CN113214075B - Device and method for producing high-quality acrylic acid - Google Patents
Device and method for producing high-quality acrylic acid Download PDFInfo
- Publication number
- CN113214075B CN113214075B CN202110400314.0A CN202110400314A CN113214075B CN 113214075 B CN113214075 B CN 113214075B CN 202110400314 A CN202110400314 A CN 202110400314A CN 113214075 B CN113214075 B CN 113214075B
- Authority
- CN
- China
- Prior art keywords
- tower
- acrylic acid
- light component
- component removal
- extraction
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- 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
- C07C51/48—Separation; Purification; Stabilisation; Use of additives by liquid-liquid treatment
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The invention provides an apparatus and a method for producing high-quality acrylic acid. The utility model provides a device for producing high-quality acrylic acid, including absorption tower and lightness-removing tower, the absorption tower top of the tower is equipped with the absorption tower gaseous phase material export that is connected to the lightness-removing tower cauldron, lightness-removing tower cauldron is equipped with the lightness-removing tower liquid phase material export that is connected to the absorption tower top of the tower, be equipped with acrylic acid absorption section in the absorption tower, be equipped with acrylic acid in the lightness-removing tower and purify section and second circulation condensation segment, be equipped with second circulation condenser outside the lightness-removing tower, second circulation condenser's hot side entry linkage is under the second circulation condensation segment in the lightness-removing tower, second circulation condenser's hot side exit linkage is on the second circulation condensation segment in the lightness-removing tower. The invention can reduce the concentration of acetic acid in the absorption tower and the light component removal tower in the production process of acrylic acid, improve the quality of the concentrated acrylic acid in the tower kettle of the absorption tower, and is beneficial to further refining the concentrated acrylic acid to obtain a high-quality acrylic acid product.
Description
Technical Field
The present invention relates to an apparatus and a method for producing acrylic acid, and more particularly, to an apparatus and a method for producing high-quality acrylic acid.
Background
Acrylic acid is an unsaturated fatty acid, is an important industrial derivative of propylene, and is also one of important organic chemical raw materials. The acrylic acid contains active double bonds and carboxyl functional groups, is particularly suitable for preparing high water absorption materials, dispersants, flocculants, thickeners and the like, and is widely applied to the fields of chemical fibers, textiles, coatings, water treatment, daily necessities and the like.
In the existing acrylic acid production process, a propylene gas phase oxidation method is widely used, which takes propylene and air as raw materials, and carries out oxidation reaction through a fixed bed catalyst bed layer in the presence of water vapor and other inert gases, the reaction is divided into two steps, wherein in the first step, the propylene is oxidized into acrolein, in the second step, the acrolein is oxidized into acrylic acid, an acrylic acid gas phase mixture is obtained at the outlet of a reactor, the acrylic acid gas phase mixture mainly comprises acrylic acid gas, nitrogen, aldehyde compounds, carboxylic acid compounds, carbon dioxide, carbon monoxide, oxygen and the like, and the acrylic acid gas phase mixture is subjected to a refining separation system to obtain an acrylic acid product.
At present, the commonly used acrylic acid gas phase separation processes mainly comprise three different technical routes: organic solvent absorption rectification technology, water absorption azeotropic rectification technology and water absorption extraction rectification technology. The organic solvent absorption rectification technology has the advantages of short flow and relatively low energy consumption; the defects that the acrylic acid needs to be absorbed by a solvent, the operation temperature is high, the acrylic acid is easy to polymerize, and the operation period is short; the water absorption azeotropic distillation technology has the advantages of shorter flow, low investment cost and high operation cost, and has the disadvantages of high energy consumption and high operation cost because an azeotropic agent is required to be used; the water absorption extraction rectification technology has the advantages of low energy consumption and low operating cost; the disadvantages of longer process, high investment cost, use of extractant and high consumption of polymerization inhibitor.
Chinese patent CN102775295A discloses a method for purifying acrylic acid, which comprises two towers of absorption tower and purification tower, the acrylic acid cooling, absorption and purification process are coupled, a device composed of two towers is used to complete the recovery and refining of acrylic acid, meanwhile, water is recycled as absorbent and coolant, other solvents (extraction agent and azeotropic agent) are not used, and the pollution of solvent to environment is avoided. The method has relatively simple flow, and reduces the equipment investment cost and the running cost, but because the acetic acid aqueous solution at the top of the absorption tower is adopted as the absorbent in the method, the content of acrylic acid in the tail gas at the top of the tower is higher (about 0.3wt percent), the unit consumption of propylene is increased, and the production cost is increased more; meanwhile, because the device is not provided with liquid phase extraction of acetic acid aqueous solution, the content of acrylic acid in the tail gas at the top of the tower is reduced, and the content of acetic acid in the tower kettle of the absorption tower is increased, thereby influencing the quality of acrylic acid products extracted by the purification tower.
Chinese patent CN109232232A discloses a method for refining acrylic acid, which comprises subjecting acrylic acid process gas to high-concentration gas quenching absorption, low-concentration gas reabsorption, purification, extraction and stripping, coupling the cooling process, absorption process and purification process of acrylic acid gas phase mixture, and performing subsequent acid water treatment, wherein the absorption process is improved, and no entrainer is used in the refining process. The method has relatively simple flow and reduced operation cost, but because desalted water needs to be added from the top of the lightness-removing tower in the process of reabsorption, the desalted water is consumed, and the amount of acid water discharged from the system is increased; and the middle upper part of the light component removal tower is not provided with liquid phase extraction of acetic acid aqueous solution, which can also cause the increase of the acetic acid content in the tower kettle of the absorption tower, thereby influencing the quality of acrylic acid products extracted by the purification tower.
The process methods provided by Chinese patents CN102775295A and CN109232232A have a common problem, and are forced to increase the temperature of tail gas to be incinerated in order to reduce the content of acetic acid in the system and meet the quality of acrylic acid products, so that a small amount of acrylic acid is removed from the tail gas incineration system along with the tail gas and the acetic acid, the material consumption of the device is increased, and the yield is reduced.
Disclosure of Invention
The invention aims to provide a device for producing high-quality acrylic acid, which is applied to a process flow for producing a concentrated acrylic acid solution by quenching and absorbing acrylic acid reaction gas, and can effectively reduce the content of acetic acid in an absorption tower, thereby improving the quality of acrylic acid products of a subsequent refining unit and solving the problems in the background art.
It is another object of the present invention to provide a process for producing high-quality acrylic acid.
The technical scheme adopted by the invention for solving the technical problems is as follows:
the utility model provides a device for producing high-quality acrylic acid, including absorption tower and lightness-removing tower, the absorption tower top of the tower is equipped with the absorption tower gaseous phase material export that is connected to the lightness-removing tower cauldron, lightness-removing tower cauldron is equipped with the lightness-removing tower liquid phase material export that is connected to the absorption tower top of the tower, be equipped with acrylic acid absorption section in the absorption tower, be equipped with acrylic acid in the lightness-removing tower and purify section and second circulation condensation segment, be equipped with the second circulation condenser outside the lightness-removing tower, the hot side entry linkage of second circulation condenser is to under the second circulation condensation segment in the lightness-removing tower, the hot side exit linkage of second circulation condenser is to on the second circulation condensation segment in the lightness-removing tower.
Preferably, a first circulating condensation section is further arranged in the light component removing tower, a first circulating condenser is further arranged outside the light component removing tower, a hot-side inlet of the first circulating condenser is connected to the bottom of the light component removing tower, and a hot-side outlet of the first circulating condenser is connected to the first circulating condensation section in the light component removing tower.
Preferably, an acetic acid purification section is further arranged in the light component removal tower, the acetic acid purification section is arranged above the acrylic acid purification section, and a second wastewater extraction port is arranged at the bottom of the acetic acid purification section.
Preferably, the apparatus for producing high-quality acrylic acid further comprises an extraction column and a solvent regeneration column; the top of the extraction tower is provided with a raffinate phase outlet connected to the acrylic acid purification section, a solvent heat exchanger is arranged between the extraction tower and the solvent regeneration tower, and the bottom of the extraction tower is provided with an extract phase outlet connected to the top of the solvent regeneration tower through the solvent heat exchanger; the top of the solvent regeneration tower is provided with a gas-phase material outlet of the solvent regeneration tower connected to the lower part of the absorption tower, and the bottom of the solvent regeneration tower is provided with a liquid-phase material outlet of the solvent regeneration tower connected to the top of the extraction tower through a solvent heat exchanger.
Preferably, the bottom of the acrylic acid purification section is provided with a first wastewater extraction port connected to the tower kettle of the extraction tower, an acid water cooler is arranged between the light component removal tower and the extraction tower, the first wastewater extraction port is connected to the tower kettle of the extraction tower through the acid water cooler, a reboiler of the regeneration tower is arranged outside the solvent regeneration tower, and the reboiler of the regeneration tower is connected with the lower part of the solvent regeneration tower.
Preferably, an absorption tower heater is arranged outside the absorption tower, the absorption tower heater is connected with the lower part of the absorption tower, and the bottom of the absorption tower is provided with a raw material crude acrylic acid reaction gas inlet and a liquid phase concentrated acrylic acid outlet.
Preferably, a recycle gas compressor is arranged outside the light component removal tower, and a light component removal tower gas-phase material outlet connected to the recycle gas compressor is arranged at the top of the light component removal tower.
Preferably, the lightness-removing column is provided with an incineration waste gas outlet on the acrylic acid purification section or on the top of the lightness-removing column.
A method for producing high-quality acrylic acid according to the above apparatus, the method comprising the steps of:
(1) Feeding raw material crude acrylic acid reaction gas into the bottom of an absorption tower, feeding gas-phase materials at the top of the absorption tower into a tower kettle of a light component removal tower, discharging liquid-phase materials at the tower kettle of the absorption tower as concentrated acrylic acid out of a device, and controlling the operation pressure at the top of the absorption tower to be 50-350 kPa;
(2) The gas-phase material in the step (1) sequentially flows through an acrylic acid purification section and a second circulation condensation section in an absorption tower, the gas-phase material at the top of a light component removal tower is divided into two parts, one part is taken as a circulation gas discharge device, the other part enters a subsequent solvent regeneration tower kettle, the gas-phase side line above the acrylic acid purification section extracts incineration waste gas and discharges the incineration waste gas, the side line extracted waste water below the acrylic acid purification section enters a subsequent extraction tower kettle, the liquid-phase material at the bottom of the light component removal tower enters the top of the absorption tower, and the operation pressure at the top of the light component removal tower is 40-300 kPa;
(3) An extraction tower and a solvent regeneration tower are arranged behind the light component removal tower, raffinate phase materials at the top of the extraction tower are divided into two strands, one strand enters an acrylic acid purification section of the light component removal tower, the other strand serves as a wastewater removal device, extract phase materials at the bottom of the extraction tower enter the top of the solvent regeneration tower, and the operation pressure at the top of the extraction tower is 101-400 kPa;
(4) The gas phase at the top of the solvent regeneration tower enters the lower part of the absorption tower, the liquid phase material at the bottom of the solvent regeneration tower enters the top of the extraction tower, and the operation pressure at the top of the solvent regeneration tower is 40-400 kPa.
Preferably, in the step (1), the operation pressure at the top of the absorption tower is 101-200 kpa, the operation temperature at the top of the absorption tower is 50-95 ℃, and the operation temperature at the bottom of the absorption tower is 70-100 ℃; in the step (2), the operation pressure at the top of the lightness-removing column is 101-200 kPa, the operation temperature at the top of the lightness-removing column is 20-75 ℃, and the operation temperature at the bottom of the light-removing column is 40-90 ℃; in the step (3), the operation pressure of the top of the extraction tower is 101-200 kPa, the operation temperature of the top of the extraction tower is 20-90 ℃, and the operation temperature of the tower kettle is 20-90 ℃; in the step (4), the operation pressure at the top of the solvent regeneration tower is 101-200 kpa, the operation temperature at the top of the tower is 50-120 ℃, and the operation temperature at the bottom of the tower is 100-210 ℃.
The invention has the beneficial effects that:
the device and the method for producing high-quality acrylic acid can reduce the concentration of acetic acid in the absorption tower and the light component removal tower in the production process of acrylic acid, improve the quality of the concentrated acrylic acid at the tower bottom of the absorption tower, and facilitate the further refining of the concentrated acrylic acid to obtain a high-quality acrylic acid product.
Drawings
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 or the prior art descriptions will be briefly described below, it is obvious that the drawings in the following description are only embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the provided drawings without creative efforts.
FIG. 1 is a schematic view of example 1 of the present invention;
FIG. 2 is a schematic view of example 2 of the present invention;
FIG. 3 is a schematic view of embodiment 3 of the present invention;
FIG. 4 is a schematic view of embodiment 4 of the present invention;
FIG. 5 is a schematic view of example 5 of the present invention;
FIG. 6 is a schematic view of example 6 of the present invention;
FIG. 7 is a schematic view of example 7 of the present invention;
FIG. 8 is a schematic view of example 8 of the present invention;
FIG. 9 is a schematic view of example 9 of the present invention;
fig. 10 is a schematic view of embodiment 10 of the present invention.
In the figure: 1. raw material crude acrylic acid reaction gas inlet, 2, absorption tower gas phase material outlet, 3, liquid phase concentrated acrylic acid outlet, 4, light component removal tower gas phase material outlet, 8, second waste water outlet, 10, first waste water outlet, 12, light component removal tower liquid phase material outlet, 13, raffinate phase outlet, 17, extract phase outlet, 19, solvent regeneration tower gas phase material outlet, 20, solvent regeneration tower liquid phase material outlet, C1201, recycle gas compressor, E1101, absorption tower heater, E1201, second recycle condenser, E1202, first recycle condenser, E1203, acid water cooler, E1301, solvent heat exchanger, E1401, regeneration tower reboiler, S1101, acrylic acid absorption section, S1201, first recycle condensation section, S1202, acrylic acid purification section, S1203, acetic acid purification section, S1204, second recycle condensation section, T110, absorption tower, T120, light component removal tower, T130, extraction tower, T140, solvent regeneration tower.
Detailed Description
The technical solution of the present invention is further specifically described below by way of specific examples in conjunction with the accompanying drawings. It is to be understood that the invention is not limited to the following examples, and that any changes and/or modifications may be made to the invention as described herein.
In the present invention, all parts and percentages are by weight, unless otherwise specified, and the equipment and materials used are commercially available or commonly used in the art. The methods in the following examples are conventional in the art unless otherwise specified. The components or devices in the following examples are, unless otherwise specified, standard parts or parts known to those skilled in the art, the structure and principle of which are known to those skilled in the art through technical manuals or through routine experimentation.
The invention relates to a device and a method for effectively reducing the content of acetic acid in an absorption tower for producing concentrated acrylic acid solution by quenching and absorbing acrylic acid reaction gas, which are applied to various quenching, absorbing and concentrating process processes which take crude acrylic acid reaction gas as raw materials. The raw material crude acrylic acid reaction gas mentioned in the device and the method of the invention comprises the following typical components (by mass percent): 69.5780% nitrogen, 0.5273% carbon monoxide, 4.9466% oxygen, 2.1208% carbon dioxide, 0.1472% propylene, 0.0050% ethylene, 0.0635% propane, 0.0050% butane, 0.2392% formaldehyde, 0.0020% acetaldehyde, 0.0508% acrolein, 0.0010% acetone, 7.5233% water, 0.2515% acetic acid, 14.4267% acrylic acid, 0.0956% maleic anhydride, 0.0005% propionic acid, 0.0017% benzoic acid, 0.0035% furfural, 0.0108% crotonic acid.
Example 1:
an apparatus for producing high-quality acrylic acid, as shown in FIG. 1, comprises an absorption column T110, a lightness-removing column T120, an extraction column T130 and a solvent regeneration column T140, which are connected in this order.
The top of the absorption tower T110 is provided with an absorption tower gas-phase material outlet 2 connected to the tower kettle of the light component removal tower T120, an acrylic acid absorption section S1101 is arranged in the absorption tower T110, an absorption tower heater E1101 is arranged outside the absorption tower T110, the absorption tower heater E1101 is connected with the lower part of the absorption tower T110, and the bottom of the absorption tower T110 is provided with a raw material crude acrylic acid reaction gas inlet 1 and a liquid-phase concentrated acrylic acid outlet 3.
The tower kettle of the lightness-removing tower T120 is provided with a lightness-removing tower liquid-phase material outlet 12 connected to the tower top of the absorption tower T110, and the lightness-removing tower T120 is internally provided with a first circulating condensation section S1201, an acrylic acid purification section S1202, an acetic acid purification section S1203 and a second circulating condensation section S1204 from bottom to top in sequence. A first circulation condenser E1202 is arranged outside the lightness-removing column T120, a hot side inlet of the first circulation condenser E1202 is connected to the bottom of the lightness-removing column T120, and a hot side outlet of the first circulation condenser E1202 is connected to the first circulation condensing section S1201 in the lightness-removing column T120. A second circulation condenser E1201 is arranged outside the lightness-removing column T120, the hot side inlet of the second circulation condenser E1201 is connected to the inside of the lightness-removing column T120 below the second circulation condensing section S1204, and the hot side outlet of the second circulation condenser E1201 is connected to the inside of the lightness-removing column T120 above the second circulation condensing section S1204. The bottom of the acrylic acid purification section S1202 is provided with a first wastewater extraction port 10 connected to the tower kettle of the extraction tower T130, an acid water cooler E1203 is arranged between the lightness-removing tower T120 and the extraction tower T130, and the first wastewater extraction port 10 is connected to the tower kettle of the extraction tower T130 through the acid water cooler E1203. The bottom of the acetic acid purification section S1203 is provided with a second wastewater extraction outlet 8. The top of the light component removal tower T120 is provided with a circulating gas compressor C1201, and the top of the light component removal tower T120 is provided with a light component removal tower gas-phase material outlet 4 connected to the circulating gas compressor C1201.
The top of the extraction tower T130 is provided with a raffinate phase outlet 13 connected to the acrylic acid purification section S1202, a solvent heat exchanger E1301 is arranged between the extraction tower T130 and the solvent regeneration tower T140, and the bottom of the extraction tower T130 is provided with an extract phase outlet 17 connected to the top of the solvent regeneration tower T140 through the solvent heat exchanger E1301.
The top of the solvent regeneration tower T140 is provided with a gas-phase material outlet 19 of the solvent regeneration tower connected to the lower part of the absorption tower T110, and the bottom of the solvent regeneration tower T140 is provided with a liquid-phase material outlet 20 of the solvent regeneration tower connected to the top of the extraction tower T130 through a solvent heat exchanger E1301. The outside of the solvent regenerator T140 is provided with a regenerator reboiler E1401, and the regenerator reboiler E1401 is connected to the lower part of the solvent regenerator T140.
Raw material crude acrylic acid reaction gas 1 enters the bottom of an absorption tower T110, gas-phase materials at the top of the absorption tower T110 enter a tower kettle of a lightness-removing tower T120 through a gas-phase material outlet 2 of the absorption tower, the lower part of the absorption tower T110 is heated by an absorption tower heater E1101, and liquid-phase materials at the tower kettle are taken as concentrated acrylic acid and are sent out of the device through a liquid-phase concentrated acrylic acid outlet 3 arranged at the bottom of the absorption tower T110.
The gas phase material at the top of the light component removal tower T120 is divided into two parts from a gas phase material outlet 4 of the light component removal tower to a circulating gas compressor C1201, one part is taken as circulating gas to be sent out of the device, and the other part enters the tower kettle of a solvent regeneration tower T140.
The raffinate phase at the top of the extraction tower T130 is divided into two streams, one stream enters the upper part of an acrylic acid purification section S1202 of the lightness-removing tower T120, and the other stream is mixed with the wastewater extracted from the lower side of an acetic acid purification section of the lightness-removing tower T120 and then is sent out of the device. The extraction phase at the bottom of the extraction tower T130 enters the top of the solvent regeneration tower T140 after being preheated by a solvent heat exchanger E1301.
The heat source used by the absorber heater E1101 and the regeneration tower reboiler E1401 can be fresh steam, heat conduction oil or material steam generated inside the system.
The cooling medium used in the second circulation condenser E1201, the first circulation condenser E1202, and the acid water cooler E1203 may be circulating water, chilled water, or another cooling medium such as a cold material generated inside the system.
The acrylic acid absorption section S1101, the first circulating condensation section S1201, the acrylic acid purification section S1202, the acetic acid purification section S1203 and the second circulating condensation section S1204 are respectively provided with a macroporous flow-through tower plate and a metal corrugated plate, and are matched with structured packing for combined use, so that the corresponding treatment effect is achieved.
A method for producing high-quality acrylic acid by adopting the device comprises the following steps:
(1) Raw material crude acrylic acid reaction gas enters the bottom of an absorption tower T110, gas phase materials at the top of the absorption tower T110 enter a tower kettle of a lightness-removing tower T120, liquid phase materials at the tower kettle of the absorption tower T110 serve as a concentrated acrylic acid discharge device, the operation pressure at the top of the absorption tower T110 is 101-200 kpa, the operation temperature at the top of the tower is 50-95 ℃, and the operation temperature at the tower kettle is 70-100 ℃;
(2) The gas phase material in the step (1) sequentially flows through a first circulating condensation section S1201, an acrylic acid purification section S1202, an acetic acid purification section S1203 and a second circulating condensation section S1204 in an absorption tower T110, the gas phase material at the top of a lightness-removing tower T120 is divided into two strands, one strand is taken as a circulating gas exhaust device, the other strand enters a subsequent solvent regeneration tower T140 tower kettle, a gas phase side line extraction burning waste gas exhaust device above the acrylic acid purification section S1202, side line extraction waste water below the acrylic acid purification section S1202 enters a subsequent extraction tower T130 tower kettle, the liquid phase material at the bottom of the lightness-removing tower T120 tower enters the top of the absorption tower T110, the operation pressure at the top of the lightness-removing tower T120 tower is 101-200 kPa, the operation temperature at the top of the absorption tower is 20-75 ℃, and the operation temperature at the bottom of the tower kettle is 40-90 ℃;
(3) An extraction tower T130 and a solvent regeneration tower T140 are arranged behind a lightness-removing tower T120, raffinate phase material at the top of the extraction tower T130 is divided into two streams, one stream enters an acrylic acid purification section S1202 of the lightness-removing tower T120, the other stream serves as a wastewater removal device, extract phase material at the bottom of the extraction tower T130 enters the top of the solvent regeneration tower T140, the operating pressure at the top of the extraction tower T130 is 101-200 kPa, the operating temperature at the top of the tower is 20-90 ℃, and the operating temperature at the bottom of the tower is 20-90 ℃;
(4) The gas phase at the top of the solvent regeneration tower T140 enters the lower part of the absorption tower T110, the liquid phase material at the bottom of the solvent regeneration tower T140 enters the top of the extraction tower T130, the operation pressure at the top of the solvent regeneration tower T140 is 101-200 kpa, the operation temperature at the top of the tower is 50-120 ℃, and the operation temperature at the bottom of the tower is 100-210 ℃.
In this example, the specific operating conditions for each column were as follows: the operation pressure at the top of the absorption tower T110 is 117kpa, the temperature at the top of the tower is 62 ℃, and the temperature in a tower kettle is 81 ℃; the operation pressure of the top of the lightness-removing column T120 is 114kpa, the temperature of the top of the column is 56 ℃, and the temperature of the bottom of the column is 62 ℃; the operation pressure at the top of the extraction tower T130 is 101kpa, the temperature at the top of the tower is 49 ℃, and the temperature at the bottom of the tower is 49 ℃; the operation pressure of the tower top of the solvent regeneration tower T140 is 130kpa, the tower top is 82 ℃, and the tower kettle is 180 ℃; the acrylic acid content of the concentrated acrylic acid solution at the bottom of the absorption tower T110 is 90 percent, and the acetic acid content is less than 3 percent.
The device and the method can effectively improve the quality of the acrylic acid product of the subsequent refining unit, and have extremely obvious economic benefit and wide application prospect.
Example 2:
the apparatus for producing high-quality acrylic acid shown in FIG. 2 is the same as that of example 1 except that:
the light component removal tower T120 is internally provided with a first circulating condensation section S1201, an acrylic acid purification section S1202 and a second circulating condensation section S1204 from bottom to top, and is not provided with an acetic acid purification section S1203 and a second wastewater extraction outlet 8. The wastewater is extracted from the lower side line of the second circulating condensation section S1204 of the lightness-removing column T120, cooled by the second circulating condenser E1201 and mixed with the residual wastewater at the top of the extraction column T130 and then sent out of the device.
Example 3:
the apparatus for producing high-quality acrylic acid shown in FIG. 3 is the same as that of example 1 except that:
a first circulation condensing section S1201, an acrylic acid purifying section S1202, a second circulation condensing section S1204 and an acetic acid purifying section S1203 are sequentially arranged in the lightness-removing column T120 from bottom to top, the acetic acid purifying section S1203 is arranged at the top of the column, the second circulation condensing section S1204 is arranged below the acetic acid purifying section S1203, and fresh process water is supplemented at the top of the lightness-removing column T120 to be used as an acetic acid absorption liquid. The wastewater is collected from the lower side line of the second circulating condensation section S1204 of the lightness-removing column T120, cooled by the second circulating condenser E1201 and mixed with the raffinate wastewater at the top of the extraction column T130, and then is sent out of the device.
Example 4:
the apparatus for producing high-quality acrylic acid shown in FIG. 4 is the same as that of example 1 except that:
an apparatus for producing high-quality acrylic acid includes an absorption column T110 and a light ends removal column T120 connected in this order without providing an extraction column T130 and a solvent regeneration column T140. The gas phase material at the top of the light component removal tower T120 is directly taken as recycle gas to be sent out of the device after being sent to a recycle gas compressor C1201 from a gas phase material outlet 4 of the light component removal tower.
Example 5:
the apparatus for producing high-quality acrylic acid shown in FIG. 5 is the same as that of example 4 except that:
the light component removal tower T120 is internally provided with a first circulating condensation section S1201, an acrylic acid purification section S1202 and a second circulating condensation section S1204 from bottom to top in sequence. The acetic acid purification section S1203 and the second wastewater production port 8 at the bottom thereof are not provided. And the side-draw liquid-phase material below the second circulating condensation section S1204 is cooled by a second circulation-removing condenser E1201 and then is sent out of the device as wastewater.
Example 6:
the apparatus for producing high-quality acrylic acid shown in FIG. 6 is the same as that of example 1 except that:
an acrylic acid purification section S1202, an acetic acid purification section S1203 and a second circulating condensation section S1204 are sequentially arranged in the lightness-removing column T120 from bottom to top. The first loop condenser section S1201 is not provided. The first wastewater production port 10 at the bottom of the acrylic acid purification section S1202 is not provided. Waste water extracted from a second waste water extraction port 8 at the bottom of the acetic acid purification section S1203 is divided into two streams, one stream of waste water is cooled by an acid water cooler E1203 and then enters a tower kettle of an extraction tower T130, and the other stream of waste water is mixed with raffinate at the top of the extraction tower T130 and then is used as a waste water discharge device.
Example 7:
an apparatus for producing high-quality acrylic acid as shown in FIG. 7 is the same as that of example 4 except that:
an acrylic acid purification section S1202, an acetic acid purification section S1203 and a second circulating condensation section S1204 are sequentially arranged in the lightness-removing column T120 from bottom to top. The first circulation condensation section S1201 and the first circulation condenser E1202 are not provided.
Example 8:
an apparatus for producing high-quality acrylic acid as shown in FIG. 8 is the same as that of example 1 except that:
the gas phase side line above the acrylic acid purification section S1202 is not provided with the extracted incineration waste gas, the gas phase material at the top of the light component removal tower T120 is extracted from a gas phase material outlet 4 of the light component removal tower and then divided into two parts, the first part is taken as an incineration waste gas delivery device, the second part is taken as a circulating gas compressor C1201 and then divided into two parts, one part is taken as a circulating gas delivery device, and the other part enters the tower kettle of the solvent regeneration tower T140.
Example 9:
an apparatus for producing high-quality acrylic acid as shown in FIG. 9 is similar to that of example 4 except that:
the gas phase side line above the acrylic acid purification section S1202 is not provided with the extracted incineration waste gas, the gas phase material at the top of the light component removal tower T120 is extracted from a gas phase material outlet 4 of the light component removal tower and then divided into two parts, one part is used as an incineration waste gas delivery device, and the other part is used as a circulating gas delivery device after being pressurized by a circulating gas compressor C1201.
Example 10:
an apparatus for producing high-quality acrylic acid as shown in FIG. 10 is the same as that of example 1 except that:
the first wastewater withdrawal port 10 at the bottom of the acrylic acid purification section S1202 is not provided. Waste water extracted from a second waste water extraction port 8 at the bottom of the acetic acid purification section S1203 is divided into two streams, one stream of waste water is cooled by an acid water cooler E1203 and then enters a tower kettle of an extraction tower T130, and the other stream of waste water is mixed with raffinate at the top of the extraction tower T130 and then is used as a waste water discharge device.
The above-described embodiment is a preferred embodiment of the present invention, and is not intended to limit the present invention in any way, and other variations and modifications may be made without departing from the spirit and scope of the invention as defined in the appended claims.
Claims (5)
1. An apparatus for producing high-quality acrylic acid, characterized in that: the device for producing the high-quality acrylic acid comprises an absorption tower (T110) and a light component removal tower (T120), wherein an absorption tower gas-phase material outlet (2) connected to a tower kettle of the light component removal tower (T120) is formed in the tower top of the absorption tower (T110), a light component removal tower liquid-phase material outlet (12) connected to the tower top of the absorption tower (T110) is formed in the tower kettle of the light component removal tower (T120), an acrylic acid absorption section (S1101) is arranged in the absorption tower (T110), an acrylic acid purification section (S1202) and a second circulating condensation section (S1204) are arranged in the light component removal tower (T120), a second circulating condenser (E1201) is arranged outside the light component removal tower (T120), a hot side inlet of the second circulating condenser (E1201) is connected to the lower part of the second circulating condensation section (S1204) in the light component removal tower (T120), and a hot side outlet of the second circulating condenser (E) is connected to the upper part of the second circulating condensation section (S1204) in the light component removal tower (T120);
a first circulating condensation section (S1201) is further arranged in the light component removal tower (T120), a first circulating condenser (E1202) is further arranged outside the light component removal tower (T120), a hot side inlet of the first circulating condenser (E1202) is connected to the bottom of the light component removal tower (T120), and a hot side outlet of the first circulating condenser (E1202) is connected to the first circulating condensation section (S1201) in the light component removal tower (T120);
an acetic acid purification section (S1203) is further arranged in the lightness-removing tower (T120), the acetic acid purification section (S1203) is arranged above the acrylic acid purification section (S1202), and a second wastewater extraction port (8) is arranged at the bottom of the acetic acid purification section (S1203);
the apparatus for producing high-quality acrylic acid further comprises an extraction column (T130) and a solvent regeneration column (T140); the top of the extraction tower (T130) is provided with a raffinate phase outlet (13) connected to the acrylic acid purification section (S1202), a solvent heat exchanger (E1301) is arranged between the extraction tower (T130) and the solvent regeneration tower (T140), and the bottom of the extraction tower (T130) is provided with an extract phase outlet (17) connected to the top of the solvent regeneration tower (T140) through the solvent heat exchanger (E1301); the tower top of the solvent regeneration tower (T140) is provided with a gas-phase material outlet (19) of the solvent regeneration tower connected to the lower part of the absorption tower (T110), and the tower kettle of the solvent regeneration tower (T140) is provided with a liquid-phase material outlet (20) of the solvent regeneration tower connected to the tower top of the extraction tower (T130) through a solvent heat exchanger (E1301);
the bottom of the acrylic acid purification section (S1202) is provided with a first wastewater extraction outlet (10) connected to a tower kettle of the extraction tower (T130), an acid water cooler (E1203) is arranged between the light component removal tower (T120) and the extraction tower (T130), the first wastewater extraction outlet (10) is connected to the tower kettle of the extraction tower (T130) through the acid water cooler (E1203), a regeneration tower reboiler (E1401) is arranged outside the solvent regeneration tower (T140), and the regeneration tower reboiler (E1401) is connected with the lower part of the solvent regeneration tower (T140).
2. An apparatus for producing high-quality acrylic acid according to claim 1, characterized in that: an absorption tower heater (E1101) is arranged outside the absorption tower (T110), the absorption tower heater (E1101) is connected with the lower part of the absorption tower (T110), and the bottom of the absorption tower (T110) is provided with a raw material crude acrylic acid reaction gas inlet (1) and a liquid phase concentrated acrylic acid outlet (3).
3. An apparatus for producing high-quality acrylic acid according to claim 1, characterized in that: a recycle gas compressor (C1201) is arranged outside the light component removal tower (T120), and a light component removal tower gas-phase material outlet (4) connected to the recycle gas compressor (C1201) is arranged at the top of the light component removal tower (T120).
4. The apparatus for producing high-quality acrylic acid according to claim 1, wherein: and the light component removal tower (T120) is provided with an incineration waste gas outlet on the acrylic acid purification section (S1202) or the top of the light component removal tower (T120).
5. A method for producing high-quality acrylic acid by the apparatus according to any one of claims 1 to 4, characterized in that: the method comprises in particular the following steps,
(1) Raw material crude acrylic acid reaction gas enters the bottom of an absorption tower (T110), gas phase materials at the top of the absorption tower (T110) enter a tower kettle of a light component removal tower (T120), liquid phase materials at the tower kettle of the absorption tower (T110) are taken as a concentrated acrylic acid discharge device, the operation pressure at the top of the absorption tower (T110) is 101-200 kpa, the operation temperature at the top of the tower is 50-95 ℃, and the operation temperature at the tower kettle is 70-100 ℃;
(2) The gas phase material in the step (1) sequentially flows through an acrylic acid purification section (S1202) and a second circulating condensation section (S1204) in an absorption tower (T110), the gas phase material at the top of the light component removal tower (T120) is divided into two parts, one part is taken as a circulating gas discharge device, the other part enters a subsequent tower kettle of a solvent regeneration tower (T140), a gas phase side line extraction burning waste gas discharge device above the acrylic acid purification section (S1202), side line extraction waste water below the acrylic acid purification section (S1202) enters a subsequent tower kettle of an extraction tower (T130), a liquid phase material at the tower kettle of the light component removal tower (T120) enters the top of the absorption tower (T110), the operation pressure at the top of the light component removal tower (T120) is 101-200 kPa, the operation temperature at the top of the extraction tower is 20-75 ℃, and the operation temperature at the tower kettle is 40-90 ℃;
(3) An extraction tower (T130) and a solvent regeneration tower (T140) are arranged behind the light component removal tower (T120), raffinate phase materials at the top of the extraction tower (T130) are divided into two streams, one stream enters an acrylic acid purification section (S1202) of the light component removal tower (T120), the other stream serves as a wastewater removal device, extract phase materials at the bottom of the extraction tower (T130) enter the top of the solvent regeneration tower (T140), the operating pressure at the top of the extraction tower (T130) is 101-200 kPa, the operating temperature at the top of the tower is 20-90 ℃, and the operating temperature at the bottom of the tower is 20-90 ℃;
(4) The gas phase at the top of the solvent regeneration tower (T140) enters the lower part of the absorption tower (T110), the liquid phase material at the bottom of the solvent regeneration tower (T140) enters the top of the extraction tower (T130), the operation pressure at the top of the solvent regeneration tower (T140) is 101-200 kpa, the operation temperature at the top of the tower is 50-120 ℃, and the operation temperature at the bottom of the tower is 100-210 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110400314.0A CN113214075B (en) | 2021-04-14 | 2021-04-14 | Device and method for producing high-quality acrylic acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110400314.0A CN113214075B (en) | 2021-04-14 | 2021-04-14 | Device and method for producing high-quality acrylic acid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN113214075A CN113214075A (en) | 2021-08-06 |
| CN113214075B true CN113214075B (en) | 2022-10-18 |
Family
ID=77087190
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110400314.0A Active CN113214075B (en) | 2021-04-14 | 2021-04-14 | Device and method for producing high-quality acrylic acid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113214075B (en) |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP5821672B2 (en) * | 2012-02-07 | 2015-11-24 | 三菱化学株式会社 | Acrylic acid production method |
| CN104470884B (en) * | 2012-08-03 | 2017-02-22 | Lg化学株式会社 | Method for continuously recovering (meth)acrylate, and recovery apparatus |
| CN102775295B (en) * | 2012-08-10 | 2015-07-01 | 上海华谊丙烯酸有限公司 | Method for purifying acrylic acid |
| CN103073414A (en) * | 2013-01-30 | 2013-05-01 | 天津大学 | Novel method and device for adsorbing and refining acrylic acid |
| CN109232232B (en) * | 2018-11-19 | 2021-06-22 | 平湖石化有限责任公司 | Refining method of acrylic acid |
-
2021
- 2021-04-14 CN CN202110400314.0A patent/CN113214075B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN113214075A (en) | 2021-08-06 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| SU831076A3 (en) | Method of ethylene oxide extraction from gas flow | |
| RU2525237C2 (en) | Improved method of ethylene oxide extraction | |
| CN111302899B (en) | Ammonia and tertiary butanol recovery device and method in cyclohexanone ammoximation production process | |
| CN102838096B (en) | Joint production method and production device of dilute nitric acid and concentrated nitric acid | |
| JP5393713B2 (en) | Method for producing (meth) acrylic acid | |
| CN1163465C (en) | Method for removing and treating by-products obtd. when producing acid or methacrylic acids | |
| CN109232232B (en) | Refining method of acrylic acid | |
| CN214972942U (en) | Composite tower for producing high-quality acrylic acid | |
| KR101052710B1 (en) | (Meth) acrylic acid purification method obtained by oxidation of base material | |
| CN102775295B (en) | Method for purifying acrylic acid | |
| CN113214075B (en) | Device and method for producing high-quality acrylic acid | |
| CN111995489B (en) | System and method for treating tail gas of ethylbenzene oxidation reaction | |
| CN214571621U (en) | Apparatus for producing high-quality acrylic acid | |
| CN109134217B (en) | Oxidation device and oxidation process improvement method in cyclohexanone production process by cyclohexane oxidation method | |
| WO2022237654A1 (en) | Method and system for refining acrylic acid | |
| CN211972183U (en) | Acetic anhydride production system | |
| CN110437064A (en) | A kind of differential pressure type energy-saving processing technique of ethyl acetate | |
| CN218146433U (en) | Energy-saving process device for acrylic acid refining process | |
| CN212102637U (en) | Ammonia and tert-butyl alcohol recovery device in cyclohexanone ammoximation production process | |
| CN219342049U (en) | Process device for dehydration and deacidification of acrylic acid aqueous solution | |
| CN202315640U (en) | Production and tail gas absorption device for phthalic anhydride | |
| CN112898148A (en) | Process and apparatus for refining glyoxylic acid | |
| CN112920018A (en) | Method for producing mixture of cyclohexanol and cyclohexanone by cyclohexane oxidation | |
| CN115433080A (en) | Energy-saving process method and device for acrylic acid refining process | |
| CN218834038U (en) | Novel acrylic acid reaction gas separation system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |