CN221981602U - Supergravity rectifying device for separating butyl acetate and phenol - Google Patents
Supergravity rectifying device for separating butyl acetate and phenol Download PDFInfo
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- CN221981602U CN221981602U CN202420078355.1U CN202420078355U CN221981602U CN 221981602 U CN221981602 U CN 221981602U CN 202420078355 U CN202420078355 U CN 202420078355U CN 221981602 U CN221981602 U CN 221981602U
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- butyl acetate
- hypergravity
- phenol
- liquid phase
- tower
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- DKPFZGUDAPQIHT-UHFFFAOYSA-N Butyl acetate Natural products CCCCOC(C)=O DKPFZGUDAPQIHT-UHFFFAOYSA-N 0.000 title claims abstract description 36
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 title claims abstract description 30
- GJYCVCVHRSWLNY-UHFFFAOYSA-N ortho-butylphenol Natural products CCCCC1=CC=CC=C1O GJYCVCVHRSWLNY-UHFFFAOYSA-N 0.000 title claims abstract description 22
- FUZZWVXGSFPDMH-UHFFFAOYSA-N hexanoic acid Chemical compound CCCCCC(O)=O FUZZWVXGSFPDMH-UHFFFAOYSA-N 0.000 title claims abstract 15
- 239000007791 liquid phase Substances 0.000 claims abstract description 31
- 239000012071 phase Substances 0.000 claims abstract description 31
- 238000003860 storage Methods 0.000 claims abstract description 23
- 239000012267 brine Substances 0.000 claims abstract description 5
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 4
- 238000010992 reflux Methods 0.000 claims description 24
- 239000000463 material Substances 0.000 claims description 13
- 238000010009 beating Methods 0.000 claims description 6
- 238000011084 recovery Methods 0.000 claims description 6
- 230000003068 static effect Effects 0.000 claims description 6
- 229910000975 Carbon steel Inorganic materials 0.000 claims description 3
- 239000010962 carbon steel Substances 0.000 claims description 3
- 239000010935 stainless steel Substances 0.000 claims description 3
- 229910001220 stainless steel Inorganic materials 0.000 claims description 3
- 239000007788 liquid Substances 0.000 abstract description 15
- FUZZWVXGSFPDMH-UHFFFAOYSA-M hexanoate Chemical compound CCCCCC([O-])=O FUZZWVXGSFPDMH-UHFFFAOYSA-M 0.000 description 21
- 238000000034 method Methods 0.000 description 8
- 239000000243 solution Substances 0.000 description 8
- 230000008569 process Effects 0.000 description 6
- 238000000926 separation method Methods 0.000 description 5
- 238000005086 pumping Methods 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 239000011248 coating agent Substances 0.000 description 2
- 238000000576 coating method Methods 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000010985 leather Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000000859 sublimation Methods 0.000 description 2
- 230000008022 sublimation Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003085 diluting agent Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- -1 ester organic compound Chemical class 0.000 description 1
- 239000003292 glue Substances 0.000 description 1
- 239000000976 ink Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000013307 optical fiber Substances 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Abstract
The utility model discloses a hypergravity rectifying device for separating butyl acetate and phenol, which comprises: the mixed liquid storage tank is used for storing mixed liquid to be treated; the hypergravity rectifying tower comprises a tower body and a jacket, wherein a baffling rotor is arranged in the tower body, and the hypergravity rectifying tower is used for separating butyl acetate and phenol; the top of the hypergravity rectifying tower is connected with a gas-phase condensing system, the gas-phase condensing system comprises a first-stage condenser and a second-stage condenser, the first-stage condenser condenses circulating water, and the second-stage condenser condenses cold brine. The utility model has small equipment volume and small occupied area, and compared with the traditional tower equipment, the structure of the hypergravity rectifying device is more compact, and the volume of the equipment can be obviously reduced, thereby saving the space, improving the utilization rate of liquid phase by creating a high-speed centrifugal force field, and obtaining a product with higher purity.
Description
Technical Field
The utility model relates to the technical field of chemical industry, in particular to a hypergravity rectifying device for separating butyl acetate and phenol.
Background
Butyl acetate is a clear and colorless liquid, belongs to an ester organic compound, and has good solubility and volatility. Butyl acetate as an organic solvent can be used for extracting and separating organic matters, and is commonly used for preparing paint, printing ink, glue, resin and other chemical products in chemical production; in the coating industry, butyl acetate can be used as a diluent and a volatilization control agent to help adjust the viscosity and drying speed of the coating; in the leather industry, it can then be used as a solvent and a forming agent to help speed up the leather treatment process.
Among the existing separation methods, the stripping method is the most widely used method, and components in the mixture are separated by sublimation and condensation using a plate column or a packed column, and are realized by utilizing different boiling points or volatilities of the components. However, due to the presence of solid particles or high boilers in the mixture, these can cause clogging of the equipment during sublimation and condensation, resulting in interruption of the operating process and even damage to the equipment, requiring regular maintenance and slowing down the production process.
Disclosure of utility model
The utility model aims at: in order to solve the problems, the utility model provides a hypergravity rectifying device for separating butyl acetate and phenol.
The utility model adopts the following technical scheme for realizing the purposes, and comprises the following steps:
the mixed liquid storage tank is used for storing mixed liquid to be treated;
The high-gravity rectifying tower comprises a tower body and a jacket, wherein a baffling rotor is arranged in the tower body, and the high-gravity rectifying tower is used for separating butyl acetate and phenol;
The top of the hypergravity rectifying tower is connected with a gas-phase condensing system, the gas-phase condensing system comprises a first-stage condenser and a second-stage condenser, the first-stage condenser is used for condensing circulating water, and the second-stage condenser is used for condensing cold brine.
As a further description of the above technical solution, the discharging port at the bottom of the mixed liquor storage tank is connected with the hypergravity rectifying tower through a pipeline, the pipeline is provided with a first material pumping pump, and the mixed liquor is pumped into the hypergravity rectifying tower through the material pumping pump.
As a further description of the above technical solution, the rotor includes a stationary disc and a movable disc, the stationary disc is fixed with the housing, the movable disc is fixed with the spindle and rotates with the spindle, and a baffle ring is mounted above the stationary disc in a matching manner.
As further description of the above technical solution, the material of the tower body is any one of 304, 316L, 904L stainless steel.
As further description of the technical scheme, the jacket is made of carbon steel, and steam is introduced into the jacket to continuously supply heat to the liquid phase in the tower body.
As a further description of the above technical solution, two sides of the top of the hypergravity rectifying tower are respectively provided with a liquid phase inlet and a gas phase outlet, the liquid phase inlet is connected with a second material beating pump, and the gas phase outlet is connected with the gas phase inlet of the first-stage condenser of the gas phase condensing system through a pipeline.
As further description of the technical scheme, a liquid phase reflux port is arranged at the top of one side of the hypergravity rectifying tower and is connected with an outlet of the reflux tank through a pipeline, the pipeline is provided with a reflux pump, and part of liquid phase in the reflux tank is refluxed into the hypergravity rectifying tower through the reflux pump.
As further description of the technical scheme, a liquid phase outlet is arranged at the bottom of one side of the hypergravity rectifying tower and is connected with an inlet of a recovered phenol storage tank through a pipeline.
As a further description of the above technical solution, the gas phase outlet of the primary condenser is connected to the gas phase inlet of the secondary condenser through a pipe, the top of the secondary condenser is connected to a vacuum system, and the liquid phase outlets of the primary condenser and the secondary condenser are connected to the inlet of the receiving tank.
As a further description of the above technical solution, the receiving tank outlet and the reflux tank inlet are connected with the butyl acetate recovery tank inlet.
The beneficial effects of the utility model are as follows:
1. The utility model adopts the supergravity rectifying device to replace the traditional packed tower and plate tower, and has small equipment volume and small occupied area. Compared with the traditional tower type equipment, the structure of the hypergravity rectifying device is more compact, the volume of the equipment can be obviously reduced, thereby saving space, improving the utilization rate of liquid phase by creating a high-speed centrifugal force field, and obtaining a product with higher purity;
2. According to the utility model, an automatic device is adopted to replace manual operation, so that the contact between personnel and materials can be reduced, parameters such as temperature, pressure, flow rate and the like of the system can be monitored in real time through the DCS central control system, remote control is convenient at any time, and the production efficiency is improved. Meanwhile, the automation device can effectively reduce errors and risks of manual operation, and improve product quality and work safety.
In order to more clearly illustrate the structural features and functions of the present utility model, the present utility model will be described in detail below with reference to the accompanying drawings and the embodiments.
Drawings
FIG. 1 is a schematic diagram of the structure of the hypergravity rectification apparatus for separating butyl acetate and phenol of the present utility model.
Reference numerals:
1. A mixed liquid storage tank; 2. a first material-beating pump; 3. a hypergravity rectifying tower; 4. a first-stage condenser; 5. a second-stage condenser; 6. a receiving tank; 7. a reflux drum; 8. a reflux pump; 9. recovering a butyl acetate storage tank; 10. a second material pumping pump; 11. and (5) recovering the phenol storage tank.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present utility model more clear, the technical solutions of the embodiments of the present utility model will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present utility model.
As shown in fig. 1, in one embodiment, a hypergravity rectification apparatus for separating butyl acetate and phenol, comprises: the mixed liquor storage tank 1, the mixed liquor storage tank 1 is used for storing the mixed liquor to be treated. Wherein, the drain hole in the bottom of the mixed liquor storage tank 1 is connected with the supergravity rectifying tower 3 through a pipeline, the pipeline is provided with a first material pump 2, and the mixed liquor is pumped into the supergravity rectifying tower 3 through the material pump.
In this example, as shown in FIG. 1, a hypergravity rectifying column 3 is used for separating butyl acetate and phenol, and is composed of a column body and a jacket. Specifically, the tower body can be made of any one of 304, 316L and 904L stainless steel so as to meet different process requirements and medium characteristics. The jacket is made of carbon steel, steam is introduced through the jacket, continuous heating is provided for the liquid phase in the tower body, the constant temperature in the liquid phase is kept, and the separation efficiency and the product quality are improved.
Further, a baffling rotor is arranged in the tower body and consists of a static disc and a movable disc. The static disc is fixed with the shell, and the dynamic disc is fixed with the main shaft and rotates along with the main shaft. The baffle rings are also arranged above the static disc in a matched manner, so that the mixed liquid entering the tower can be uniformly distributed and flows. In the operation process, the mixed liquid enters the tower from the liquid phase inlet, the rotation of the rotor can generate high-speed centrifugal effect, so that components move to the periphery under the action of a centrifugal force field, and the liquid can be divided into a plurality of layers by the baffle ring, so that the separation efficiency is further improved.
With continued reference to fig. 1, the top of the hypergravity rectifying tower 3 is respectively provided with a liquid phase inlet and a gas phase outlet, the liquid phase inlet is connected with the second knockout pump 10, and the gas phase outlet is connected to the gas phase inlet of the first-stage condenser 4 of the gas phase condensing system through a pipeline. Meanwhile, a liquid phase reflux port is arranged at the top of one side of the tower, is connected with the outlet of the reflux tank 7 through a pipeline, and returns part of liquid phase to the hypergravity rectifying tower 3 through a reflux pump 8. In addition, in the case of the optical fiber, the bottom of one side of the tower is provided with a liquid phase outlet, the liquid phase outlet is connected with the inlet of the recovered phenol storage tank 11 through a pipeline. The design and the connection mode jointly realize efficient liquid-gas phase separation and reflux utilization, and ensure the high-quality output and storage of products.
As shown in fig. 1, in the present embodiment, a gas phase condensing system including a primary condenser 4 and a secondary condenser 5 is connected to the top of the hypergravity rectifying column 3. In the separation process, the circulating water is condensed by the primary condenser 4, and the cold brine is condensed by the secondary condenser 5, thereby converting the volatile components in the gas phase into liquid.
Specifically, the gas phase outlet of the primary condenser 4 is connected to the gas phase inlet of the secondary condenser 5 by a pipe, so that a continuous gas phase flow path is formed between the condensers. As the gas phase flows, the volatile components therein gradually condense and turn into a liquid state, releasing a large amount of heat. The top of the secondary condenser 5 is connected with a vacuum system, and the air pressure in the condenser is reduced to a level lower than the atmospheric pressure by the action of the vacuum system, so that the smooth flow of the gas phase and the smooth recovery of the liquid are promoted. Meanwhile, as the secondary condenser 5 adopts a cold brine condensing mode, an additional cooling medium is not needed in the condensing process, thereby reducing the cost and the energy consumption.
With continued reference to fig. 1, the liquid phase outlets of the primary condenser 4 and the secondary condenser 5 are both connected to the inlet of the receiving tank 6, and the separated liquid is collected in the receiving tank 6. The liquid phase outlet at the bottom of the receiving tank 6 is respectively connected with a reflux tank 7 and a recovered butyl acetate storage tank 9. Wherein, all set up the circulation device in mixed liquor storage tank 1, the recovery butyl acetate storage tank 9 and the recovery phenol storage tank 11, make the material dispersion more even.
Working principle: when butyl acetate is separated, mixed liquid in the mixed liquid storage tank 1 enters the hypergravity rectifying tower 3 through a material beating pump, and the butyl acetate is vaporized and fully separated from phenol by introducing steam into a jacket for heating. In the process, the DCS central control system controls the temperature, the pressure and the flow, so that the normal reaction is ensured. The separated butyl acetate gas phase is condensed from the top of the tower to a receiving tank 6 through a first-stage condenser 4, and the uncondensed butyl acetate gas phase is condensed to the receiving tank 6 through a second-stage condenser 5 to be converged. One part of the waste water enters a reflux tank 7, and the other part directly flows into a butyl acetate recovery storage tank 9. The liquid phase in the reflux tank 7 is refluxed to the hypergravity rectifying tower 3 through a reflux pipeline between the reflux tank 7 and the hypergravity rectifying tower 3, so that the purity of the butyl acetate is improved. The unvaporized phenol in the tower kettle of the hypergravity rectifying tower 3 flows into a recovered phenol storage tank 11, and the separation of butyl acetate and phenol is completed.
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present utility model. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the utility model. Thus, the present utility model is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (10)
1. A hypergravity rectification apparatus for separating butyl acetate and phenol, comprising:
The mixed liquor storage tank (1), the said mixed liquor storage tank (1) is used for storing the mixed liquor to be treated;
The high-gravity rectifying tower (3), wherein the high-gravity rectifying tower (3) comprises a tower body and a jacket, a baffling rotor is arranged in the tower body, and the high-gravity rectifying tower (3) is used for separating butyl acetate and phenol;
The top of the hypergravity rectifying tower (3) is connected with a gas-phase condensing system, the gas-phase condensing system comprises a first-stage condenser (4) and a second-stage condenser (5), the first-stage condenser (4) is used for condensing circulating water, and the second-stage condenser (5) is used for condensing cold brine.
2. The hypergravity rectifying device for separating butyl acetate and phenol according to claim 1, wherein a discharge port at the bottom of the mixed liquor storage tank (1) is connected with the hypergravity rectifying tower (3) through a pipeline, the pipeline is provided with a first material beating pump (2), and the mixed liquor is pumped into the hypergravity rectifying tower (3) through the material beating pump.
3. The hypergravity rectification device for separating butyl acetate and phenol according to claim 1, wherein the rotor comprises a static disc and a movable disc, the static disc is fixed with the shell, the movable disc is fixed with the main shaft and rotates along with the main shaft, and a baffle ring is cooperatively arranged above the static disc.
4. The hypergravity rectification device for separating butyl acetate and phenol according to claim 1, wherein the tower body is made of any one of 304, 316L and 904L stainless steel.
5. The hypergravity rectification device for separating butyl acetate and phenol according to claim 1, wherein the jacket is made of carbon steel, and steam is introduced into the jacket to continuously supply heat to the liquid phase in the tower body.
6. The hypergravity rectifying device for separating butyl acetate and phenol according to claim 1, wherein a liquid phase inlet and a gas phase outlet are respectively arranged on two sides of the top of the hypergravity rectifying tower (3), the liquid phase inlet is connected with a second material beating pump (10), and the gas phase outlet is connected with a gas phase inlet of the primary condenser (4) of the gas phase condensing system through a pipeline.
7. The hypergravity rectifying device for separating butyl acetate and phenol according to claim 1, wherein a liquid phase reflux port is arranged at the top of one side of the hypergravity rectifying tower (3), the liquid phase reflux port is connected with an outlet of a reflux tank (7) through a pipeline, the pipeline is provided with a reflux pump (8), and part of liquid phase in the reflux tank (7) is refluxed into the hypergravity rectifying tower (3) through the reflux pump (8).
8. The hypergravity rectifying device for separating butyl acetate and phenol according to claim 1, wherein a liquid phase outlet is arranged at the bottom of one side of the hypergravity rectifying tower (3), and the liquid phase outlet is connected with an inlet of a recovered phenol storage tank (11) through a pipeline.
9. The hypergravity rectification device for separating butyl acetate and phenol according to claim 1, wherein the gas phase outlet of the primary condenser (4) is connected with the gas phase inlet of the secondary condenser (5) through a pipeline, the top of the secondary condenser (5) is connected with a vacuum system, and the liquid phase outlet of the primary condenser (4) and the liquid phase outlet of the secondary condenser (5) are connected with the inlet of the receiving tank (6).
10. The hypergravity rectification device for separating butyl acetate and phenol according to claim 9, wherein the outlet of the receiving tank (6) is connected with the inlet of the reflux tank (7), and the inlet of the butyl acetate recovery tank (9) is connected.
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN221981602U true CN221981602U (en) | 2024-11-12 |
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| GR01 | Patent grant |