CN113209657A - Double-partition reaction tower for inhibiting quaternary cascade side reaction and process thereof - Google Patents
Double-partition reaction tower for inhibiting quaternary cascade side reaction and process thereof Download PDFInfo
- Publication number
- CN113209657A CN113209657A CN202110501779.5A CN202110501779A CN113209657A CN 113209657 A CN113209657 A CN 113209657A CN 202110501779 A CN202110501779 A CN 202110501779A CN 113209657 A CN113209657 A CN 113209657A
- Authority
- CN
- China
- Prior art keywords
- reaction
- tower
- zone
- reactant
- double
- 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.)
- Granted
Links
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/009—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in combination with chemical reactions
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a double-bulkhead reaction tower for inhibiting quaternary cascade side reaction and a process thereof, wherein the reaction type is a main reaction
The side reaction is
The reaction and separation are carried out in a quaternary cascade reaction system in which reactants a and B are the lightest and heavier components, respectively, and main product C and by-product D are the lighter and heaviest components, respectively, which are reacted and separated using a double-walled reaction column. The process integrates one reactive distillation column and two conventional distillation columns in a traditional reactive distillation column sequence into one column, and divides the column into seven parts by two clapboards, so that the material energy between the seven parts is fully coupled. The method can greatly improve the selectivity and effectively avoid the back mixing phenomenon while obtaining the main product with high purity, thereby reducing the operationThe energy consumption is reduced, a large number of towers are saved, the equipment cost is reduced, and the economic performance is high.
Description
Technical Field
The invention belongs to the technical field of chemical reaction and separation, and particularly relates to a process for reacting and separating a quaternary cascade side reaction system by using a double-partition reaction tower.
Background
As a classical energy-saving technology, a reaction rectifying tower organically combines reaction operation and distillation operation, the reaction and separation processes are changed to be continuous, the balance of the reaction is pushed to move rightwards, the heat of the two processes is fully utilized to be coupled with substances, the reaction rate conversion rate of a reaction system is improved, a large amount of reaction energy consumption and equipment investment are saved, but the reaction rectifying tower is limited by the sequencing of the volatility of each component in the system during specific application. For a reaction system containing four components, Yupolitan et al, Taiwan, classifies it into six types according to their system-internal material volatility ranking. One is that the product is the lightest and heaviest, with reactants in between; secondly, the reactant is lightest and lighter, and the product is heavier and heaviest; thirdly, the reaction is heavier and heaviest, and the product is lighter and lightest; fourthly, the reactant is lightest and heavier, and the product is lighter and heaviest; fifthly, reactants are lighter and heaviest, and products are lightest and heavier; sixthly, the reactants are lightest and heaviest, with the product in between. When a reactive distillation column is used in a fourth reaction type with side reactions, the product of the main reaction is in the lighter position and the by-product is in the heaviest position, Yunjing et al provide a conventional reactive distillation column process in which the reaction section is arranged in the lower half of the reactive distillation column, the lightest reactant is fed from the bottom of the column, the heavier reactant is fed from the top of the column, and the bottoms are all reboiled and refluxed, with the reactants being withdrawn from the top of the column. This configuration reduces product purity by virtue of the fact that the top of the column is the only outlet and the light reactants are more volatile than the lighter main product, so that the withdrawal of the main product carries with it some light products that have not reacted to completion, and a small amount of by-products. In order to obtain a high-purity product, Yupolitan et al achieve the purpose of obtaining a high-purity product through reaction and separation by a series of pressure heating in a single tower, but the process has extremely high energy consumption, reduces the economic performance of a reaction rectifying tower, and obviously cannot be used as a conventional means for improving the defects. The conventional solution, which requires a conventional reactive distillation column sequence followed by two conventional distillation columns to obtain a high-quality product and uses an external loop to reflux unreacted materials and side reaction products to the reactive distillation column, brings about two problems: firstly, the multi-tower structure brings about the increase of energy consumption and equipment investment, and secondly, the back mixing phenomenon of substances in the conventional rectifying tower further causes extra energy consumption. These two points severely reduce the economic performance of using a reactive distillation column. There is a greater possibility of material to energy coupling between the multiple column systems of a conventional reactive distillation column sequence.
Disclosure of Invention
The invention provides a double-bulkhead reactive distillation tower structure and a process thereof in order to ensure that a reactive distillation tower obtains a high-purity main product and simultaneously improves the economic performance of the process as much as possible, based on the improvement of the sequence of the traditional reactive distillation tower, and the reactive distillation tower and the two conventional distillation towers are integrated in one tower and are separated by two clapboards, so that the material and energy coupling among all parts is enhanced, the conversion rate and the selectivity of a system are improved, the energy consumption is saved, and the equipment investment is reduced.
In order to achieve the purpose, the technical scheme of the invention is as follows:
the reaction tower with double partition walls for inhibiting quaternary cascade side reaction has the main reaction type
The side reaction is
The reaction and separation are carried out by using a quaternary cascade reaction system, wherein reactants A and B are the lightest and heavier components respectively, and a main product C and a byproduct D are the lighter and heaviest components, and the reaction and separation are carried out by using a double-bulkhead reaction rectifying tower. The double-partition reaction rectifying tower is of a single tower structure, and two reaction rectifying towers are vertically arranged in the single towerParallel staggered baffles, a first baffle is arranged in the left half part in the single tower and is connected with the bottom of the tower, and a second baffle is arranged in the middle area of the right half part in the single tower. The upper end position of the first partition plate is higher than the lower end position of the second partition plate. The tower body is divided into seven parts by two partition plates: the system comprises a reaction zone, a separation zone, a pre-rectification zone, a pre-stripping zone, a common rectification zone, a common stripping zone and a side draw zone.
The number of the plates on the left side and the right side of each partition plate is consistent.
Catalyst is placed on each tower plate at the lower half part of the reaction zone to form a reaction section.
A liquid phase separator is arranged above each partition wall in the tower.
The column is externally equipped with two reboilers, one condenser and three surge tanks. The bottom of the reaction zone is connected with a first reboiler by a pipeline through a first buffer tank, and the first reboiler is connected to the bottom of the reaction zone through a pipeline. The bottom of the common stripping area and a second reboiler are connected by a pipeline through a second buffer tank below the common stripping area, the second reboiler is connected to the bottom of the common stripping area through a pipeline, and the other pipeline is led out and connected to the upper part of the reaction section of the reaction area to form external circulation.
The top of the public rectification area is connected with the condenser through a third buffer tank by a pipeline. The condenser is connected to the top of the public rectification area through a pipeline, and another pipeline is led out and connected to a first buffer tank at the bottom of the reaction area to form external circulation.
Because the volatility of the two reactants is different, the reactant A is a vapor phase which rises after entering the distillation tower due to the highest volatility and then gathers at the top of the tower, the reactant B is a liquid phase which falls after entering the tower due to the lower volatility, in order to ensure that the two reactants are fully contacted, the lightest reactant A is fed from the first buffer tank at the bottom of the reaction zone, and the heavier reactant B is fed from the upper part of the reaction section of the reaction zone. After the reaction section is fully contacted, a lighter main product C and a heaviest byproduct D are generated, the lighter main product C and the heaviest byproduct D and the unreacted reactant A and the unreacted reactant B enter a vapor phase and then ascend, the lightest reactant A and a part of the main product C continuously ascend and enter a pre-rectification zone, and the rest substances enter a liquid phase and descend and enter a pre-stripping zone. After the reactant A and the main product C entering the pre-rectification zone reach the top, the reactant A continuously rises and is extracted from the top of the tower and externally circulated to be combined with the feed stream of the reactant A for feeding. The main product C descends into a side draw zone. After the reactant B, the by-product D and part of the main product C entering the pre-stripping zone reach the bottom, BD continues to descend and is extracted from the bottom of the tower, and the feed streams which externally circulate to the reactant B are combined to feed. The remaining main product C then becomes the ascending vapor entering the side draw zone. The upper and lower main product C material flows are converged in a side line extraction area and extracted at the maximum concentration position to obtain a high-purity main product C.
The technical scheme can obtain the following benefits and effects:
compared with the reaction process of the traditional reaction rectifying tower sequence structure, the reaction process of the double-partition reaction rectifying tower structure integrates three towers into a single tower, reduces one reboiler and two condensers, and saves a large amount of equipment investment; substances and energy among all parts are coupled to the maximum degree, and the back mixing phenomenon is avoided, so that the operation energy consumption is reduced; the by-product flows back to the reaction section from the outside, so that the side reaction can be inhibited, and the selectivity of the system can be improved. By integrating the above steps, the reaction process of the double-bulkhead reaction rectifying tower structure can improve the economic performance of the process while obtaining the high-purity main product.
Drawings
FIG. 1 is a schematic diagram of a reaction separation process of a conventional reaction rectification column sequence structure;
FIG. 1 is a schematic diagram of a conventional reactive distillation column I; II is a first conventional distillation column; and III is a second conventional rectifying tower.
FIG. 2 is a schematic diagram of a reaction process of a double bulkhead reactive distillation column of the present invention:
FIG. 2 shows a reaction zone at 1; 2 is a separation zone; 3 is a pre-rectification zone; 4 is a pre-stripping zone; 5 is a public rectifying area; 6 is a public stripping area; 7 is a side draw zone; 8 is a first buffer tank; 9 is a second buffer tank; 10 is a third buffer tank; 11 is a first reboiler; 12 is a second reboiler; 13 is a condenser; 14 is a first partition plate; and 15 is a second partition plate.
Detailed Description
One central idea of the present invention is to provide a novel and practical structure of a double-bulkhead reactive distillation column and a process thereof.
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is described in further detail below with reference to specific embodiments and the accompanying drawings.
Example (c): the main reaction is carried out by utilizing the double-partition reaction rectifying tower structure of the invention
The side reaction is
The desired reaction system is reacted and separated.
The initial conditions were that the feed flow rates of both reactants a and B were 12.6mol/s, the reaction and separation processes were carried out in a column, the process requirements were that the purity of the main product was 95%, and the relative volatilities of the four species were a: c: b: d is 8: 4: 2: 1. the same conditions and requirements are compared with the sequence of the conventional reaction rectifying tower.
FIG. 1 shows the process with the best economic efficiency using a conventional reactive distillation column sequence, in which the number of plates of three columns is 29, 30 and 19, respectively, and the column diameters are 2.672m, 1.325m and 1.099m, respectively. The reaction section is 9 th to 29 th sections of the tower I. Reactant A was fed from the bottom of column I and reactant B was fed from tray 9 of column I. Both feed rates were 12.6 mol/s. The pressure at the top of the conventional rectifying tower is 2bar, and the pressure drop is 0.0068 bar.
A and B are fully contacted and reacted in the tower I to generate a lighter main product C and a heaviest byproduct D, the products C and D and partial unreacted reactants A and B are extracted from the top of the tower and enter a subsequent conventional tower for separation, the heavier reactant B and the heaviest byproduct D are extracted from the bottom of the tower II and are fed from a 9 th plate of C1 through an external circulation flow to continue to participate in the reaction and inhibit the side reaction. The lightest reactant A is extracted from the top of the tower III and fed to the bottom of the tower I through external circulation to continuously participate in the reaction. Finally 95% of the lighter main product C is withdrawn from the bottom of column III.
The reflux ratios of the three towers are respectively 4.61, 0.76 and 11.42, the reboiler powers are respectively 5360.46kw, 1401.95kw and 742.74kw, the total energy cost is 1533.57 $/year, the equipment cost is 1618.44 $/year and the total TAC is 3152.01 $/year.
FIG. 2 shows the process for optimizing the economic performance of a reactive distillation column using a double partition wall, which is a single column structure, wherein the column is divided into 7 parts by two partition walls. The number of the tower plates on the left side and the right side of each partition board is the same. The total plate number of the reaction zone 1 is 20; the total plate number of the separation area 2 is 9; the total plate number of the pre-rectifying area 3 is 5; the total number of plates in the pre-stripping zone 4 is 19; the total plate number of the public rectification area 5 is 9; the total plate number of the public stripping area 6 is 10; the total number of plates in the side offtake zone 7 was 26. The liquid phase separation ratio of the partition 14 was 0.76, and the liquid phase separation ratio of the partition 15 was 0.79. The lightest reactant a is fed from the bottom of reaction zone 1 and the heavier reactant B is fed from the top of reaction zone 1. Both feed rates were 12.6 mol/s. The pressure at the top of the column was 2bar and the pressure drop was 0.0068 bar.
A and B are fully contacted in a reaction zone to generate a lighter main product C and a heaviest byproduct D, the lighter main product C and the heaviest byproduct D and the unreacted four substances A and B enter a vapor phase and then rise, the lightest A and the lightest C continue to rise and enter a pre-rectification zone 3, and the rest substances enter a liquid phase and fall and enter a pre-stripping zone 4. After A and C entering the pre-rectification zone 3 reach the top, A continuously rises and is extracted from the top of the tower through a common rectification zone 5 and externally circulates to be combined with the feed stream of A to be fed. C then descends into the side draw zone 7. After entering B, D of pre-stripping section 4 and part of C reaching the bottom, BD continues to descend through common stripping section 6 to be withdrawn from the bottom of the column and combined in the feed stream that is externally recycled to B. The remainder of C becomes the ascending vapor entering the side draw zone 7. The upper and lower streams C are combined in a side draw zone 7 and are withdrawn at maximum concentration to yield 95% of a main product C.
The reflux ratio of the tower is 12.885, the reboiler power is 4388.32kw and 943.76kw respectively, the total energy cost is 1089.30 $/year, the equipment cost is 1233.30 $/year, and the total TAC is 2322.59 $/year.
Compared with the traditional reactive distillation column sequence process, the process using the double bulkhead reactive distillation column saves 26.31 percent of TAC, wherein the energy cost is 28.97 percent and the equipment investment cost is 23.77 percent.
The purpose, technical solution and beneficial effects of the invention are further explained by the above examples.
Claims (7)
1. Inhibit quaternary cascade side reaction's two next door reaction towers, its characterized in that: the double-partition reaction rectifying tower is of a single-tower structure, two parallel and staggered partition plates are vertically arranged in the single tower, the first partition plate is arranged in the left half part of the single tower and connected with the bottom of the single tower, and the second partition plate is arranged in the middle area of the right half part of the single tower; the upper end position of the first partition plate is higher than the lower end position of the second partition plate; the tower body is divided into seven parts by two partition plates: the system comprises a reaction zone, a separation zone, a pre-rectification zone, a pre-stripping zone, a common rectification zone, a common stripping zone and a side draw zone.
2. The double-walled reaction column for suppressing side reactions of the quaternary cascade of claim 1, wherein: the number of the plates on the left side and the right side of each partition plate is consistent.
3. The double-walled reaction column for suppressing side reactions of the quaternary cascade of claim 1, wherein: catalyst is placed on each tower plate at the lower half part of the reaction zone to form a reaction section.
4. The double-walled reaction column for suppressing side reactions of the quaternary cascade of claim 1, wherein: a liquid phase separator is arranged above each partition wall in the tower.
5. The double-walled reaction column for suppressing side reactions of the quaternary cascade of claim 1, wherein: the outside of the tower is provided with two reboilers, a condenser and three buffer tanks; the lower part of the reaction zone is connected with the bottom of the reaction zone and a first reboiler through a first buffer tank by a pipeline, and the first reboiler is connected with the bottom of the reaction zone through a pipeline; the bottom of the common stripping area and a second reboiler are connected by a pipeline through a second buffer tank below the common stripping area, the second reboiler is connected to the bottom of the common stripping area through a pipeline, and the other pipeline is led out and connected to the upper part of the reaction section of the reaction area to form external circulation.
6. The double-walled reaction column for suppressing side reactions of the quaternary cascade of claim 1, wherein: the top of the public rectification area is connected with the condenser through a third buffer tank by a pipeline; the condenser is connected to the top of the public rectification area through a pipeline, and another pipeline is led out and connected to a first buffer tank at the bottom of the reaction area to form external circulation.
7. The reaction process using the double-walled reaction column for suppressing the side reaction of the quaternary cascade as described in any one of claims 1 to 6, wherein: the reaction tower with double partition walls for inhibiting quaternary cascade side reaction has the main reaction type
The side reaction is
The reaction and separation are carried out in the quaternary cascade reaction system, wherein reactants A and B are the lightest and heavier components respectively, and a main product C and a byproduct D are the lighter and heaviest components, and are reacted and separated by using a double-bulkhead reaction rectifying tower; because the volatility of the two reactants is different, the reactant A is a vapor phase which rises after entering the distillation tower due to the highest volatility and then gathers at the top of the tower, the reactant B is a liquid phase which falls after entering the tower due to the lower volatility, and in order to ensure that the two reactants are separatedFully contacting, wherein the lightest reactant A is fed from a first buffer tank at the bottom of the reaction zone, and the heavier reactant B is fed from the upper part of the reaction section of the reaction zone; after the reaction section is fully contacted, a lighter main product C and a heaviest byproduct D are generated, the lighter main product C and the heaviest byproduct D and the unreacted reactant A and the unreacted reactant B enter a vapor phase and then rise, the lightest reactant A and a part of the main product C continue to rise and enter a pre-rectification zone, and the rest substances enter a liquid phase and fall and enter a pre-stripping zone; after the reactant A and the main product C entering the pre-rectification zone reach the top, the reactant A continuously rises and is extracted from the top of the tower, and the reactant A and the feed stream of the reactant A are combined and fed through external circulation; the main product C descends into a side draw-off zone; after the reactant B, the byproduct D and part of the main product C entering the pre-stripping area reach the bottom, the BD continuously descends and is extracted from the bottom of the tower, and the reactant B is combined and fed through the external circulation; the rest main product C becomes ascending steam and enters a side line extraction area; the upper and lower main product C material flows are converged in a side line extraction area and extracted at the maximum concentration position to obtain a high-purity main product C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110501779.5A CN113209657B (en) | 2021-05-08 | 2021-05-08 | Double-bulkhead reaction tower for inhibiting quaternary cascade side reaction and process thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110501779.5A CN113209657B (en) | 2021-05-08 | 2021-05-08 | Double-bulkhead reaction tower for inhibiting quaternary cascade side reaction and process thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN113209657A true CN113209657A (en) | 2021-08-06 |
| CN113209657B CN113209657B (en) | 2022-06-21 |
Family
ID=77093874
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110501779.5A Active CN113209657B (en) | 2021-05-08 | 2021-05-08 | Double-bulkhead reaction tower for inhibiting quaternary cascade side reaction and process thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113209657B (en) |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103664481A (en) * | 2013-11-11 | 2014-03-26 | 天津科林泰克科技有限公司 | Method for refining petrobenzene and thiophene by adopting double-partition-wall extraction rectifying tower |
| CN204447369U (en) * | 2015-02-17 | 2015-07-08 | 平湖石化有限责任公司 | A kind of tandem heater of acrylic acid dehydrating tower |
| US20170283350A1 (en) * | 2016-03-31 | 2017-10-05 | Uop Llc | Methods and apparatuses for phenol fractionation in a single dividing wall column |
| US20190091600A1 (en) * | 2017-09-28 | 2019-03-28 | Exxonmobil Research And Engineering Company | Dual-dividing wall column with multiple products |
| US20190330137A1 (en) * | 2016-12-21 | 2019-10-31 | Basf Se | Process for isolating pure tert-butyl (meth)acrylate from crude tert-butyl (meth)acrylate by distillation |
| CN111298471A (en) * | 2020-03-30 | 2020-06-19 | 吴嘉 | Dividing wall rectifying tower for separating complex multi-component system and rectifying method |
| CN112225680A (en) * | 2019-07-15 | 2021-01-15 | 中国石油化工股份有限公司 | Organic solvent purification method and device |
| CN112675564A (en) * | 2020-07-24 | 2021-04-20 | 天津科技大学 | Baffle rectifying tower for separating four products without gas phase separation |
-
2021
- 2021-05-08 CN CN202110501779.5A patent/CN113209657B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103664481A (en) * | 2013-11-11 | 2014-03-26 | 天津科林泰克科技有限公司 | Method for refining petrobenzene and thiophene by adopting double-partition-wall extraction rectifying tower |
| CN204447369U (en) * | 2015-02-17 | 2015-07-08 | 平湖石化有限责任公司 | A kind of tandem heater of acrylic acid dehydrating tower |
| US20170283350A1 (en) * | 2016-03-31 | 2017-10-05 | Uop Llc | Methods and apparatuses for phenol fractionation in a single dividing wall column |
| US20190330137A1 (en) * | 2016-12-21 | 2019-10-31 | Basf Se | Process for isolating pure tert-butyl (meth)acrylate from crude tert-butyl (meth)acrylate by distillation |
| US20190091600A1 (en) * | 2017-09-28 | 2019-03-28 | Exxonmobil Research And Engineering Company | Dual-dividing wall column with multiple products |
| CN112225680A (en) * | 2019-07-15 | 2021-01-15 | 中国石油化工股份有限公司 | Organic solvent purification method and device |
| CN111298471A (en) * | 2020-03-30 | 2020-06-19 | 吴嘉 | Dividing wall rectifying tower for separating complex multi-component system and rectifying method |
| CN112675564A (en) * | 2020-07-24 | 2021-04-20 | 天津科技大学 | Baffle rectifying tower for separating four products without gas phase separation |
Non-Patent Citations (2)
| Title |
|---|
| QIAN XING ET AL.: "Model predictive control of azeotropic dividing wall distillation column for separating furfural–water mixture", 《ISA TRANSACTIONS》 * |
| 顾克等: "一种新型双隔壁反应精馏塔及其性能", 《现代化工》 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN113209657B (en) | 2022-06-21 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US7399881B1 (en) | Transesterification process of methyl acetate | |
| CN101328119B (en) | Synthetic process of methyl acetate and apparatus thereof | |
| CN101244982A (en) | Hydrolyzation separation apparatus for methyl acetate and technique | |
| CN102188831B (en) | Reactive distillation method | |
| CN108059597B (en) | Method and device for producing ethyl acetate by integrating reactive distillation and pervaporation | |
| CN109678756A (en) | A kind of reaction unit producing adiponitrile and method | |
| CN102690185B (en) | For being hydrolyzed methyl acetate to obtain the reactive distillation method and apparatus of acetic acid and alcohol | |
| CN101306994A (en) | Technological process for producing high-purity methyl acetate and device | |
| CN101357887A (en) | Ethyl acetate synthetic process and apparatus thereof | |
| CN104529763A (en) | Process and device for synthesizing ethyl formate with reactive distillation dividing wall column | |
| JP2022164649A (en) | Process for energy-efficient production of alkali metal alkoxides | |
| CN102188830B (en) | Reaction distillation method | |
| CN105753649B (en) | A kind of method that isooctanol is reclaimed from the solvent slop of isooctyl thioglycolate production process | |
| CN107501093B (en) | Equipment and method for producing ethylene glycol diacetate by virtue of separation wall reaction rectifying tower | |
| CN113209657B (en) | Double-bulkhead reaction tower for inhibiting quaternary cascade side reaction and process thereof | |
| CN112110831B (en) | Method for synthesizing refined metolachlor-imine by heterogeneous catalytic reaction rectification | |
| CN107011172B (en) | A kind of method and device that vinyl acetate is refined using partition tower | |
| US10626097B2 (en) | Process for making hydroxyethyl piperazine compounds | |
| CN112441996B (en) | Process for preparing tetrahydrofuran | |
| CN102276452B (en) | Production equipment for sec-butyl acetate | |
| CN112657223B (en) | Reaction bulkhead rectifying tower for eliminating gas phase segmentation in formic acid production process | |
| CN113230685B (en) | Tower of two partition wall towers of two reaction section | |
| CN105968007A (en) | High-purity methyl acetate production process device and method | |
| JP3345985B2 (en) | Method for producing methyl methacrylate | |
| CN111349064B (en) | Process for rectifying and separating crude phthalic anhydride mixture by using dividing wall tower |
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 |