CN110551020A - Method for recovering acrylic acid in wastewater - Google Patents
Method for recovering acrylic acid in wastewater Download PDFInfo
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- CN110551020A CN110551020A CN201810541081.4A CN201810541081A CN110551020A CN 110551020 A CN110551020 A CN 110551020A CN 201810541081 A CN201810541081 A CN 201810541081A CN 110551020 A CN110551020 A CN 110551020A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
- C07C51/43—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation
- C07C51/44—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation by distillation
- C07C51/445—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation by distillation by steam distillation
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Abstract
The invention relates to a method for recovering acrylic acid in wastewater, which comprises the following steps: s1, sending a first material flow of a liquid phase to a light component fractionating tower for distillation to obtain a second material flow in a gas phase and a third material flow in a liquid phase; s2, sending the third material flow to a de-acetic acid tower for distillation to obtain a fourth material flow in a gas phase and a fifth material flow in a liquid phase; s3, sending the fifth material flow to an acrylic acid purification tower for distillation to obtain a sixth material flow in a gas phase and a seventh material flow in a liquid phase, wherein the sixth material flow is condensed at the top of the acrylic acid purification tower and then divided into two parts, one part of the sixth material flow is refluxed to the acrylic acid purification tower, and the other part of the sixth material flow is sent to a finished product tank. S4, sending the seventh stream to an acrylic acid stripping tower for distillation to obtain an eighth stream in a gas phase and a ninth stream in a liquid phase, sending the eighth stream to the light component fractionating tower, and sending the ninth stream to the outside. According to the invention, the recovery of acrylic acid in the wastewater is realized, and the utilization rate of raw materials is improved.
Description
Technical Field
the invention relates to a method for recovering acrylic acid in wastewater, in particular to a method for recovering acrylic acid in wastewater in acrolein production.
background
Acrolein is used as an important fine chemical intermediate, is mainly used for preparing animal feed additives such as methionine, glycerol, glutaraldehyde and water treatment agents, and is widely applied to industries such as feed industry, papermaking, water treatment and medical treatment. The preparation technology of the acrolein mainly comprises a formaldehyde-acetaldehyde gas phase condensation method, a propylene ether pyrolysis method and a propylene oxidation method. The existing method for preparing acrolein by propylene oxidation is the best method for industrially producing acrolein, and the method has the advantages of simple production process, low-price and easily-obtained raw materials, good product quality and suitability for large-scale industrial production; the method takes propylene and oxygen as raw materials, and generates strong exothermic oxidation reaction under the action of a catalyst, so that acrolein is mainly generated in the reaction, and byproducts such as acrylic acid, propionic acid, acetic acid, carbon monoxide, carbon dioxide and the like are generated at the same time. The acrylic acid-containing wastewater generated by the traditional acrolein production process can only be treated as three wastes because of low acrylic acid content, so that the treatment difficulty is high, and the acrylic acid in the wastewater is wasted.
Disclosure of Invention
The invention aims to provide a method for recovering acrylic acid in wastewater, which can recover acrylic acid in wastewater generated in an acrolein production process.
in order to achieve the above object, the present invention provides a method for recovering acrylic acid from wastewater, comprising:
S1, sending a first material flow of a liquid phase to a light component fractionating tower for distillation to obtain a second material flow in a gas phase and a third material flow in a liquid phase;
S2, sending the third material flow to a de-acetic acid tower for distillation to obtain a fourth material flow in a gas phase and a fifth material flow in a liquid phase;
s3, sending the fifth material flow to an acrylic acid purification tower for distillation to obtain a sixth material flow in a gas phase and a seventh material flow in a liquid phase, wherein the sixth material flow is condensed at the top of the acrylic acid purification tower and then divided into two parts, one part of the sixth material flow is refluxed to the acrylic acid purification tower, and the other part of the sixth material flow is sent to a finished product tank.
S4, sending the seventh stream to an acrylic acid stripping tower for distillation to obtain an eighth stream in a gas phase and a ninth stream in a liquid phase, sending the eighth stream to the light component fractionating tower, and sending the ninth stream to the outside.
According to one aspect of the invention, in step S2, the third stream is divided into two parts, wherein one part is cooled by heat exchange and then refluxed to the bottom of the light component fractionating tower, and the other part is sent to the acetic acid removing tower.
According to an aspect of the present invention, in step S2, the fourth stream is condensed at the top of the de-acetic acid column and then divided into two parts, wherein one part is mixed with the third stream fed to the de-acetic acid column and then refluxed to the de-acetic acid column, and the other part is sent to the bottom of the light component fractionation column.
According to one aspect of the present invention, in step S1, the second stream is condensed at the top of the light ends fractionation column and then divided into two portions, one of which is refluxed to the light ends fractionation column and the other is sent to a waste disposal unit.
according to one aspect of the present invention, in step S3, the fifth stream is divided into two parts, one of which is cooled by heat exchange and then refluxed to the bottom of the acetic acid removal column, and the other is sent to the acrylic acid purification column.
According to an aspect of the present invention, in step S4, the seventh stream is divided into two parts, one of which is cooled by heat exchange and refluxed to the bottom of the acrylic acid purification column, and the other is sent to the acrylic acid stripping column.
According to one aspect of the present invention, in step S1, the overhead operating temperature of the light ends fractionation column is 35 to 55 ℃;
The tower bottom operating temperature of the light component fractionating tower is 80-100 ℃;
The light component fractionation column is operated at a pressure of 10 to 40 kPaA.
According to one aspect of the invention, in step S2, the tower top operation temperature of the de-acetic acid tower is 55-75 ℃;
The tower bottom operating temperature of the acetic acid removing tower is 85-105 ℃;
the operating pressure of the de-acetic acid tower is 5-30 kPaA.
according to an aspect of the present invention, in step S3, the top operating temperature of the acrylic acid purifying column is 50 to 70 ℃;
The tower bottom operating temperature of the acrylic acid purification tower is 90-110 ℃;
The operating pressure of the acrylic acid purification column is 2 to 25 kPaA.
According to an aspect of the present invention, in step S4, the operating temperature of the acrylic acid stripping column is 85 to 105 ℃;
The operating pressure of the acrylic acid stripping column is 20 to 50 kPaA.
according to one scheme of the invention, the acrylic acid in the wastewater is effectively recovered after the processes of light fraction removal, acetic acid removal and purification are sequentially carried out on the wastewater containing the acrylic acid. Meanwhile, acrylic acid in the material flow is recovered by further stripping after purification is finished, so that the recovery rate of acrylic acid is further improved, and the waste of acrylic acid is avoided. According to the invention, the operation temperature and the operation pressure in each separation tower are controlled, so that the recovery of acrylic acid in the waste water is further improved, and the recovery efficiency of the acrylic acid is further improved. According to the invention, by recovering the acrylic acid in the wastewater generated in the acrolein production process, the problem of overhigh treatment of three wastes (COD (chemical oxygen demand) is solved, and the wastewater treatment cost is reduced; but also improves the utilization rate of the raw materials and further improves the economic benefit.
According to one embodiment of the invention, the reflux portions of the third and fourth streams are mixed so that the fourth stream is fully absorbed by the third stream, thereby facilitating the rapid return of the mixed stream to the bottom of the de-acetic acid column. Meanwhile, the third material flow absorbs the fourth material flow, so that the acrylic acid in the fourth material flow is fully recovered, and the recovery rate of the acrylic acid is further improved. The fourth stream is conveyed to the light component fractionating tower, the third stream and the fourth stream are mixed through the tower bottom of the light component fractionating tower, the acrylic acid in the fourth stream is fully recovered by the third stream, and the recovery rate of the acrylic acid is further improved.
According to one scheme of the invention, the seventh stream is stripped by arranging an acrylic acid stripping tower, so that the recovery of the residual acrylic acid in the seventh stream is realized, the stripped eighth stream is conveyed to the light component fractionating tower, the eighth stream and the third stream are converged, the third stream can fully absorb the acrylic acid in the eighth stream, and the improvement of the recovery rate of the acrylic acid is further facilitated.
Drawings
FIG. 1 schematically shows a structural view of an acrylic acid recovering system according to an embodiment of the present invention.
Detailed Description
in order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the embodiments will be briefly described below. It is obvious that the drawings in the following description are only some embodiments of the invention, and that for a person skilled in the art, other drawings can be derived from them without inventive effort.
In describing embodiments of the present invention, the terms "longitudinal," "lateral," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," and the like are used in an orientation or positional relationship that is based on the orientation or positional relationship shown in the associated drawings, which is for convenience and simplicity of description only, and does not indicate or imply that the referenced device or element must have a particular orientation, be constructed and operated in a particular orientation, and thus, the above-described terms should not be construed as limiting the present invention.
The present invention is described in detail below with reference to the drawings and the specific embodiments, which are not repeated herein, but the embodiments of the present invention are not limited to the following embodiments.
According to an embodiment of the present invention, a method for recovering acrylic acid in wastewater of the present invention comprises:
S1, sending a first material flow A in a liquid phase to a light component fractionating tower 1 for distillation to obtain a second material flow B in a gas phase and a third material flow C in a liquid phase;
S2, sending the third material flow C to an acetic acid removal tower 2 for distillation to obtain a fourth material flow D in a gas phase and a fifth material flow E in a liquid phase;
s3, sending the fifth material flow E to an acrylic acid purification tower 3 for distillation to obtain a sixth material flow F in a gas phase and a seventh material flow G in a liquid phase, wherein the sixth material flow F is condensed at the top of the acrylic acid purification tower 3 and then divided into two parts, one part of the two parts reflows to the acrylic acid purification tower 3, and the other part of the two parts is sent to a finished product tank 4.
S4, sending the seventh material flow G to an acrylic acid stripping tower 5 for distillation to obtain an eighth material flow H in a gas phase and a ninth material flow I in a liquid phase, sending the eighth material flow H to a light component fractionating tower 1, and sending the ninth material flow I to the outside.
The process of the present invention is carried out by an acrylic acid recovery system. As shown in fig. 1, according to an embodiment of the present invention, an acrylic acid recovery system includes a light component fractionating tower 1, a de-acetic acid tower 2, an acrylic acid purifying tower 3, a finished product tank 4, an acrylic acid stripping tower 5, and a waste treatment unit 6. in the present embodiment, the tops of the light component fractionating tower 1, the de-acetic acid tower 2, and the acrylic acid purifying tower 3 are respectively provided with a condenser 7, and the condenser 7 constitutes a top reflux sub-system at the tops of the light component fractionating tower 1, the de-acetic acid tower 2, and the acrylic acid purifying tower 3 through pipes, respectively. The bottoms of the light component fractionating tower 1, the acetic acid removing tower 2 and the acrylic acid purifying tower 3 are respectively provided with a heat exchanger 8, and the heat exchangers 8 respectively form tower bottom reflux subsystems at the bottoms of the light component fractionating tower 1, the acetic acid removing tower 2 and the acrylic acid purifying tower 3 through pipelines. In this embodiment, the bottom of the light ends fractionation column 1 is also connected by a line to the overhead reflux sub-system at the top of the de-acetic acid column 2. The top reflux subsystem at the top of the light fraction fractionating tower 1 is connected to a waste treatment plant 6. The tower bottom of the acetic acid removing tower 2 is connected with an acrylic acid purifying tower 3 through a pipeline. The top reflux subsystem at the top of the acrylic acid purifying tower 3 is connected with the finished product tank 4, and the bottom of the acrylic acid purifying tower 3 is connected with the acrylic acid stripping tower 5 through a pipeline. The top of the acrylic acid stripping column 5 is connected to the light component fractionation column 1 through a line.
in step S1, the first stream a in the liquid phase is sent to the light components fractionation column 1 to be distilled to obtain a second stream B in the vapor phase and a third stream C in the liquid phase. In this embodiment, water, acetic acid and acrylic acid in the first stream a are separated in the light component fractionation column 1 and then distilled off from the top of the column to produce a second stream B containing water and acetic acid. The second stream B is condensed by the condenser 7 of the overhead reflux sub-system of the light fraction fractionating column 1 and then divided into two parts, wherein one part of the second stream B is refluxed into the light fraction fractionating column 1, and the other part of the second stream B is sent to the waste treatment device 6 through a pipeline. The second stream B conveyed to the waste treatment device 6 is treated by adopting a thermal incineration or biological treatment method and is discharged after reaching the standard.
In this embodiment, the first stream a is sent to the light fraction fractionating column 1 for distillation, the operating temperature of the bottom of the light fraction fractionating column 1 is in the range of 80 to 100 ℃, the operating temperature of the top of the light fraction fractionating column 1 is in the range of 35 to 55 ℃, and the operating pressure of the light fraction fractionating column is in the range of 10 to 40 kPaA. By setting the operation temperature of the bottom of the light component fractionating tower 1 to 80-100 ℃ and the operation pressure of the light component fractionating tower to 10-40kPaA, the method is favorable for quickly separating water, acetic acid and acrylic acid in the first material flow A, so that the concentration of acrylic acid in the third material flow C is effectively increased, and the extraction of acrylic acid in the third material flow C is further favorable. The operation temperature of the top of the light component fractionating tower 1 is set to be 35-55 ℃, so that the second stream B is cooled when passing through the top of the light component fractionating tower 1, thereby being beneficial to cooling or condensing acrylic acid-containing components of the second stream B, being beneficial to recovering acrylic acid contained in the second stream B, reducing the content of acrylic acid in the second stream B and further improving the recovery efficiency of acrylic acid.
In step S2, the third stream C is sent to the deacetylation column 2 to be distilled to obtain a fourth stream D in a vapor phase and a fifth stream E in a liquid phase. In this embodiment, the third stream C is sent out from the bottom of the light component fractionation tower 1 and then divided into two parts, wherein one part of the third stream C is sent to the bottom reflux subsystem through a pipeline, and is cooled by heat exchange in the heat exchanger 8 and then refluxed to the bottom of the light component fractionation tower 1, and the other part of the third stream C is sent to the acetic acid removal tower 2 through a pipeline. In the present embodiment, water, acetic acid and a part of acrylic acid in the third stream C are distilled out to form a fourth stream D in the deethanizer 2, and a fifth stream E is formed at the bottom of the deethanizer 2. The fourth material flow D is condensed by a condenser 7 in a reflux subsystem at the top of the acetic acid removing tower 2 and then is divided into two parts, wherein one part of the fourth material flow D is mixed with the third material flow C conveyed to the acetic acid removing tower 2 and then is refluxed to the acetic acid removing tower 2, and the other part of the fourth material flow D is conveyed to the bottom of the light component fractionating tower 1 through a pipeline. By mixing the reflux parts of the third stream C and the fourth stream D, the fourth stream D can be fully absorbed by the third stream C, and the mixed stream can be quickly returned to the bottom of the acetic acid removing tower 2. Meanwhile, the third material flow C absorbs the fourth material flow D, so that the acrylic acid in the fourth material flow D is fully recovered, and the recovery rate of the acrylic acid is further improved. The fourth material flow D is conveyed to the light component fractionating tower 1, the third material flow C and the fourth material flow D are mixed through the tower bottom of the light component fractionating tower 1, the acrylic acid in the fourth material flow D is fully recovered by the third material flow C, and the recovery rate of the acrylic acid is further improved.
in this embodiment, the third stream C is sent to the deethanizer 2 for distillation. The operation temperature of the tower bottom of the acetic acid removing tower 2 is 85-105 ℃, and the operation pressure of the acetic acid removing tower 2 is 5-30 kPaA. By setting the operation temperature at the bottom of the acetic acid removing tower 2 to 85-105 ℃ and the operation pressure of the acetic acid removing tower 2 to 5-30kPaA, the rapid separation of the acetic acid and the acrylic acid in the third material flow C is facilitated, so that the concentration of the acrylic acid in the fifth material flow E is effectively increased, and the extraction of the acrylic acid in the fifth material flow E is further facilitated. The operation temperature of the top of the acetic acid removing tower 2 is set to be 55-75 ℃, so that the fourth material flow D is cooled when passing through the top of the acetic acid removing tower 2, thereby being beneficial to cooling or condensing the component containing acrylic acid in the fourth material flow D, effectively separating the acrylic acid and acetic acid in the fourth material flow D, being beneficial to recovering the acrylic acid in the fourth material flow D, reducing the content of the acrylic acid in the fourth material flow D and further improving the recovery efficiency of the acrylic acid.
In step S3, the fifth stream E is sent to the acrylic acid purification column 3 to be distilled to obtain a sixth stream F in a vapor phase and a seventh stream G in a liquid phase. In the embodiment, the fifth material flow E is sent out from the bottom of the acetic acid removing column 2 and then divided into two parts, wherein one part of the fifth material flow E is sent to the bottom reflux subsystem through a pipeline, and is sent to the bottom of the acetic acid removing column 2 through the heat exchanger 8 for heat exchange and cooling, and then is refluxed to the bottom of the acetic acid removing column 2, and the other part of the fifth material flow E is sent to the acrylic acid purifying column 3 through a pipeline. In the present embodiment, the heavy components in the fifth stream E are separated from acrylic acid in the acrylic acid purification column 3 to form a sixth stream F containing acrylic acid at the top and a seventh stream G containing heavy components at the bottom of the acrylic acid purification column 3. The sixth material flow F is condensed by a condenser 7 in a reflux subsystem at the top of the acrylic acid purifying tower 3 and then divided into two parts, wherein one part of the sixth material flow F refluxes to the acrylic acid purifying tower 3, and the other part of the sixth material flow F is sent to a finished product tank 4 through a pipeline.
in the present embodiment, the fifth stream E is sent to the acrylic acid purification column 3 for distillation. The bottom operating temperature of the acrylic acid purifying column 3 is 90 to 110 ℃ and the operating pressure of the acrylic acid purifying column 3 is 2 to 25 kPaA. The operating temperature of the bottom of the acrylic acid purification column 3 is set to 90-110 ℃, and the operating pressure of the acrylic acid purification column 3 is set to 2-25kPaA, so that the acrylic acid in the fifth material flow E is favorably and rapidly purified, the acrylic acid is separated from heavy components in the fifth material flow E, and the purity of the acrylic acid in the sixth material flow F is effectively improved. The operation temperature of the top of the acrylic acid purification column 3 is set to 50 to 70 ℃, so that the sixth stream F is cooled while passing through the top of the acrylic acid purification column 3, thereby facilitating the cooling or condensation of heavy components contained in the sixth stream F, effectively separating acrylic acid from the heavy components contained in the sixth stream F, and further improving the purity of acrylic acid in the sixth stream F.
In step S4, the seventh stream G is sent to an acrylic acid stripping column 5 to be distilled to obtain an eighth stream H in a vapor phase and a ninth stream I in a liquid phase, the eighth stream H is sent to a lights fractionation column 1, and the ninth stream I is sent to the outside. In the present embodiment, the seventh stream G at the bottom of the acrylic acid purifying column 3 is sent out and divided into two parts, wherein one part of the seventh stream G is sent to the bottom reflux subsystem through a pipeline, and is sent to the bottom of the acrylic acid purifying column 3 through the heat exchanger 8 for heat exchange and cooling, and then is refluxed to the bottom of the acrylic acid purifying column 3, and the other part of the seventh stream G is sent to the acrylic acid stripping column 5 through a pipeline. Steam J is introduced into the acrylic acid stripping column 5, and the input position of the steam J is below the position where the seventh stream G is introduced. In the present embodiment, the seventh stream G is stripped of acrylic acid by steam J to form an eighth stream H in a vapor phase, and the eighth stream H is sent to the light components fractionation column 1 through a pipe at the top of the acrylic acid stripping column 5 to further recover acrylic acid. Meanwhile, the ninth material flow I of the liquid phase is conveyed to the outside for packaging treatment. The seventh material flow G is stripped by the acrylic acid stripping tower 5, so that residual acrylic acid in the seventh material flow G is recovered, the stripped eighth material flow H is conveyed to the light component fractionating tower 1, the eighth material flow H and the third material flow C are converged, the third material flow C can fully absorb acrylic acid in the eighth material flow H, and the recovery rate of the acrylic acid is further improved.
In this embodiment, the seventh stream G is sent to acrylic acid stripper 5 for distillation. The operating temperature of acrylic acid stripping column 5 is 85 to 105 ℃ and the operating pressure of acrylic acid stripping column 5 is 20 to 50 kPaA. By setting the operating temperature of the acrylic acid stripping tower 5 to 85-105 ℃ and the operating pressure of the acrylic acid stripping tower 5 to 20-50kPaA, the acrylic acid in the seventh stream G is effectively separated from heavy components, the content of acrylic acid in the eighth stream H is effectively increased, the recovery of acrylic acid in the eighth stream H is facilitated, and the recovery efficiency of acrylic acid is further increased.
The foregoing is merely exemplary of particular aspects of the present invention and devices and structures not specifically described herein are understood to be those of ordinary skill in the art and are intended to be implemented in such conventional ways.
The above description is only one embodiment of the present invention, and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A method for recovering acrylic acid from wastewater, comprising:
s1, sending a first material flow of a liquid phase to a light component fractionating tower for distillation to obtain a second material flow in a gas phase and a third material flow in a liquid phase;
S2, sending the third material flow to a de-acetic acid tower for distillation to obtain a fourth material flow in a gas phase and a fifth material flow in a liquid phase;
S3, sending the fifth material flow to an acrylic acid purification tower for distillation to obtain a sixth material flow in a gas phase and a seventh material flow in a liquid phase, wherein the sixth material flow is condensed at the top of the acrylic acid purification tower and then divided into two parts, one part of the sixth material flow is refluxed to the acrylic acid purification tower, and the other part of the sixth material flow is sent to a finished product tank.
s4, sending the seventh stream to an acrylic acid stripping tower for distillation to obtain an eighth stream in a gas phase and a ninth stream in a liquid phase, sending the eighth stream to the light component fractionating tower, and sending the ninth stream to the outside.
2. The method of claim 1, wherein in step S2, the third stream is divided into two parts, one part of the three parts is cooled by heat exchange and then refluxed to the bottom of the light component fractionating tower, and the other part is sent to the acetic acid removing tower.
3. The method according to claim 2, wherein in step S2, the fourth stream is condensed at the top of the de-acetic acid column and then divided into two parts, wherein one part is mixed with the third stream fed to the de-acetic acid column and then refluxed to the de-acetic acid column, and the other part is sent to the bottom of the light components fractionation column.
4. The process of claim 1, wherein in step S1, the second stream is condensed at the top of the light ends fractionation column and divided into two portions, one portion being refluxed to the light ends fractionation column and the other portion being sent to a waste disposal unit.
5. The method of claim 1, wherein in step S3, the fifth stream is divided into two parts, one part of the fifth stream is cooled by heat exchange and then refluxed to the bottom of the acetic acid removing column, and the other part of the fifth stream is sent to the acrylic acid purifying column.
6. The method of claim 1, wherein in step S4, the seventh stream is divided into two parts, one part of the seventh stream is cooled by heat exchange and then refluxed to the bottom of the acrylic acid purification column, and the other part of the seventh stream is sent to the acrylic acid stripping column.
7. the method according to claim 1 or 4, wherein in step S1, the overhead operating temperature of the light component fractionation column is 35-55 ℃;
The tower bottom operating temperature of the light component fractionating tower is 80-100 ℃;
The light component fractionation column is operated at a pressure of 10 to 40 kPaA.
8. The method according to claim 1 or 3, wherein in step S2, the tower top operation temperature of the de-acetic acid tower is 55-75 ℃;
The tower bottom operating temperature of the acetic acid removing tower is 85-105 ℃;
the operating pressure of the de-acetic acid tower is 5-30 kPaA.
9. The method as claimed in claim 1, wherein, in step S3, the operating temperature of the top of the acrylic acid purification column is 50-70 ℃;
the tower bottom operating temperature of the acrylic acid purification tower is 90-110 ℃;
The operating pressure of the acrylic acid purification column is 2 to 25 kPaA.
10. The method according to claim 1, wherein in step S4, the operating temperature of the acrylic acid stripping column is 85-105 ℃;
The operating pressure of the acrylic acid stripping column is 20 to 50 kPaA.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115259509A (en) * | 2022-06-06 | 2022-11-01 | 兰州石化职业技术学院 | Acrylic acid effluent treatment plant |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115259509A (en) * | 2022-06-06 | 2022-11-01 | 兰州石化职业技术学院 | Acrylic acid effluent treatment plant |
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