the device. The operating temperature of the product gas side outlet in the warm water heat exchanger 2.2 is 60-100 ℃. The operating temperature of the product gas side outlet in the circulating water cooler 2.4 is 30-50 ℃.
The circulating gas compressor 6 for pressurizing the circulating gas is arranged on the conveying pipeline of the circulating gas in the embodiment. The top of the absorption tower 4 is provided with an air supply line for supplying another part of the obtained purified circulating tail gas to the waste gas treatment system 5, and the downstream line of the waste gas treatment system 5 is optionally provided with a cross-line pipeline 5.1 for supplying a part of the purified gas to the conveying pipeline of the circulating gas. The flow ratio of the cross-line pipeline 5.1 is controlled to be 0.5-60.0% (the flow of the cross-line pipeline accounts for 0.5-60.0% of the total flow of the tail gas after passing through the waste gas treatment system) so as to control the content of organic matters in the circulating gas.
The embodiment also comprises a condenser 8 and a reflux tank 9 which are connected in series with the top of the azeotropic tower 7 and are used for carrying out non-uniform separation on the materials at the top of the azeotropic tower 7 so as to return the separated entrainer to the azeotropic tower 7, discharge acetic acid-containing wastewater and discharge waste gas torch-removing system. The bottom of the azeotropic column 7 is provided with a reboiler 11.
The absorption tower 4 takes fresh desalted water as an absorbent to wash and absorb the gas at the top of the primary separation tower, and the liquid-gas ratio of the fresh desalted water to the circulating tail gas in the absorption tower 4 is 0.01-0.1; the operating pressure of the absorption tower 4 is 0.01-0.2 MPaG.
A product gas separation system of a 20 ten thousand ton/year scale propylene oxidation acrylic acid production device is taken as an example for explanation:
acrylic acid product gas (150-300 ℃ and 0.01-0.20 MPaG) at 140-190 t/hr firstly enters a primary cooling system 2, energy recovery is carried out sequentially through an air preheater 2.1, a warm water heat exchanger 2.2, a propylene superheater 2.3 and a circulating water cooler 2.4, the temperature of the product gas is reduced to 40-60 ℃, and preheated air and gas-phase propylene are sent to a reaction system 1. The product gas after primary cooling is directly introduced into a primary separation tower 3 for condensation separation, a condensation section is arranged at the top of the primary separation tower 3, raw material liquefied propylene (12-20 ℃) is used as a cold source, and the reaction gas at the top of the primary separation tower 3 is cooled to 15-35 ℃. Most of acrylic acid in the reaction gas is condensed in the primary separation tower 3, flows out from the bottom of the tower and enters the azeotropic tower 7, and the rest gas enters the absorption tower 4. The absorption tower 4 uses fresh desalted water as an absorbent to wash and absorb the residual gas after condensation and separation of the primary separation tower 3, the liquid-gas ratio of desalted water to product gas is 0.01-0.10, purified and circulated tail gas is obtained at the top of the absorption tower 4, part of the tail gas (40-100%) is subjected to high-temperature catalytic oxidation treatment through a waste gas treatment system 5, the standard-reaching flue gas emission is realized, and part of the tail gas (0-60%) is returned to the reaction system 1 after being boosted by a circulating gas compressor 6. In order to ensure the normal operation of the reactor, a cross-line pipeline 51 between the tail gas pipeline behind the waste gas treatment system and the circulating gas is arranged, and the content of organic matters in the circulating gas can be adjusted and controlled through the flow ratio (0.0-60.0%). The bottom of the absorption tower 4 is acrylic acid absorption liquid which enters an azeotropic tower 7 for separation and purification. In the azeotropic tower 7, the acrylic acid solution is subjected to azeotropic distillation separation by adopting an entrainer at the tower top, the proportion of the entrainer to the acrylic acid solution in the azeotropic tower is 1.0-3.0, crude acrylic acid liquid obtained at the tower bottom is removed to an acrylic acid refining system 12, and finally an acrylic acid product is obtained. And after heterogeneous separation of the top of the azeotropic tower through a reflux tank 9, the entrainer returns to the azeotropic tower, the acetic acid-containing wastewater is discharged outside, and a small amount of waste gas is discharged to a torch system.
Through calculation, after the 20 ten thousand tons/year scale propylene oxidation acrylic acid preparation device adopts a novel product gas separation system, the consumption of fresh water can be reduced by about 2 t-20 t/h, which accounts for about 50-85% of the traditional technology, the consumption of steam can be saved by about 15 t-21 t/h, which accounts for about 10-15% of the traditional technology, the treatment capacity of waste gas can be reduced by about 10-40 t/h, which accounts for about 7-30% of the traditional technology, and the treatment capacity of waste liquid can be reduced by about 1 t-4 t/h, which accounts for about 5-20% of the traditional technology.
Example 2:
the present example differs from example 1 in that: as shown in fig. 2, the condensation section at the top of the preliminary separation column 3 is separated into the preliminary separation column 3, and the preliminary separation column 3 and the absorption column 4 are connected in the form of a preliminary separation column condenser 13 and a liquid separation tank 14.
Example 3:
this example differs from example 1 in that: as shown in fig. 3, in view of the small number of theoretical plates required for the preliminary separation column 3, the preliminary separation column 3 and the azeotropic column 7 are coupled in one column body to reduce the floor area of the apparatus.
Example 4:
the present example differs from example 1 in that: as shown in fig. 4, the heat exchange sequence in the product gas primary cooling system 2 is changed, and considering that the temperature of the vaporized propylene is low, in the primary cooling system 2, the compressed fresh raw material air, warm water and the circulating water vaporized propylene are sequentially used as heat exchange media to recover the energy of the acrylic acid product gas, and the condensation temperature of the product gas is reduced. After passing through the primary cooling system 1, the temperature of the product air can be reduced to 30-50 ℃.
Claims (10)
1. A novel acrylic acid reaction gas separation system characterized by comprising:
a reaction system for generating acrylic acid gas;
the primary cooling system is arranged at the downstream of the reaction system and is used for recovering energy of the acrylic acid gas generated by the reaction system and preheating air; the primary cooling system is provided with a first outlet for returning gas-phase propylene obtained after energy recovery to the reaction system and a second outlet for outputting the obtained product gas;
the primary separating tower is arranged at the downstream of the primary cooling system and is used for condensing and separating the product gas, an inlet for inputting the product gas at a second outlet of the primary cooling system and a first output port for outputting a liquid phase are formed in the bottom of the primary separating tower, and a second output port for outputting a gas phase is formed in the top of the primary separating tower;
the azeotropic tower is arranged at the downstream of the primary separation tower, is communicated with a first output port of the primary separation tower, is used for carrying out azeotropic rectification separation on the acrylic acid solution, and is provided with an output port for inputting the obtained crude acrylic acid liquid at the bottom;
the acrylic acid refining system is arranged at the downstream of the azeotropic tower, is communicated with an output port at the bottom of the azeotropic tower and is used for refining propylene to obtain an acrylic acid product; and
and the absorption tower is arranged at the downstream of the primary separation tower, is communicated with a second output port of the primary separation tower, is used for washing and absorbing residual gas after condensation and separation of the primary separation tower, and is provided with a conveying pipeline for conveying part of the obtained purified circulating tail gas to the reaction system as circulating gas on the tower top.
2. The novel acrylic acid reaction gas separation system according to claim 1, characterized in that: the upper portion of primary tower is provided with the condensation structure who adopts raw materials propylene as the cold source.
3. The novel acrylic acid reaction gas separation system according to claim 2, characterized in that: the primary tower is a rectifying tower with a condenser, the top of the rectifying tower is provided with a condensation section, and the condensation structure is arranged in the condensation section.
4. The novel acrylic acid reaction gas separation system according to claim 1, characterized in that: the primary cooling system comprises an air preheater, a warm water heat exchanger, a propylene superheater and a circulating water cooler which are sequentially connected in series, wherein one inlet of the air preheater is connected with an acrylic acid gas output port of the reaction system, and the outlet of the circulating water cooler forms a second outlet of the primary cooling system and is communicated with the primary separation tower.
5. The novel acrylic acid reaction gas separation system according to claim 4, characterized in that: and one side of the air preheater is provided with an inlet for inputting fresh raw material air, and the other side of the air preheater is provided with an outlet for inputting preheated fresh raw material air to the reaction system.
6. The novel acrylic acid reaction gas separation system according to claim 4, characterized in that: one side of the propylene superheater is communicated with the top of the primary separation tower and is provided with an opening for inputting the vaporized propylene, and the other side of the propylene superheater is provided with a first outlet of the primary cooling system.
7. The novel acrylic acid reaction gas separation system according to any one of claims 1 to 6, characterized in that: and a circulating gas compressor for pressurizing the circulating gas is arranged on the circulating gas conveying pipeline.
8. The novel acrylic acid reaction gas separation system according to any one of claims 1 to 6, characterized in that: the top of the absorption tower is provided with a gas supply pipeline for supplying the other part of the obtained purified circulating tail gas to a waste gas treatment system, and a downstream pipeline of the waste gas treatment system is optionally provided with a cross-line pipeline for supplying part of the purified gas to a conveying pipeline of the circulating gas.
9. The novel acrylic acid reaction gas separation system according to any one of claims 1 to 6, characterized in that: the device also comprises a condenser and a reflux tank which are connected with the top of the azeotropic tower in series and are used for carrying out non-uniform separation on the materials at the top of the azeotropic tower so as to return the separated entrainer to the azeotropic tower, discharging acetic acid-containing wastewater and discharging waste gas to a flare system.
10. The novel acrylic acid reaction gas separation system according to any one of claims 1 to 6, characterized in that: and a reboiler is arranged at the bottom of the azeotropic tower.
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