CN112441905A - Process for preparing acrylic acid by propylene oxidation - Google Patents
Process for preparing acrylic acid by propylene oxidation Download PDFInfo
- Publication number
- CN112441905A CN112441905A CN201910845408.1A CN201910845408A CN112441905A CN 112441905 A CN112441905 A CN 112441905A CN 201910845408 A CN201910845408 A CN 201910845408A CN 112441905 A CN112441905 A CN 112441905A
- Authority
- CN
- China
- Prior art keywords
- acrylic acid
- material flow
- water vapor
- gas
- propylene
- 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.)
- Pending
Links
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 title claims abstract description 40
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 title claims abstract description 40
- NIXOWILDQLNWCW-UHFFFAOYSA-N 2-Propenoic acid Natural products OC(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 title claims abstract description 37
- SMZOUWXMTYCWNB-UHFFFAOYSA-N 2-(2-methoxy-5-methylphenyl)ethanamine Chemical compound COC1=CC=C(C)C=C1CCN SMZOUWXMTYCWNB-UHFFFAOYSA-N 0.000 title claims abstract description 36
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 29
- 230000003647 oxidation Effects 0.000 title claims abstract description 28
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 19
- 239000007789 gas Substances 0.000 claims abstract description 70
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 62
- 239000000463 material Substances 0.000 claims abstract description 32
- 238000006243 chemical reaction Methods 0.000 claims abstract description 29
- 238000000034 method Methods 0.000 claims abstract description 23
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 18
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 18
- 239000001301 oxygen Substances 0.000 claims abstract description 18
- 239000002994 raw material Substances 0.000 claims abstract description 18
- HGINCPLSRVDWNT-UHFFFAOYSA-N Acrolein Chemical compound C=CC=O HGINCPLSRVDWNT-UHFFFAOYSA-N 0.000 claims abstract description 14
- 230000008569 process Effects 0.000 claims abstract description 11
- 238000007670 refining Methods 0.000 claims abstract description 9
- 239000000203 mixture Substances 0.000 claims abstract description 8
- 238000010521 absorption reaction Methods 0.000 claims abstract description 6
- 239000007791 liquid phase Substances 0.000 claims abstract description 4
- 239000012071 phase Substances 0.000 claims abstract description 4
- 230000001590 oxidative effect Effects 0.000 claims description 11
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 claims description 6
- LPXPTNMVRIOKMN-UHFFFAOYSA-M sodium nitrite Chemical compound [Na+].[O-]N=O LPXPTNMVRIOKMN-UHFFFAOYSA-M 0.000 claims description 6
- 239000004323 potassium nitrate Substances 0.000 claims description 3
- 235000010333 potassium nitrate Nutrition 0.000 claims description 3
- 150000003839 salts Chemical class 0.000 claims description 3
- 235000010288 sodium nitrite Nutrition 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 8
- 239000003054 catalyst Substances 0.000 description 7
- 239000007795 chemical reaction product Substances 0.000 description 5
- 230000009471 action Effects 0.000 description 4
- 238000003795 desorption Methods 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- 229910001882 dioxygen Inorganic materials 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 239000013067 intermediate product Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- JCGCKSUCGVTMNB-UHFFFAOYSA-N acetic acid;formaldehyde Chemical compound O=C.CC(O)=O JCGCKSUCGVTMNB-UHFFFAOYSA-N 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- XENVCRGQTABGKY-ZHACJKMWSA-N chlorohydrin Chemical compound CC#CC#CC#CC#C\C=C\C(Cl)CO XENVCRGQTABGKY-ZHACJKMWSA-N 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- CCGKOQOJPYTBIH-UHFFFAOYSA-N ethenone Chemical compound C=C=O CCGKOQOJPYTBIH-UHFFFAOYSA-N 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- WOFDVDFSGLBFAC-UHFFFAOYSA-N lactonitrile Chemical compound CC(O)C#N WOFDVDFSGLBFAC-UHFFFAOYSA-N 0.000 description 1
- 238000011031 large-scale manufacturing process Methods 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
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
- C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
- C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
- C07C51/23—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of oxygen-containing groups to carboxyl groups
- C07C51/235—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of oxygen-containing groups to carboxyl groups of —CHO groups or primary alcohol groups
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/27—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation
- C07C45/32—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen
- C07C45/33—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties
- C07C45/34—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties in unsaturated compounds
- C07C45/35—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties in unsaturated compounds in propene or isobutene
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a process method for preparing acrylic acid by propylene oxidation, which comprises the following steps: s1, feeding raw material gas comprising oxygen-containing atmosphere, propylene and water vapor to a first oxidation reactor to generate a first material flow containing acrolein; s2, mixing the first material flow with an oxygen-containing atmosphere again, and sending the mixture to a second oxidation reactor to generate a second material flow containing acrylic acid; s3, sending the second material flow to an absorption tower to obtain a third material flow containing acrylic acid and in a liquid phase and a fourth material flow in a gas phase; and S4, sending the third material flow to an acrylic acid refining unit for refining, sending the fourth material flow to an incineration unit for treatment to generate tail gas containing water vapor, and mixing a part of the tail gas with the raw material gas. The circulating tail gas contains a certain amount of water vapor, so that the proportion of the circulating tail gas and the added water vapor is properly controlled, the proper proportion of water and propylene is adjusted, the reaction selectivity is favorably enhanced, and meanwhile, the energy consumption and the production cost of the device are favorably reduced.
Description
Technical Field
The invention relates to the field of chemical industry, in particular to a process method for preparing acrylic acid by oxidizing propylene.
Background
Acrylic acid is a very important chemical raw material, and can be used for producing acrylic esters, high-performance water-absorbent resins, daily chemical additives and the like. The industrial production of acrylic acid has gone through a number of stages, and early production methods include a chlorohydrin method, a cyanoethanol method, a high-pressure Reppe method, a ketene method, a modified Reppe method, a formaldehyde-acetic acid method, a propylene hydrolysis method, an ethylene method, and the like, and the currently mainstream production method is a propylene oxidation method. The oxidation of propylene to produce acrylic acid is divided into a one-step oxidation process and a two-step oxidation process.
The two-step oxidation process is currently used industrially. The two-step oxidation process comprises: the first step is that propylene is oxidized to generate acrolein under the action of air and a catalyst, and the second step is that the acrolein is further oxidized to generate acrylic acid under the action of air and a catalyst. The mixed gas entering the first reactor should contain a certain amount of water vapor, and the water vapor is also indispensable for playing the role. Because the water vapor has larger specific heat capacity, the reaction heat can be effectively removed and taken out of the reactor; and flammable gases such as propylene and the like can be diluted, so that the reaction is prevented from being carried out in an explosion area. In the traditional production process, water vapor is supplied from the outside, the use amount is large, the storage is not easy, and the production cost of acrylic acid is increased.
Disclosure of Invention
The invention aims to provide a process method for preparing acrylic acid by oxidizing propylene, which reduces the production cost of the acrylic acid.
In order to achieve the above object, the present invention provides a process for preparing acrylic acid by oxidizing propylene, comprising:
s1, feeding raw material gas comprising oxygen-containing atmosphere, propylene and water vapor to a first oxidation reactor to generate a first material flow containing acrolein;
s2, mixing the first material flow with an oxygen-containing atmosphere again, and sending the mixture to a second oxidation reactor to generate a second material flow containing acrylic acid;
s3, sending the second material flow to an absorption tower to obtain a third material flow containing acrylic acid and in a liquid phase and a fourth material flow in a gas phase;
and S4, sending the third material flow to an acrylic acid refining unit for refining, sending the fourth material flow to an incineration unit for treatment to generate tail gas containing water vapor, and mixing a part of the tail gas with the raw material gas.
According to an aspect of the present invention, in the step S4, the temperature of the tail gas mixed with the raw material gas is 100 to 200 ℃.
According to one aspect of the invention, in the step S4, the content of water vapor in the tail gas mixed with the raw material gas is 8-40% of the total amount of water vapor participating in the reaction in the first oxidation reactor.
According to an aspect of the present invention, in step S1, the ratio of the water vapor to the propylene content in the feed gas is 0.8 to 2.0.
According to one aspect of the invention, the proportion of water vapour in the first oxidation reactor is between 5% and 20% of all gases.
According to one aspect of the invention, the oxygen-containing atmosphere is oxygen or air.
According to one aspect of the invention, the exothermic heat of reaction in the first reactor is carried out of the reactor by a molten salt consisting of sodium nitrite and potassium nitrate.
According to one aspect of the invention, in step S2, the first stream is cooled and then mixed again with an oxygen containing atmosphere.
According to one scheme of the invention, the content of the water vapor in the initial reaction process is set to be in the range, so that the normal operation of the reaction can be effectively ensured. In addition, through the arrangement, the desorption of the reaction product at the active site of the catalyst by the water vapor can be effectively ensured, so that the reaction process is accelerated, and the reaction selectivity is improved. Therefore, it is advantageous to properly control the water vapor content so that the ratio of water to propylene is as described above to enhance the reaction selectivity and to reduce the energy consumption of the apparatus.
According to one scheme of the invention, the temperature of the tail gas is controlled within the range, so that the moderate temperature of the water vapor in the tail gas is effectively ensured, particularly when the tail gas is added into the first reactor, the temperature of the water vapor is ensured to be favorable for ensuring the normal reaction, and the influence on reaction products due to the over-low or over-high temperature of the water vapor is avoided. In addition, the tail gas is controlled within the temperature range, so that the tail gas is prevented from being heated, the energy is saved, and the energy consumption and the production cost are reduced.
According to one embodiment of the invention, part of the offgas is recycled to the reactor as part of the feed gas composition. The circulating tail gas contains a certain amount of water vapor, so that the proportion of the circulating tail gas and the added water vapor is properly controlled, the proper proportion of water and propylene is adjusted, the reaction selectivity is favorably enhanced, and meanwhile, the energy consumption, the waste water discharge and the production cost of the device are reduced. Therefore, the water-olefin ratio is optimized to control the water vapor content in the circulating tail gas, and further the redundant water vapor content in the feed gas is controlled, so that energy conservation and emission reduction are necessary.
Drawings
FIG. 1 is a schematic flow diagram of a process for the oxidation of propylene to acrylic acid according to one 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.
As shown in FIG. 1, according to one embodiment of the present invention, a process for producing acrylic acid by oxidizing propylene comprises:
s1, feeding raw material gas comprising oxygen-containing atmosphere, propylene and water vapor to a first oxidation reactor to generate a first material flow containing acrolein;
s2, mixing the first material flow with an oxygen-containing atmosphere again, and sending the mixture to a second oxidation reactor to generate a second material flow containing acrylic acid;
s3, sending the second material flow to an absorption tower to obtain a third material flow containing acrylic acid and in a liquid phase and a fourth material flow in a gas phase;
and S4, sending the third material flow to an acrylic acid refining unit for refining, sending the fourth material flow to an incineration unit for treatment to generate tail gas containing water vapor, and mixing part of the tail gas with the raw material gas.
According to one embodiment of the invention, the molecular oxygen-containing atmosphere is compressed by an air compressor and fed into a feed mixer, where it is thoroughly mixed with a feed gas comprising superheated propylene and preheated water and fed into a first oxidation reactor, where propylene and oxygen are reacted under the action of a ring catalyst to form a first stream comprising acrolein. The heat released by the reaction is carried out of the reactor by the molten salt consisting of sodium nitrite and potassium nitrate. The first stream is in gaseous form and is cooled to a certain temperature in an outlet cooler of the first oxidation reactor before leaving the reactor. Then mixing the mixture with the atmosphere containing molecular oxygen again in the second mixer, and then feeding the mixture into a second oxidation reactor, and continuously carrying out selective oxidation reaction under the action of a two-stage spherical catalyst to generate a second stream containing acrylic acid. And cooling the product by a cooler, then feeding the product into an absorption tower, absorbing the second stream in the absorption tower to form a solution, sending the solution to an acrylic acid refining unit through the tower bottom, and directly carrying out catalytic incineration treatment on all the fourth stream which is not absorbed at the tower top. In the present embodiment, the content ratio of water vapor to propylene in the raw material gas is 0.8 to 2.0. In this embodiment, the ratio of the water vapor to the propylene in the raw material gas is controlled in the range of 0.8 to 2.0, and the conversion of propylene and the yield of intermediate products are remarkably improved, as shown in table 1 below.
TABLE 1
As can be seen from the above table, the ratio of the water vapor to the propylene in the feed gas was controlled in the range of 0.8 to 2.0, and the conversion of propylene and the yield of the intermediate product were maintained at high levels. Through the setting, the content of the water vapor in the initial reaction process is set to be within the range, and the normal operation of the reaction can be effectively ensured. In addition, through the arrangement, the desorption of the reaction product at the active site of the catalyst by the water vapor can be effectively ensured, so that the reaction process is accelerated, and the reaction selectivity is improved. Therefore, it is advantageous to properly control the water vapor content so that the ratio of water to propylene is as described above to enhance the reaction selectivity and to reduce the energy consumption of the apparatus.
According to one embodiment of the invention, after the fourth stream is incinerated into carbon dioxide, water and the like which reach the standard, one part is discharged to the atmosphere, the other part controls the content of water vapor, one part of tail gas with stable water vapor content is recycled to the mixer in front of the first reactor after being controlled to a certain temperature, and the water vapor in the tail gas enters the first reactor to be mixed with the raw material gas after being controlled to the optimal ratio, so that the cyclic utilization of the water vapor in the tail gas is realized. In the present embodiment, the temperature of the exhaust gas mixed with the raw material gas is 100 to 200 ℃. Through the arrangement, the temperature of the tail gas is controlled within the range, the moderate temperature of the water vapor in the tail gas is effectively ensured, particularly when the tail gas is added into a first reactor, the temperature of the water vapor is ensured to be favorable for ensuring the normal reaction, and the influence on reaction products caused by the over-low or over-high temperature of the water vapor is avoided. In addition, the tail gas is controlled within the temperature range, so that the tail gas is prevented from being heated, the energy is saved, and the energy consumption and the production cost are reduced.
According to one embodiment of the invention, the content of water vapor in the tail gas mixed with the raw material gas is 8-40% of the total amount of water vapor participating in the reaction in the first oxidation reactor. By the arrangement, part of tail gas is recycled to the reactor to be used as one part of the composition of the raw material gas. The circulating tail gas contains a certain amount of water vapor, so that the proportion of the circulating tail gas and the added water vapor is properly controlled, the proper proportion of water and propylene is adjusted, the reaction selectivity is favorably enhanced, and meanwhile, the energy consumption of the device is reduced, and the wastewater discharge is favorably reduced. Therefore, the water-olefin ratio is optimized to control the water vapor content in the circulating tail gas, and further the redundant water vapor content in the feed gas is controlled, so that energy conservation and emission reduction are necessary.
According to one embodiment of the invention, the proportion of water vapour in the first oxidation reactor is between 5% and 20% of the total gas. The content of the water vapor is set to be within the range, so that the normal reaction can be effectively ensured. In addition, through the arrangement, the desorption of the reaction product at the active site of the catalyst by the water vapor can be effectively ensured, so that the reaction process is accelerated, and the reaction selectivity is improved. Therefore, it is advantageous to properly control the water vapor content so that the ratio of water to propylene is as described above to enhance the reaction selectivity and to reduce the energy consumption of the apparatus.
According to one embodiment of the invention, the oxygen-containing atmosphere is oxygen or air. By using oxygen or air, it is convenient to obtain, has low cost, and is beneficial to the large-scale production of the process of the invention.
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 (8)
1. A process for preparing acrylic acid by oxidizing propylene comprises the following steps:
s1, feeding raw material gas comprising oxygen-containing atmosphere, propylene and water vapor to a first oxidation reactor to generate a first material flow containing acrolein;
s2, mixing the first material flow with an oxygen-containing atmosphere again, and sending the mixture to a second oxidation reactor to generate a second material flow containing acrylic acid;
s3, sending the second material flow to an absorption tower to obtain a third material flow containing acrylic acid and in a liquid phase and a fourth material flow in a gas phase;
and S4, sending the third material flow to an acrylic acid refining unit for refining, sending the fourth material flow to an incineration unit for treatment to generate tail gas containing water vapor, and mixing a part of the tail gas with the raw material gas.
2. The process for preparing acrylic acid by oxidizing propylene according to claim 1, wherein in step S4, the temperature of the tail gas mixed with the raw material gas is 100-200 ℃.
3. The process for preparing acrylic acid by oxidizing propylene according to claim 2, wherein in step S4, the content of water vapor in the tail gas mixed with the raw material gas is 8-40% of the total amount of water vapor participating in the reaction in the first oxidation reactor.
4. The process for preparing acrylic acid by oxidizing propylene according to claim 3, wherein in step S1, the ratio of water vapor to propylene in the feed gas is 0.8-2.0.
5. The process for preparing acrylic acid by oxidizing propylene according to claim 4, wherein the steam in said first oxidation reactor is 5% to 20% of the total gas.
6. The process for preparing acrylic acid by oxidizing propylene according to claim 5, wherein said oxygen-containing atmosphere is oxygen or air.
7. The process for preparing acrylic acid by oxidizing propylene according to claim 6, wherein the exothermic heat of reaction in said first reactor is carried out of the reactor by a molten salt comprising sodium nitrite and potassium nitrate.
8. The process for the oxidation of propylene to acrylic acid as claimed in claim 7, wherein in step S2, the first stream is cooled and then mixed again with an oxygen-containing atmosphere.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910845408.1A CN112441905A (en) | 2019-09-05 | 2019-09-05 | Process for preparing acrylic acid by propylene oxidation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910845408.1A CN112441905A (en) | 2019-09-05 | 2019-09-05 | Process for preparing acrylic acid by propylene oxidation |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN112441905A true CN112441905A (en) | 2021-03-05 |
Family
ID=74733597
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910845408.1A Pending CN112441905A (en) | 2019-09-05 | 2019-09-05 | Process for preparing acrylic acid by propylene oxidation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112441905A (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4031135A (en) * | 1974-07-31 | 1977-06-21 | Basf Aktiengesellschaft | Manufacture of acrylic acid by oxidation of propylene with oxygen-containing gases in two separate catalyst stages |
| US4147885A (en) * | 1976-03-11 | 1979-04-03 | Nippon Shokubai Kagaku Kogyo Co. Ltd. | Process for producing acrylic acid from propylene |
| CN101260032A (en) * | 2008-01-27 | 2008-09-10 | 中国石油集团工程设计有限责任公司东北分公司 | Modified technique for preparing acrylic acid by propylene two-step oxygenation method |
| CN105001072A (en) * | 2015-07-21 | 2015-10-28 | 中国化学赛鼎宁波工程有限公司 | Propylene-to-acrylic acid oxidation absorption system and method thereof |
| CN105461532A (en) * | 2015-11-26 | 2016-04-06 | 山东新和成氨基酸有限公司 | Clean production method for preparing acrolein and acrylic acid by propylene oxidation |
-
2019
- 2019-09-05 CN CN201910845408.1A patent/CN112441905A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4031135A (en) * | 1974-07-31 | 1977-06-21 | Basf Aktiengesellschaft | Manufacture of acrylic acid by oxidation of propylene with oxygen-containing gases in two separate catalyst stages |
| US4147885A (en) * | 1976-03-11 | 1979-04-03 | Nippon Shokubai Kagaku Kogyo Co. Ltd. | Process for producing acrylic acid from propylene |
| CN101260032A (en) * | 2008-01-27 | 2008-09-10 | 中国石油集团工程设计有限责任公司东北分公司 | Modified technique for preparing acrylic acid by propylene two-step oxygenation method |
| CN105001072A (en) * | 2015-07-21 | 2015-10-28 | 中国化学赛鼎宁波工程有限公司 | Propylene-to-acrylic acid oxidation absorption system and method thereof |
| CN105461532A (en) * | 2015-11-26 | 2016-04-06 | 山东新和成氨基酸有限公司 | Clean production method for preparing acrolein and acrylic acid by propylene oxidation |
Non-Patent Citations (2)
| Title |
|---|
| 吴立娟: "丙烯酸装置尾气循环工艺分析", 化工设计 * |
| 罗明陨 等: "尾气循环工艺在大型丙烯酸装置上的应用", 广州化工 * |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| KR100622167B1 (en) | High productivity process to produce maleic anhydride from n-butane | |
| CN105294414A (en) | Formaldehyde production system | |
| JP2020522530A (en) | System and process for co-producing dimethyl carbonate and ethylene glycol | |
| CN211837226U (en) | Oxidizing solution production equipment and flue gas denitration device | |
| US3927182A (en) | Process for making nitric acid by the ammonia oxidation-nitric oxide oxidation-water absorption method | |
| CN103193617A (en) | Tail gas circulating process in acrylic acid production by propane one-step method | |
| CN113996167B (en) | Process and device for purifying and recycling oxidation reaction tail gas | |
| CN105732342A (en) | Formaldehyde production method based on exhaust gas circulating process | |
| CN102336658B (en) | Production method of 3,5-dimethylbenzoic acid | |
| CN105731386A (en) | System for preparing sulfur from metallurgical off-gas | |
| CN101177369A (en) | Method for oxidation of benzene ring side chain containing electron-attracting groups by combination of ozone and nitric acid | |
| CN109400480B (en) | Method and equipment for preparing methyl nitrite | |
| CN112441905A (en) | Process for preparing acrylic acid by propylene oxidation | |
| CN106542993A (en) | The oxidation of one step of propane prepares acrylic acid system and method | |
| CN111116335B (en) | Process for preparing acrolein or methacrolein | |
| JPS60215644A (en) | Preparation of aqueous solution of formaldehyde | |
| TWI331145B (en) | ||
| CN111138266B (en) | Method and device for preparing acrylic acid or methacrylic acid | |
| CN102423720A (en) | Ionic liquid catalyst and method for catalytic oxidation and purification of hydrogen phosphide-containing tail gas therewith | |
| CN106745066A (en) | Produce, purify the safe technology and system of hydrogen cyanide | |
| CN105017008B (en) | A kind of continuous production acrylic acid of the step of propane one oxidation | |
| CN103877838B (en) | A kind of method for improving the nitric acid rate of recovery in Glucurolactone production | |
| CN114749110B (en) | Maleic anhydride production device and method for tail gas recycling | |
| CN113277924B (en) | Heat exchange system for propylene preparation | |
| RU2009996C1 (en) | Method of producing nitric acid |
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 | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20210305 |