CN220237773U - Paramydehyde continuous film distillation plant - Google Patents
Paramydehyde continuous film distillation plant Download PDFInfo
- Publication number
- CN220237773U CN220237773U CN202321590807.6U CN202321590807U CN220237773U CN 220237773 U CN220237773 U CN 220237773U CN 202321590807 U CN202321590807 U CN 202321590807U CN 220237773 U CN220237773 U CN 220237773U
- Authority
- CN
- China
- Prior art keywords
- film evaporator
- thin film
- chlorobenzaldehyde
- condenser
- residual liquid
- 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
- 238000004821 distillation Methods 0.000 title claims abstract description 33
- 239000007788 liquid Substances 0.000 claims abstract description 105
- 239000010409 thin film Substances 0.000 claims abstract description 66
- AVPYQKSLYISFPO-UHFFFAOYSA-N 4-chlorobenzaldehyde Chemical compound ClC1=CC=C(C=O)C=C1 AVPYQKSLYISFPO-UHFFFAOYSA-N 0.000 claims abstract description 56
- 239000010408 film Substances 0.000 claims abstract description 35
- 239000000413 hydrolysate Substances 0.000 claims abstract description 11
- 230000009194 climbing Effects 0.000 claims abstract description 8
- 150000001299 aldehydes Chemical class 0.000 claims description 8
- 239000000047 product Substances 0.000 abstract description 13
- 239000000463 material Substances 0.000 abstract description 12
- 230000005484 gravity Effects 0.000 abstract description 9
- 238000010438 heat treatment Methods 0.000 abstract description 3
- 238000002309 gasification Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 15
- 238000000034 method Methods 0.000 description 9
- 230000000630 rising effect Effects 0.000 description 7
- 239000000243 solution Substances 0.000 description 4
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 3
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000000575 pesticide Substances 0.000 description 3
- JUJWROOIHBZHMG-UHFFFAOYSA-N Pyridine Chemical compound C1=CC=NC=C1 JUJWROOIHBZHMG-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 229940079593 drug Drugs 0.000 description 2
- 239000000975 dye Substances 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- ZWJINEZUASEZBH-UHFFFAOYSA-N fenamic acid Chemical compound OC(=O)C1=CC=CC=C1NC1=CC=CC=C1 ZWJINEZUASEZBH-UHFFFAOYSA-N 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- YNWVFADWVLCOPU-MDWZMJQESA-N (1E)-1-(4-chlorophenyl)-4,4-dimethyl-2-(1H-1,2,4-triazol-1-yl)pent-1-en-3-ol Chemical compound C1=NC=NN1/C(C(O)C(C)(C)C)=C/C1=CC=C(Cl)C=C1 YNWVFADWVLCOPU-MDWZMJQESA-N 0.000 description 1
- RMOGWMIKYWRTKW-UONOGXRCSA-N (S,S)-paclobutrazol Chemical compound C([C@@H]([C@@H](O)C(C)(C)C)N1N=CN=C1)C1=CC=C(Cl)C=C1 RMOGWMIKYWRTKW-UONOGXRCSA-N 0.000 description 1
- DKIDEFUBRARXTE-UHFFFAOYSA-N 3-mercaptopropanoic acid Chemical compound OC(=O)CCS DKIDEFUBRARXTE-UHFFFAOYSA-N 0.000 description 1
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- SGHZXLIDFTYFHQ-UHFFFAOYSA-L Brilliant Blue Chemical compound [Na+].[Na+].C=1C=C(C(=C2C=CC(C=C2)=[N+](CC)CC=2C=C(C=CC=2)S([O-])(=O)=O)C=2C(=CC=CC=2)S([O-])(=O)=O)C=CC=1N(CC)CC1=CC=CC(S([O-])(=O)=O)=C1 SGHZXLIDFTYFHQ-UHFFFAOYSA-L 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 1
- 239000005985 Paclobutrazol Substances 0.000 description 1
- 239000005627 Triclopyr Substances 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- -1 amino-phenylaminobutyric acid Chemical compound 0.000 description 1
- 239000000908 ammonium hydroxide Substances 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 230000002363 herbicidal effect Effects 0.000 description 1
- 239000004009 herbicide Substances 0.000 description 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 239000011344 liquid material Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- UMJSCPRVCHMLSP-UHFFFAOYSA-N pyridine Natural products COC1=CC=CN=C1 UMJSCPRVCHMLSP-UHFFFAOYSA-N 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 150000007659 semicarbazones Chemical class 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- REEQLXCGVXDJSQ-UHFFFAOYSA-N trichlopyr Chemical compound OC(=O)COC1=NC(Cl)=C(Cl)C=C1Cl REEQLXCGVXDJSQ-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model relates to a distillation technology, and discloses a p-chlorobenzaldehyde continuous film distillation device. Materials in the p-chlorobenzaldehyde hydrolysate receiving tank are quantitatively transferred to the climbing film evaporator through the transfer pump to carry out negative pressure distillation, then the materials subjected to negative pressure distillation enter the gas-liquid separator to be separated, gas directly enters the condenser, liquid enters the thin film evaporator through gravity, heat conduction oil is introduced to carry out heating, gas phase temperature is controlled to be 130-160 ℃ during gasification (heat conduction oil inlet and outlet valves are controlled) and then passes through the first-stage thin film evaporator, distilled p-chlorobenzaldehyde gas enters the condensing pipe, non-distilled materials are transferred to the second-stage thin film evaporator through gravity to continue distillation, the heat conduction oil inlet and outlet valves are controlled to be at 140-160 ℃, distilled gas is condensed through the condenser, condensate p-chlorobenzaldehyde is finished to the p-aldehyde fine receiving tank, residual liquid enters the residual liquid receiving tank, and the thin film evaporator and the condenser are used, so that the purity of the p-chlorobenzaldehyde is improved, and the product quality is improved.
Description
Technical Field
The utility model relates to the technical field of distillation, in particular to a p-chlorobenzaldehyde continuous film distillation device.
Background
The molecular formula of the p-chlorobenzaldehyde is C7H5ClO, the relative molecular mass is 140.57, and the p-chlorobenzaldehyde is colorless or pale yellow crystal to granular, is easily dissolved in organic solvents such as ethanol, diethyl ether, acetone, benzene and the like, is an important fine chemical intermediate, and can be widely applied to pesticides and medicines. Dyes, etc. In the pesticide industry, p-chlorobenzaldehyde is used for synthesizing herbicide triclopyr powder, plant production regulator paclobutrazol, uniconazole and the like in pesticides. In the pharmaceutical industry, the p-chlorobenzaldehyde is condensed and cyclized with mercaptopropionic acid to prepare the fenamic acid, and the fenamic acid can also be synthesized into medicines such as amino-phenylaminobutyric acid. P-chlorobenzaldehyde is used in the dye industry for the synthesis of acid blue 7BF, acid brilliant blue 6B, and the like. In other aspects, the reaction of p-chlorobenzaldehyde with pyridine and ammonium hydroxide solutions to produce crystalline semicarbazones can be used to isolate and identify ketone or aldehyde species.
The existing method for purifying the p-chlorobenzaldehyde from the p-chlorobenzaldehyde aqueous solution has low purity, so that the product quality is low, and the energy consumption is high and the resource is wasted in the p-chlorobenzaldehyde purification process.
Disclosure of Invention
The application provides a continuous thin film distillation device for p-chlorobenzaldehyde, which solves the problems that impurities are not completely removed in the process of purifying p-chlorobenzaldehyde, the purity of the purified p-chlorobenzaldehyde is low, the quality of p-chlorobenzaldehyde products is low, the energy consumption is high in the process of purifying p-chlorobenzaldehyde, and resources are wasted.
The application provides a continuous thin film distillation plant of p-chlorobenzaldehyde, including climbing film evaporator, hydrolysate receiving tank, gas-liquid separator, thin film evaporator, first condenser and second condenser, climbing film evaporator with hydrolysate receiving tank with gas-liquid separator passes through the pipe connection respectively, gas-liquid separator passes through the feed liquor union coupling thin film evaporator, thin film evaporator with gas-liquid separator is connected through first outlet duct, second outlet duct and third outlet duct respectively first condenser's air inlet, first condenser with second condenser passes through fourth outlet duct and connects, first condenser with second condenser's gas outlet is connected with to aldehyde fine transfer groove through first drain pipe and second drain pipe respectively.
Preferably, the thin film evaporator comprises a primary thin film evaporator and a secondary thin film evaporator, the gas-liquid separator is connected with the primary thin film evaporator through a first liquid inlet pipe, and the primary thin film evaporator is connected with the secondary thin film evaporator through a second liquid inlet pipe.
Preferably, the rising film evaporator is provided with a steam inlet pipe and a steam outlet pipe.
Preferably, the primary thin film evaporator and the secondary thin film evaporator are respectively provided with a heat inlet heat conducting oil pipe and a heat outlet heat conducting oil pipe.
Preferably, the second-stage thin film evaporator is connected with a first residual liquid receiving tank and a second residual liquid receiving tank through a residual liquid outlet pipe, and the first residual liquid receiving tank and the second residual liquid receiving tank are respectively connected with a first residual liquid barrel and a second residual liquid barrel.
Preferably, temperature sensors are respectively arranged in the inner cavities of the primary thin film evaporator and the secondary thin film evaporator.
Preferably, liquid level sensors are respectively installed in the inner cavities of the first residual liquid receiving tank and the second residual liquid receiving tank.
According to the technical scheme, when the device is used, materials in the p-chlorobenzaldehyde hydrolysate receiving tank are quantitatively transferred to the climbing film evaporator through the transfer pump to carry out negative pressure distillation (the vacuum degree is more than or equal to 0.09 Mpa), then the materials subjected to negative pressure distillation enter the gas-liquid separator to be separated, gas directly enters the condenser, liquid enters the thin film evaporator through gravity, heat conduction oil is introduced to carry out heating, gas phase temperature is controlled to be 130-160 ℃ when the liquid is gasified (the heat conduction oil is controlled to enter and exit the valve) and pass through the first-stage thin film evaporator, distilled p-chlorobenzaldehyde gas enters the condensing pipe, non-distilled materials are transferred to the second-stage thin film evaporator through gravity to continue distillation, the heat conduction oil is controlled to enter and exit the valve to enable the temperature to be controlled to be 140-160 ℃, distilled gas is condensed through the condenser, condensate p-chlorobenzaldehyde finished product enters the p-aldehyde fine receiving tank, and residual liquid is removed from the residual liquid receiving tank.
Compared with the prior art, the utility model has the beneficial effects that:
1. the operation procedure of the utility model relies on the existing automation system to realize automatic control, thereby saving labor force and being safe and efficient.
2. The combination of the first-stage thin film evaporator, the second-stage thin film evaporator, the first condenser and the second condenser improves the purity of the p-chlorobenzaldehyde, thereby improving the product quality and having large productivity.
3. The use and recovery of steam and heat conducting oil not only achieves the test conditions, but also saves energy.
In summary, the use of the thin film evaporator and the condenser in the p-chlorobenzaldehyde continuous thin film distillation device improves the purity of the p-chlorobenzaldehyde, thereby improving the product quality, saving the energy, and realizing the automatic control by depending on the existing automatic system in the whole operation procedure, thereby saving the labor force, and being safe and efficient.
Drawings
For a clearer description of the technical solutions of the present application, the drawings that are necessary for the implementation will be briefly described, it being obvious to a person skilled in the art that other drawings can be obtained from these drawings without inventive effort.
Fig. 1 is a schematic structural diagram of a p-chlorobenzaldehyde continuous thin film distillation device provided by the utility model.
Reference numerals in the specific embodiments are as follows:
1. a rising film evaporator; 2. a hydrolysate receiving tank; 3. a gas-liquid separator; 4. a first liquid inlet pipe; 5. a first-stage thin film evaporator; 6. a second liquid inlet pipe; 7. a two-stage thin film evaporator; 8. a residual liquid outlet pipe; 9. a first raffinate receiving tank; 10. a first raffinate tank; 11. a second raffinate receiving tank; 12. a second raffinate tank; 13. a first air outlet pipe; 14. a second air outlet pipe; 15. a third air outlet pipe; 16. a first condenser; 17. a fourth air outlet pipe; 18. a second condenser; 19. a first liquid outlet pipe; 20. a second liquid outlet pipe; 21. a branch liquid outlet pipe; 22. a transfer tank for refined aldehyde; 23. a temperature sensor; 24. a liquid level sensor; 25. a steam inlet pipe; 26. a steam outlet pipe; 27. a heat conducting oil pipe is fed; 28. and (5) discharging the heat conducting oil pipe.
Detailed Description
In order to better understand the technical solutions in the present application, the following description will clearly and completely describe the technical solutions in the embodiments of the present application with reference to the accompanying drawings.
Referring to fig. 1, a continuous thin film distillation device for p-chlorobenzaldehyde is provided, the application aims to solve the problems that impurities are not completely removed in the process of purifying p-chlorobenzaldehyde, the purity of purified p-chlorobenzaldehyde is low, the quality of p-chlorobenzaldehyde products is low, the energy consumption is large in the process of purifying p-chlorobenzaldehyde, and resources are wasted, the continuous thin film distillation device for p-chlorobenzaldehyde is provided, the purity of p-chlorobenzaldehyde is improved, the product quality is improved, the energy is saved, the whole operation procedure depends on the existing automatic system, the automatic control is realized, the labor force is saved, and the device is safe and efficient. Specifically, a p-chlorobenzaldehyde continuous thin film distillation device comprises a climbing film evaporator 1, a hydrolysate receiving tank 2, a gas-liquid separator 3, a thin film evaporator, a first condenser 16 and a second condenser 18. The rising film evaporator 1 is respectively connected with the hydrolysate receiving tank 2 and the gas-liquid separator 3 through pipelines, the gas-liquid separator 3 is connected with the first condenser 16 through the first air outlet pipe 13, materials in the p-chlorobenzaldehyde hydrolysate receiving tank 2 are quantitatively transferred to the rising film evaporator 1 through the transfer pump to be subjected to negative pressure distillation (the vacuum degree is more than or equal to 0.09 Mpa), the rising film evaporator 1 is provided with the steam inlet pipe 25 and the steam outlet pipe 26, the introduced steam heats the rising film evaporator 1, hydrogen chloride is removed through evaporation, the residual materials after the negative pressure distillation enter the gas-liquid separator 3 to be separated, p-chlorobenzaldehyde gas directly enters the first condenser 16 through the first air outlet pipe 13 to be condensed, and liquid enters the film evaporator through gravity. The gas-liquid separator 3 is connected with the film evaporator through a liquid inlet pipe, the film evaporator comprises a first-stage film evaporator 5 and a second-stage film evaporator 7, the first-stage film evaporator 5 and the second-stage film evaporator 7 are respectively provided with a heat inlet oil pipe 27 and a heat outlet oil pipe 28, temperature sensors 23 are respectively arranged in the inner cavities of the first-stage film evaporator 5 and the second-stage film evaporator 7, the gas-liquid separator 3 is connected with the first-stage film evaporator 5 through a first liquid inlet pipe 4, liquid materials after gas-liquid separation enter the first-stage film evaporator 5 through gravity, the temperature is raised through heat conducting oil from the heat inlet oil pipe 27, and the gas phase temperature is controlled to be 130-160 ℃ through a heat conducting oil inlet valve and a heat outlet valve when the first-stage film evaporator 5 gasifies; the first-stage thin film evaporator 5 is connected with the second-stage thin film evaporator 7 through a second liquid inlet pipe 6, the first-stage thin film evaporator 5 and the second-stage thin film evaporator 7 are respectively connected with an air inlet of the first condenser 16 through a second air outlet pipe 14 and a third air outlet pipe 15, the first condenser 16 and the second condenser 18 are connected through a fourth air outlet pipe 17, p-chlorobenzaldehyde gas evaporated in the first-stage thin film evaporator 5 enters the first condenser 16 through the second air outlet pipe 14 to be condensed, materials which are not evaporated after the first-stage evaporation are transferred into the second-stage thin film evaporator 7 through the second liquid inlet pipe 6 by gravity to continue distillation, and heat conduction oil inlet and outlet valves on the second-stage thin film evaporator 7 are controlled to enable the temperature to be controlled at 140-160 ℃, and the evaporated p-chlorobenzaldehyde gas enters the first condenser 16 through the third air outlet pipe 15 to be condensed. The air outlets of the first condenser 16 and the second condenser 18 are respectively connected with an aldehyde fine transfer tank 22 through a first liquid outlet pipe 19, a second liquid outlet pipe 20 and a expenditure liquid pipe 21, condensate p-chlorobenzaldehyde finished products condensed in the first condenser 16 directly enter the aldehyde fine transfer tank 22 through the first liquid outlet pipe 19, p-chlorobenzaldehyde gas which is not completely cooled in the first condenser 16 enters the second condenser 18 through a fourth air outlet pipe 17 to be continuously condensed, condensate p-chlorobenzaldehyde finished products completely condensed by the second condenser 18 enter the aldehyde fine transfer tank 22 through the second liquid outlet pipe 20, and when the second liquid outlet pipe 20 needs to be overhauled, the condensate p-chlorobenzaldehyde finished products can enter the aldehyde fine transfer tank 22 through the expenditure liquid pipe 21. The combined use of the film evaporator and the condenser improves the purity of the p-chlorobenzaldehyde, thereby improving the product quality and having large productivity. The second-stage thin film evaporator 7 is connected with a first residual liquid receiving tank 9 and a second residual liquid receiving tank 11 through a residual liquid outlet pipe 8, liquid level sensors 24 are respectively arranged in the inner cavities of the first residual liquid receiving tank 9 and the second residual liquid receiving tank 11, the first residual liquid receiving tank 9 and the second residual liquid receiving tank 11 are respectively connected with a first residual liquid barrel 10 and a second residual liquid barrel 12, residual liquid obtained after primary distillation and secondary distillation enters the first residual liquid receiving tank 9 through the residual liquid outlet pipe 8, when the liquid level sensors in the inner cavities of the first residual liquid receiving tank 9 detect that the residual liquid reaches 80%, the valves entering the first residual liquid receiving tank 9 are controlled to be closed through an automatic system, the residual liquid enters the second residual liquid receiving tank 11 to continuously receive the residual liquid, and the residual liquid in the first residual liquid receiving tank 9 is transferred into the first residual liquid barrel to be subjected to high-temperature treatment; when the liquid level in the second residual liquid receiving tank 11 also reaches 80%, the valve entering the first residual liquid receiving tank 9 is opened to receive, the valve entering the second residual liquid receiving tank 11 is closed, and the residual liquid in the second residual liquid receiving tank 11 is also transferred into the second residual liquid barrel 12 to carry out high-temperature treatment. The whole operation procedure depends on the existing automatic system to realize automatic control, so that not only is labor saved, but also safety and high efficiency are realized.
According to the technical scheme, when the device is used, materials in the p-chlorobenzaldehyde hydrolysate receiving tank 2 are quantitatively transferred to the rising film evaporator 1 through the transfer pump to carry out negative pressure distillation (the vacuum degree is more than or equal to 0.09 Mpa), then the materials subjected to negative pressure distillation enter the gas-liquid separator 3 to be separated, gas directly enters the first condenser 16 and the second condenser 18 to be condensed, liquid enters the first-stage thin film evaporator 5 and the second-stage thin film evaporator 7 through gravity, heat conduction oil is used for heating, the gas phase temperature is controlled to be 130-160 ℃ when the vaporized heat conduction oil enters and exits through the first-stage thin film evaporator 5 (the control of the heat conduction oil entering and exits), the distilled p-chlorobenzaldehyde gas enters the first condenser 16, the non-distilled materials are continuously distilled through the gravity into the second-stage thin film evaporator 7, the control of the heat conduction oil entering and exits the control of the temperatures of 140-160 ℃, the distilled gas enters the first condenser 16 to be condensed, the p-chlorobenzaldehyde gas which is not completely cooled in the first condenser 16 continues to be condensed, the condensate p-chlorobenzaldehyde finished product enters the p-aldehyde refined transfer tank 22, and the residual liquid is removed through the first-stage thin film evaporator 5 and the second-stage thin film evaporator 7 and the first residual liquid receiving tank 11 after the residual liquid is received by the first-stage thin film evaporator 9.
Other embodiments of the present application will be apparent to those skilled in the art from consideration of the specification and practice of the application disclosed herein. This application is intended to cover any variations, uses, or adaptations of the application following, in general, the principles of the application and including such departures from the present disclosure as come within known or customary practice within the art to which the application pertains. It is intended that the specification and examples be considered as exemplary only, with a true scope of the application being indicated by the following claims.
It is to be understood that the present application is not limited to the precise arrangements and instrumentalities shown in the drawings, which have been described above, and that various modifications and changes may be effected without departing from the scope thereof. The above-described embodiments of the present application are not intended to limit the scope of the present application.
Claims (7)
1. A p-chlorobenzaldehyde continuous film distillation device is characterized in that: including climbing film evaporator (1), hydrolysate receiving tank (2), vapour and liquid separator (3), film evaporator, first condenser (16) and second condenser (18), climbing film evaporator (1) with hydrolysate receiving tank (2) with vapour and liquid separator (3) are respectively through the pipe connection, vapour and liquid separator (3) are connected through the feed liquor pipe film evaporator, film evaporator with vapour and liquid separator (3) are respectively through first outlet duct (13), second outlet duct (14) and third outlet duct (15) are connected with the air inlet of first condenser (16), first condenser (16) with second condenser (18) are connected through fourth outlet duct (17), first condenser (16) with the gas outlet of second condenser (18) are connected with through first drain pipe (19) and second drain pipe (20) respectively and are connected with to aldehyde exquisite transfer groove (22).
2. A p-chlorobenzaldehyde continuous thin film distillation apparatus as claimed in claim 1, wherein: the thin film evaporator comprises a first-stage thin film evaporator (5) and a second-stage thin film evaporator (7), wherein the gas-liquid separator (3) is connected with the first-stage thin film evaporator (5) through a first liquid inlet pipe (4), and the first-stage thin film evaporator (5) is connected with the second-stage thin film evaporator (7) through a second liquid inlet pipe (6).
3. A p-chlorobenzaldehyde continuous thin film distillation apparatus as claimed in claim 1, wherein: the climbing film evaporator (1) is provided with a steam inlet pipe (25) and a steam outlet pipe (26).
4. A p-chlorobenzaldehyde continuous thin film distillation apparatus as claimed in claim 2, wherein: and the primary thin film evaporator (5) and the secondary thin film evaporator (7) are respectively provided with a heat inlet heat conducting oil pipe (27) and a heat outlet heat conducting oil pipe (28).
5. A p-chlorobenzaldehyde continuous thin film distillation apparatus as claimed in claim 2, wherein: the secondary thin film evaporator (7) is connected with a first residual liquid receiving groove (9) and a second residual liquid receiving groove (11) through a residual liquid outlet pipe (8), and the first residual liquid receiving groove (9) and the second residual liquid receiving groove (11) are respectively connected with a first residual liquid barrel (10) and a second residual liquid barrel (12).
6. A p-chlorobenzaldehyde continuous thin film distillation apparatus as claimed in claim 2, wherein: temperature sensors (23) are respectively arranged in the inner cavities of the primary thin film evaporator (5) and the secondary thin film evaporator (7).
7. The p-chlorobenzaldehyde continuous thin film distillation apparatus as claimed in claim 5, wherein: and liquid level sensors (24) are respectively arranged in the inner cavities of the first residual liquid receiving groove (9) and the second residual liquid receiving groove (11).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321590807.6U CN220237773U (en) | 2023-06-21 | 2023-06-21 | Paramydehyde continuous film distillation plant |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321590807.6U CN220237773U (en) | 2023-06-21 | 2023-06-21 | Paramydehyde continuous film distillation plant |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220237773U true CN220237773U (en) | 2023-12-26 |
Family
ID=89234470
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321590807.6U Active CN220237773U (en) | 2023-06-21 | 2023-06-21 | Paramydehyde continuous film distillation plant |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220237773U (en) |
-
2023
- 2023-06-21 CN CN202321590807.6U patent/CN220237773U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2020155571A1 (en) | Separation and recycle system for water-containing organic waste liquid and organic solvent, and recycle method | |
| CN102512835A (en) | Multi-effect plate type rising film countercurrent evaporation concentration device and method thereof | |
| CN109369444A (en) | Dimethylformamide is from backheat distillation system and recovery method | |
| CN220237773U (en) | Paramydehyde continuous film distillation plant | |
| CN105732319B (en) | A kind of method for being thermally integrated transformation batch fractionating separation methanol-acetonitrile azeotropic mixture | |
| CN113307774B (en) | Method for recovering imidazole from imidazole hydrochloride wastewater | |
| EP4219407B1 (en) | System and method for improving water quality of dehydrating tower of purified terephthalic acid apparatus | |
| US7959766B2 (en) | Method for obtaining cyclododecatriene by evaporation | |
| CN214060377U (en) | System for recycling acetonitrile from cephalosporin medicine intermediate | |
| CN104844420A (en) | Continuous treatment process and device of neopentyl glycol condensed washing mother liquor | |
| CN114177852A (en) | Continuous esterification reaction system, production method of dimethyl adipate and application | |
| CN107256653B (en) | Ethyl acetate esterification-hydrolysis circulating equipment and use method thereof | |
| CN212560048U (en) | Economizer of cyclohexanol dehydrogenation reaction in cyclohexanone production process | |
| CN105217654B (en) | Alkylation waste sulfuric acid recycling treatment device and method | |
| CN103102369A (en) | Production method for diethyl ethanephosphonate | |
| CN110585994B (en) | Device and method for synthesizing 2-methoxy-3, 4-dihydropyran | |
| NO145949B (en) | PROCEDURE FOR MANUFACTURING UREA. | |
| JPH02273636A (en) | Production of concentrated solution of ethanol | |
| CN213643134U (en) | Refined naphthalene recovery unit | |
| CN111116486A (en) | Synthesis method of 5-nitrobenzimidazole ketone | |
| CN221245191U (en) | Phenyl succinic acid preparation facilities | |
| CN220989717U (en) | Organic pigment crude solvent recovery processing system | |
| CN220531232U (en) | Ethanol membrane separation dehydration purification device | |
| CN220443807U (en) | Intermittent production system for 3-methoxy-N, N-dimethyl propionamide | |
| CN211987148U (en) | Fractionating device for mixed acid of phosphoric acid, acetic acid and nitric acid |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CP03 | Change of name, title or address | ||
| CP03 | Change of name, title or address |
Address after: 750001 North of Qide Road, West of Shazhu Road, South of Qijian Road, New Material Park, Ningxia Ningdong Energy and Chemical Base, Lingwu City, Yinchuan City, Ningxia Hui Autonomous Region Patentee after: Ningxia Jianpai Agrochemical Technology Co.,Ltd. Country or region after: China Address before: 750000 New Materials Park, Ningdong Energy and Chemical Base, Lingwu City, Yinchuan City, Ningxia Hui Autonomous Region, North Side of Qide Road, West Side of Shazhu Road, South Side of Qijian Road Patentee before: Ningxia sulongda Chemical Co.,Ltd. Country or region before: China |