CN217612992U - Mixed butyraldehyde separation and purification device - Google Patents
Mixed butyraldehyde separation and purification device Download PDFInfo
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- CN217612992U CN217612992U CN202221707593.1U CN202221707593U CN217612992U CN 217612992 U CN217612992 U CN 217612992U CN 202221707593 U CN202221707593 U CN 202221707593U CN 217612992 U CN217612992 U CN 217612992U
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Abstract
The utility model relates to a separation and purification device of mixed butyraldehyde, which comprises a rectifying tower, wherein a mixed butyraldehyde feeding pipeline is arranged in the middle of the side wall of the rectifying tower, and a reboiler component is arranged at the bottom of the rectifying tower; the top of the rectifying tower is communicated with a reflux tank, an overhead condenser is arranged between the reflux tank and the rectifying tower, a separation assembly is arranged in the reflux tank, the reflux tank is respectively provided with a propylene and propane discharge pipeline, a water discharge pipeline and an isobutyraldehyde extraction pipeline, the isobutyraldehyde extraction pipeline is provided with a reflux pipeline communicated with the top of the rectifying tower, and the isobutyraldehyde extraction pipeline is provided with an isobutyraldehyde cooler; the middle lower part of the rectifying tower is communicated with a n-butyraldehyde buffer tank, the top of the n-butyraldehyde buffer tank is provided with a gas phase reflux pipeline, and the bottom of the n-butyraldehyde buffer tank is communicated with a n-butyraldehyde delivery pipeline; the bottom of the rectifying tower is communicated with an impurity delivery pipeline. The utility model discloses a mixed butyraldehyde of rectifying column and impurity are separated, obtain high-purity n-butyl aldehyde and isobutyraldehyde, have the beneficial effect that the energy consumption is low, with low costs.
Description
Technical Field
The utility model relates to a separation and purification device especially relates to a mix butyraldehyde's separation and purification device, belongs to and mixes butyraldehyde splitter technical field.
Background
Industrially, n-butyraldehyde and iso-butyraldehyde are mainly prepared by reacting carbon monoxide, hydrogen and propylene, and n-butyraldehyde and iso-butyraldehyde are mainly generated as by-products. The n-butyraldehyde and the isobutyraldehyde are isomers, and the boiling point of the n-butyraldehyde is 74 ℃ and the boiling point of the isobutyraldehyde is 64 ℃. The mixed butyraldehyde produced industrially needs to be separated. Because the boiling point is relatively close to the separation difficulty, the normal-butyl aldehyde and the isobutyraldehyde are relatively difficult to separate, and the mixed components generated in the industrial production are relatively complex and contain impurities such as water, propylene, propane, butyraldehyde trimer, n-butyl alcohol and the like. Two-tower or three-tower process is often needed in industry to obtain high-purity n-butyraldehyde and isobutyraldehyde, the investment is high, and the energy consumption is high.
In the prior art, CN104788302A discloses a method for separating n-butyraldehyde and iso-butyraldehyde, which comprises a butyraldehyde isomer tower, a first rectifying tower and a second rectifying tower, wherein the three towers are adopted for separating the n-butyraldehyde from the iso-butyraldehyde, the process is complex, and the operation difficulty is high; in the prior art, CN112299979A also discloses an isobutyraldehyde extraction method, which comprises a butyraldehyde isomer and an isobutyraldehyde rectifying tower, wherein the two towers are connected in series for operation, and the overall operation difficulty is still higher although the process is improved.
SUMMERY OF THE UTILITY MODEL
The utility model discloses mainly be to the mixed butyraldehyde separation difficulty that prior art exists, the energy consumption is high, problem with big costs, provide a mixed butyraldehyde's separation and purification device.
The purpose of the utility model is mainly realized by the following scheme:
the mixed butyraldehyde separation and purification device comprises a rectifying tower, wherein a mixed butyraldehyde feeding pipeline for conveying the mixed butyraldehyde is arranged in the middle of the side wall of the rectifying tower, and a reboiler component for heating materials in the rectifying tower is arranged at the bottom of the rectifying tower; the top of the rectifying tower is communicated with a reflux tank, an overhead condenser is arranged between the reflux tank and the rectifying tower, a separation assembly is arranged in the reflux tank, the reflux tank is respectively provided with a propylene discharge pipeline, a propane discharge pipeline, a water discharge pipeline and an isobutyraldehyde extraction pipeline, the isobutyraldehyde extraction pipeline is provided with a reflux pipeline communicated with the top of the rectifying tower, and an isobutyraldehyde cooler is arranged on the isobutyraldehyde extraction pipeline; the middle lower part of the rectifying tower is communicated with a n-butyraldehyde buffer tank, the top of the n-butyraldehyde buffer tank is communicated with the middle lower part of the rectifying tower through a gas phase reflux pipeline, and the bottom of the n-butyraldehyde buffer tank is communicated with a n-butyraldehyde delivery pipeline; the bottom of the rectifying tower is communicated with an impurity delivery pipeline.
Preferably, the rectifying tower adopts a float valve tower, the number of internal tower trays of the rectifying tower is 130-160 layers, the distance between adjacent tower trays is 300-500mm, the temperature range of a tower kettle of the rectifying tower is 90-110 ℃, the temperature range of a tower top of the rectifying tower is 50-80 ℃, and the pressure range of the tower top of the rectifying tower is 0.02-0.2Mpag.
Preferably, a feeding switching valve A and a feeding switching valve B which are communicated with the rectifying tower are respectively arranged on the mixed butyraldehyde feeding pipeline.
Preferably, an n-butyraldehyde extraction valve A and an n-butyraldehyde extraction valve B which are communicated with the rectifying tower are respectively arranged at the inlet of the n-butyraldehyde buffer tank.
Preferably, the reboiler assembly comprises a first reboiler and a second reboiler which are arranged on the rectifying tower, the inlets of the first reboiler and the second reboiler are connected with the material outlet at the bottom of the rectifying tower, and the outlets of the first reboiler and the second reboiler are connected with the tower kettle of the rectifying tower.
Preferably, the medium inlet of the first reboiler is communicated with the bottom of the low-pressure vapor condensate tank through a low-pressure condensate booster pump, the inlet of the low-pressure vapor condensate tank is communicated with the low-pressure vapor condensate pipeline, the medium outlet of the first reboiler is communicated with the inlet of the low-pressure vapor condensate tank through a low-low pressure vapor condensate pipeline a, and the outlet of the low-pressure vapor condensate tank is communicated with a low-low pressure vapor condensate delivery pipeline.
Preferably, the top of the low-pressure steam condensate tank is communicated with a medium inlet of a second reboiler through a low-pressure steam exhaust pipeline, and a medium outlet of the second reboiler is converged into a low-pressure steam condensate pipeline A through a low-pressure steam condensate pipeline B.
Preferably, the separation component comprises a coalescer and a baffle, a liquid inlet cylinder is arranged at an inlet at the top of the backflow tank, a guide plate and a mixing component are sequentially arranged in the liquid inlet cylinder from top to bottom, the coalescer and the baffle are horizontally arranged at intervals in the liquid return tank and divide the backflow tank into a feeding area, a drainage area and an isobutyraldehyde collecting area, the liquid inlet cylinder corresponds to the feeding area, an isobutyraldehyde extracting pipeline corresponds to the isobutyraldehyde collecting area, the bottom of the drainage area is communicated with a water drainage pipeline through a dewatering drum, and the top of the backflow tank is communicated with a propylene and propane drainage pipeline.
Preferably, said coalescer occupies the entire cross-section of the return tank, and the baffle occupies a part of the cross-section of the return tank.
Preferably, a wire mesh demister is further installed at a communication part between the reflux tank and the propylene and propane discharge pipeline.
Therefore, compared with the prior art, the utility model discloses possess following advantage: the utility model discloses a n-butyraldehyde is adopted to single platform plate rectifying column tower side line, the isobutyraldehyde is adopted in the top separation, obtain n-butyraldehyde and isobutyraldehyde, and with the water that is difficult to the desorption among the prior art, propylene, propane, butyraldehyde trimer, impurity desorption such as n-butanol, the n-butyraldehyde that obtains, isobutyraldehyde product purity is higher, the high temperature lime set that produces in the production of novelty carries out recycle in addition, the difficult problem of heat recovery utilization has been solved, low cost has, it is effectual and the energy consumption is low to mix butyraldehyde separation purification.
Drawings
Fig. 1 is a schematic structural diagram of the present invention;
FIG. 2 is a schematic flow diagram of the present invention;
fig. 3 is a schematic diagram of the internal structure of the middle reflux drum of the present invention.
Illustration of the drawings: 1-a rectifying tower, 2-a first reboiler, 3-a second reboiler, 4-an overhead condenser, 5-a reflux tank, 51-a liquid inlet cylinder, 52-a guide plate, 53-a mixing member, 54-a coalescer, 55-a baffle, 56-a dewatering drum, 57-a wire mesh demister, 6-an isobutyraldehyde cooler, 7-an n-butyraldehyde buffer tank, 8-a low-pressure vapor condensate tank, 9-a low-pressure vapor condensate tank, 10-a mixed butyraldehyde liquid inlet pipeline, 11-a feed switching valve A, 12-a feed switching valve B, 13-a low-pressure vapor condensate pipeline, 14-a low-pressure exhaust vapor pipeline, 15-a low-pressure condensate booster pump, 16-a low-pressure vapor condensate pipeline A, 17-a low-pressure vapor condensate delivery pipeline, 18-a reflux pipeline, 19-a water discharge pipeline, 20-an isobutyraldehyde production pipeline, 21-an n-butyraldehyde production valve A, 22-an n-butyraldehyde production valve B, 23-an n-butyraldehyde external delivery pipeline, 24-an impurity external delivery pipeline, 25-a low-pressure vapor discharge pipeline, 25-a low-pressure vapor condensate pipeline, 26-a propylene gas phase reflux pipeline, and a gas phase reflux pipeline.
Detailed Description
The technical solution of the present invention is further specifically described below by way of specific embodiments and with reference to the accompanying drawings. It is to be understood that the practice of the invention is not limited to the following examples, and that any modifications and/or changes in form made to the invention are intended to fall within the scope of the invention.
In the utility model, all parts and percentages are weight units, and the adopted equipment, raw materials and the like can be purchased from the market or commonly used in the field if not specified. The methods in the following examples are conventional in the art unless otherwise specified. Unless otherwise indicated, the components or devices in the following examples are all common standard components or components known to those skilled in the art, and their structures and principles can be known to those skilled in the art through technical manuals or through routine experimentation.
Example 1:
as shown in fig. 1, the utility model provides a technical solution, a separation and purification device for mixed butyraldehyde adopts a single tower to complete the separation of n-butyraldehyde and iso-butyraldehyde, the iso-butyraldehyde is extracted from the tower top, water, propylene and propane are removed, the n-butyraldehyde is extracted from the middle lower part of the tower, and impurities such as butyraldehyde trimer and n-butanol are removed in the tower kettle; the device comprises a rectifying tower 1, wherein a mixed butyraldehyde feeding pipeline 10 for conveying mixed butyraldehyde is arranged in the middle of the side wall of the rectifying tower 1, and a reboiler component for heating materials in the rectifying tower 1 is arranged at the bottom of the rectifying tower 1; the top of the rectifying tower 1 is communicated with a reflux tank 5, an overhead condenser 4 is arranged between the reflux tank 5 and the rectifying tower 1, the overhead condenser 4 is a vertical or horizontal condenser, the cooling mode is water cooling or air cooling, a separation component for separating isobutanol is arranged in the reflux tank 5, the reflux tank 5 is respectively provided with a propylene and propane discharge pipeline 26, a water discharge pipeline 19 and an isobutyraldehyde extraction pipeline 20, the isobutyraldehyde extraction pipeline 20 is provided with a reflux pipeline 18 communicated with the top of the rectifying tower 1, the isobutyraldehyde extraction pipeline 20 is provided with an isobutyraldehyde cooler 6, and the isobutyraldehyde cooler 6 adopts a U-shaped pipe cooler; the middle lower part of the rectifying tower 1 is communicated with a n-butyraldehyde buffer tank 7, the n-butyraldehyde buffer tank 7 adopts a vertical or horizontal storage tank, the top of the n-butyraldehyde buffer tank 7 is communicated with the middle lower part of the rectifying tower 1 through a gas phase reflux pipeline 27, and the bottom of the n-butyraldehyde buffer tank 7 is communicated with a n-butyraldehyde delivery pipeline 23; the bottom of the rectifying tower 1 is communicated with an impurity outward-conveying pipeline 24.
The rectifying tower 1 adopts a float valve tower, the number of tower trays in the rectifying tower 1 is 130-160 layers, the distance between adjacent tower trays is 300-500mm, the temperature range of a tower kettle of the rectifying tower 1 is 90-110 ℃, the temperature range of the top of the rectifying tower 1 is 50-80 ℃, and the pressure range of the top of the rectifying tower 1 is 0.02-0.2Mpag.
As shown in fig. 2, mixed butyraldehyde containing impurities enters the middle part of a rectifying tower 1 from a mixed butyraldehyde feeding pipeline 10, a plurality of temperature detection points are arranged in the rectifying tower 1 from top to bottom, the rectifying tower 1 heats materials through a reboiler assembly to generate rising steam, and the rising steam and reflux liquid perform heat transfer and mass transfer on a tower plate, so that isobutyraldehyde is gasified and enters a gas phase, and a n-butyraldehyde product enters a liquid phase; the gas phase of the isobutyraldehyde on the top of the tower is condensed by a condenser 4 on the top of the tower and then enters a reflux tank 5, water is discharged from a water discharge pipeline 19 and is discharged to a water treatment device under the separation action of a separation component, other light components such as propylene and propane contained in the mixed butyraldehyde are not condensed and are discharged through a propylene and propane discharge pipeline on the top of the reflux tank 5, the pure isobutyraldehyde obtained in the reflux tank 5 returns to the rectifying tower 1 through a reflux pipeline to be refluxed, and a small part of the isobutyraldehyde is taken as an isobutyraldehyde product and is extracted through an isobutyraldehyde extraction pipeline; pure n-butyraldehyde is extracted through a side line at the middle lower part of the tower, the side line extraction is positioned at the position of 5-10 layers of a tray at the bottom, the pure n-butyraldehyde enters a n-butyraldehyde buffer tank 7, a gas phase at the top of the n-butyraldehyde buffer tank 7 returns to the rectifying tower 1 through a gas phase reflux pipeline 27, and the pure n-butyraldehyde is extracted as a product at the bottom of the n-butyraldehyde buffer tank 7; impurities such as butyraldehyde trimer and n-butanol are extracted through an impurity delivery pipeline 24 according to the temperature of the bottom of the rectifying tower 1.
Example 2:
as shown in fig. 1, the utility model provides another technical scheme, mixed butyraldehyde's separation and purification device, with embodiment 1 the difference lies in, install respectively on the mixed butyraldehyde feeding pipeline 10 with rectifying column 1 intercommunication feeding diverter valve A11 and feeding diverter valve B12, mixed butyraldehyde in this embodiment is the material of n-butyraldehyde/isobutyraldehyde 7:1-40, its feeding temperature is 70-90 ℃, because the proportion of normal, isobutyraldehyde exists the fluctuation in production, consequently set up feeding diverter valve A11 and feeding diverter valve B12 and be used for resisting the interference, increase the practicality, use feeding diverter valve B12 when n-butyraldehyde increases, use feeding diverter valve A11 when n-butyraldehyde reduces.
The inlet of the n-butyraldehyde buffer tank 7 is respectively provided with a n-butyraldehyde extraction valve A21 and a n-butyraldehyde extraction valve B22 which are communicated with the rectifying tower 1, and the two extraction valves are arranged at the positions mainly for avoiding effectively removing heavy components when the heavy components in the feed are increased.
Example 3:
as shown in fig. 1, the utility model provides another technical scheme, mixed butyraldehyde's separation and purification device, with embodiment 1's difference lies in, the reboiler subassembly by install on rectifying column 1 first reboiler 2 and second reboiler 3 constitute, first reboiler 2 and second reboiler 3 all adopt vertical or horizontal reboiler, wherein second reboiler 3 is rectifying column 1 reboiler, first reboiler 2 is rectifying column 1 waste heat utilization reboiler, the entry of first reboiler 2 and second reboiler 3 all links to each other with the material export of rectifying column 1 bottom, the export of first reboiler 2 and second reboiler 3 links to each other with the tower cauldron of rectifying column 1; the heating medium of the second reboiler 3 is steam, the main function is that when the start-up is performed and the heating amount of the waste heat utilization reboiler is insufficient, the heating medium of the first reboiler 2 is steam condensate, the specific heat source of the second reboiler 3 is exhaust steam recovered from the top of the low-pressure steam condensate tank 8, the condensate enters the low-pressure condensate tank 9 after the exhaust steam is used, the heat source of the first reboiler 2 is from the low-pressure steam condensate tank 8, the two reboilers perform integrated utilization on waste heat generated in production, the effect of saving steam is achieved, steam consumption basically does not need to be increased in the application, and the condensate after being used is recovered into the low-pressure steam condensate tank 9 through the low-pressure steam condensate pipeline A16 and the low-pressure steam condensate pipeline B25 respectively and is delivered to the water treatment unit for recycling.
Specifically, a medium inlet of the first reboiler 2 is communicated with the bottom of the low-pressure steam condensate tank 8 through a low-pressure condensate booster pump 15, an inlet of the low-pressure steam condensate tank 8 is communicated with a low-pressure steam condensate pipeline 13, a medium outlet of the first reboiler 2 is communicated with an inlet of the low-pressure steam condensate tank 9 through a low-pressure steam condensate pipeline a16, an outlet of the low-pressure steam condensate tank 9 is communicated with a low-pressure steam condensate delivery pipeline 16, the top of the low-pressure steam condensate tank 8 is communicated with a medium inlet of the second reboiler 3 through a low-pressure exhaust steam pipeline 14, and a medium outlet of the second reboiler 3 is converged into the low-pressure steam condensate pipeline a16 through a low-pressure steam condensate pipeline B25.
Example 4:
as shown in fig. 1 and 3, the utility model provides another technical scheme, mixed butyraldehyde's separation and purification device, the difference with embodiment 1 lies in, above-mentioned separation assembly includes coalescer 54 and baffle 55, the top import department of backward flow jar 5 is equipped with into liquid section of thick bamboo 28, be equipped with guide plate 52 and mixing component 53 from last to down in proper order in the feed section of thick bamboo 51, coalescer 54 and baffle 55 set up and divide backward flow jar 5 into the feeding zone from the right side to the left side, drainage zone and isobutyraldehyde collecting region in the liquid return jar, and feed section of thick bamboo 51 corresponds the feeding zone, isobutyraldehyde pipeline 20 corresponds the isobutyraldehyde collecting region, the bottom of drainage zone is through dehydration package 56 and water discharge line 19 intercommunication, the top of backward flow jar 5 and propylene, propane discharge line 26 communicate, coalescer 54 occupies the whole cross section of backward flow jar, baffle 55 occupies the partial cross section of backward flow jar, in addition, still install silk screen remover 57 with the intercommunication department of propylene, propane discharge line 26 in backward flow jar 5.
The reflux tank 5 is a horizontal or vertical tank, and a horizontal tank is used in this embodiment.
The temperature of the top of the rectifying tower 1 is controlled at 75-80 ℃, the gas-phase isobutyraldehyde at the top of the rectifying tower is condensed to 50-70 ℃ through a top condenser 4, the gas-phase isobutyraldehyde at the top of the rectifying tower enters a reflux tank 5 and is limited to pass through a liquid inlet cylinder 51 to reduce the flow rate, a guide plate 52 is integrally an elliptic cambered plate, a small hole with the diameter of 5-15mm is formed in the guide plate 52 to reduce the flow rate and increase the retention time, in the embodiment, the guide plate 52 is welded on the opposite sides of the liquid inlet cylinder 51 in a staggered mode and is obliquely and downwards arranged, a mixing member 53 is formed by overlapping 2-10 layers of metal plates in a reversed-L shape, slow blanking is carried out through gaps among the metal plates, water dissolved in n-butyl alcohol passes through a coalescer 54 to be demulsified, coalesced and settled, emulsified liquid is demulsified, then the small water beads after demulsified are coalesced into large water beads, water beads due to density difference, the water is settled to the bottom of a shell of the coalescer 54 and is collected in a dehydration bag 56, then flows to a water discharge pipeline 19 to a water treatment device, pure overflow of the n-butyl alcohol flows through a baffle 55 and flows to an isobutyraldehyde discharge pipeline 20, other light components contained in the mixed butyraldehyde, such as propylene and is condensed, and discharged through a propylene and a propylene screen on the top of the reflux tank 5, and a propane discharge pipeline 57, and a propane is discharged, and propane is removed, and propane is discharged through a screen, and propane is removed.
The utility model provides a mixed butyraldehyde's separation and purification device, just, the result of use is better in the isobutyraldehyde separation, adopt single platform board-like rectifying column side line to adopt n-butyraldehyde, obtain the higher n-butyraldehyde of purity, and with the water that is difficult to the desorption in the present technology, propylene, propane, the butyraldehyde trimer, the n-butyl alcohol desorption, just obtain, isobutyraldehyde product purity is higher, n-butyraldehyde can reach 99.85wt% with the purity homoenergetic of isobutyraldehyde, waste heat utilization carries out exhaust steam separation and comprehensive utilization with the steam condensate after using, use two reboilers to reduce steam usage, the difficult problem of heat recovery utilizes has been solved, the utility model is strong, and good economic benefits has.
It should be understood that this example is only for illustrating the present invention and is not intended to limit the scope of the present invention. Furthermore, it should be understood that various changes or modifications can be made by those skilled in the art after reading the teachings of the present invention, and these equivalents also fall within the scope of the appended claims.
Claims (10)
1. Mixed butyraldehyde's separation and purification device, including rectifying column (1), its characterized in that: a mixed butyraldehyde feeding pipeline (10) for conveying mixed butyraldehyde is arranged in the middle of the side wall of the rectifying tower (1), and a reboiler component for heating materials in the rectifying tower (1) is arranged at the bottom of the rectifying tower (1); the top of the rectifying tower (1) is communicated with a reflux tank (5), a tower top condenser (4) is installed between the reflux tank (5) and the rectifying tower (1), a separation assembly is installed in the reflux tank (5), a propylene and propane discharge pipeline (26), a water discharge pipeline (19) and an isobutyraldehyde extraction pipeline (20) are respectively arranged on the reflux tank (5), a reflux pipeline (18) communicated with the top of the rectifying tower (1) is arranged on the isobutyraldehyde extraction pipeline (20), and an isobutyraldehyde cooler (6) is installed on the isobutyraldehyde extraction pipeline (20); the middle lower part of the rectifying tower (1) is communicated with a n-butyraldehyde buffer tank (7), the top of the n-butyraldehyde buffer tank (7) is communicated with the middle lower part of the rectifying tower (1) through a gas phase reflux pipeline (27), and the bottom of the n-butyraldehyde buffer tank (7) is communicated with a n-butyraldehyde delivery pipeline (23); the bottom of the rectifying tower (1) is communicated with an impurity delivery pipeline (24).
2. The apparatus for separating and purifying mixed butyraldehyde according to claim 1, wherein: the rectifying tower (1) adopts a float valve tower, the number of trays in the rectifying tower is 130-160 layers, and the distance between adjacent trays is 300-500mm.
3. The apparatus for separating and purifying mixed butyraldehyde according to claim 1, wherein: and a feeding switching valve A (11) and a feeding switching valve B (12) which are communicated with the rectifying tower (1) are respectively arranged on the mixed butyraldehyde feeding pipeline (10).
4. The apparatus for separating and purifying mixed butyraldehyde according to claim 1, wherein: and a n-butyraldehyde extraction valve A (21) and a n-butyraldehyde extraction valve B (22) which are communicated with the rectifying tower (1) are respectively arranged at the inlet of the n-butyraldehyde buffer tank (7).
5. The apparatus for separating and purifying mixed butyraldehyde according to claim 1, wherein: the reboiler component comprises a first reboiler (2) and a second reboiler (3) which are installed on the rectifying tower (1), the inlets of the first reboiler (2) and the second reboiler (3) are connected with the material outlet at the bottom of the rectifying tower (1), and the outlets of the first reboiler (2) and the second reboiler (3) are connected with the tower kettle of the rectifying tower (1).
6. The apparatus for separating and purifying mixed butyraldehyde according to claim 5, wherein: the bottom intercommunication of the medium import of first reboiler (2) through low pressure condensate booster pump (15) and low pressure steam condensate tank (8), and the import and the low pressure steam condensate pipeline (13) intercommunication of low pressure steam condensate tank (8), the medium export of first reboiler (2) is through the import intercommunication of low pressure steam condensate pipeline A (16) and low pressure steam condensate tank (9), the export intercommunication of low pressure steam condensate tank (9) has low pressure steam condensate outward conveying pipeline (17).
7. The apparatus for separating and purifying mixed butyraldehyde according to claim 6, wherein: the top of the low-pressure steam condensate tank (8) is communicated with a medium inlet of a second reboiler (3) through a low-pressure steam exhaust pipeline (14), and a medium outlet of the second reboiler (3) is converged into a low-pressure steam condensate pipeline A (16) through a low-pressure steam condensate pipeline B (25).
8. The apparatus for separating and purifying mixed butyraldehyde according to claim 1, wherein: the separation component comprises a coalescer (54) and a baffle (55), a liquid inlet cylinder (51) is arranged at the inlet of the top of the backflow tank (5), a guide plate (52) and a mixing component (53) are sequentially arranged in the liquid inlet cylinder (51) from top to bottom, the coalescer (54) and the baffle (55) are horizontally arranged at intervals in the backflow tank and divide the backflow tank (5) into a feeding area, a draining area and an isobutyraldehyde collecting area, the liquid inlet cylinder (51) corresponds to the feeding area, the isobutyraldehyde collecting pipeline (20) corresponds to the isobutyraldehyde collecting area, the bottom of the draining area is communicated with a water discharging pipeline (19) through a dewatering drum (56), and the top of the backflow tank (5) is communicated with a propylene and propane discharging pipeline (26).
9. The apparatus for separating and purifying mixed butyraldehyde according to claim 8, wherein: the coalescer (54) occupies the entire cross section of the return tank, and the baffle (55) occupies a part of the cross section of the return tank.
10. The apparatus for separating and purifying mixed butyraldehyde according to claim 9, wherein: and a wire mesh demister (57) is also arranged at the communication part of the reflux tank (5) and the propylene and propane discharge pipeline (26).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221707593.1U CN217612992U (en) | 2022-07-01 | 2022-07-01 | Mixed butyraldehyde separation and purification device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221707593.1U CN217612992U (en) | 2022-07-01 | 2022-07-01 | Mixed butyraldehyde separation and purification device |
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| Publication Number | Publication Date |
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| CN217612992U true CN217612992U (en) | 2022-10-21 |
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| CN202221707593.1U Active CN217612992U (en) | 2022-07-01 | 2022-07-01 | Mixed butyraldehyde separation and purification device |
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2022
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