CN212246831U - Acetic acid azeotropic dehydration device suitable for producing trimellitic anhydride - Google Patents
Acetic acid azeotropic dehydration device suitable for producing trimellitic anhydride Download PDFInfo
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- CN212246831U CN212246831U CN202021051150.2U CN202021051150U CN212246831U CN 212246831 U CN212246831 U CN 212246831U CN 202021051150 U CN202021051150 U CN 202021051150U CN 212246831 U CN212246831 U CN 212246831U
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Abstract
The utility model provides an acetic acid azeotropic dehydration device suitable for production trimellitic anhydride, it includes azeotropic distillation tower, still includes solvent recovery tower, azeotropic distillation tower at its top with I pipe connection of condenser, I pipe connection of condenser has the profit phase-splitting jar, the oil phase subregion of profit phase-splitting jar through distribution line V with azeotropic distillation tower pipe connection, water phase subregion are connected with distribution line III, an export of distribution line III with V pipe connection of distribution line, another export with solvent recovery tower pipe connection; the solvent recovery tower is connected with a liquid-liquid phase separation tank through a condenser II; the liquid-liquid phase separation tank is respectively connected with an IPA intermediate storage tank and an intermediate storage tank through pipelines. The utility model discloses can carry out the azeotropic dehydration of acetic acid in succession, equipment input is little, the production energy consumption is low.
Description
Technical Field
The utility model relates to a trimellitic anhydride apparatus for producing, concretely relates to contains water acetic acid low energy consumption water trap in trimellitic anhydride production process.
Background
Trimellitic anhydride, abbreviated as trimellitic anhydride or TMA. The production process is to prepare trimellitic acid from trimellitic benzene and then prepare trimellitic anhydride. The acetic acid azeotropic separation technology is mostly used for PTA devices, in trimellitic anhydride production devices, because large-scale production cannot be realized, the total amount of water-containing acetic acid is not large, and acetic acid contains a small amount of pseudocumene, in order to realize the recovery of the pseudocumene, the existing devices mostly adopt a thermal coupling tower to carry out the separation of water and the recovery of the pseudocumene. Because acetic acid is highly corrosive, the separation column must be made of special materials. On the whole, the factors such as large equipment investment, high energy consumption and the like which are not beneficial to reducing the production cost exist.
Disclosure of Invention
The utility model aims to solve the technical problem that an acetic acid azeotropic dehydration device suitable for production trimellitic anhydride is provided, can carry out the acetic acid azeotropic dehydration in succession, and equipment investment is little, the production energy consumption is low.
In order to solve the technical problem, the acetic acid azeotropic dehydration device suitable for producing trimellitic anhydride comprises an azeotropic rectifying tower and a solvent recovery tower, wherein a condenser I is arranged above the azeotropic rectifying tower, the azeotropic rectifying tower is connected with the condenser I through a pipeline at the top of the azeotropic rectifying tower, and the bottom of the azeotropic rectifying tower is connected with an acetic acid product storage tank; the condenser I is connected with an oil-water phase separation tank through a pipeline, an oil phase partition of the oil-water phase separation tank is connected with the pipeline of the azeotropic distillation tower through a distribution line V, and an oil phase distribution pump and a valve II are arranged on the distribution line V; the water phase partition of the oil-water phase separation tank is connected with a distribution line III through a water phase distribution pump, one outlet of the distribution line III is connected with a pipeline of the distribution line V through a valve III, and the other outlet of the distribution line III is connected with a pipeline of the solvent recovery tower through a valve IV; the top pipeline of the solvent recovery tower is connected with a condenser II, and the condenser II is connected with a liquid-liquid phase separation tank through a pipeline; an outlet of the liquid-liquid phase separation tank is connected with an IPA intermediate storage tank through a valve V, the IPA intermediate storage tank is connected with a distribution line I through a reflux distribution pump, and the distribution line I is connected with an oil phase partition pipeline of the oil-liquid phase separation tank through the valve I; and the other outlet of the liquid-liquid phase separation tank is connected with a PSC intermediate storage tank through a valve VI pipeline.
The liquid-liquid phase separation tank is arranged above the IPA intermediate storage tank and the PSC intermediate storage tank, so that liquid subjected to phase separation in the liquid-liquid phase separation tank can flow into the two intermediate storage tanks respectively under the self weight.
The utility model also provides an acetic acid azeotropic dehydration method suitable for production trimellitic anhydride, including following step:
step 1: preheating an azeotropic distillation dilute acetic acid raw material liquid with the concentration of 80-85% to 80 +/-5 ℃, then feeding the azeotropic distillation dilute acetic acid raw material liquid into an azeotropic distillation tower, simultaneously adding isopropyl acetate into the tower as an entrainer, controlling the pressure in a tower kettle to be 40-60 kpa, controlling the temperature at the top of the tower to be 52-60 ℃, and controlling the temperature in the tower kettle to be 110 ℃ through a reboiler so as to separate components with different boiling points.
Step 2: acetic acid with the concentration of 96 percent extracted from the bottom of the azeotropic distillation tower enters an acetic acid product storage tank, gas-phase diluted acetic acid, water and an entrainer at the top of the azeotropic distillation tower are condensed by a condenser I and then enter an oil-water phase-splitting tank for phase splitting, an oil phase reflows to enter the azeotropic distillation tower through an oil phase distribution pump and a distribution line V, a part of the water phase is controlled to return to the top of the azeotropic distillation tower through a valve III after being output by the reflux distribution pump, and the rest of the water phase enters a solvent recovery tower through a valve IV for re-separation;
and step 3: the gas phase at the top of the solvent recovery tower enters a liquid-liquid phase separation tank after being condensed by a condenser II, PSC and IPA are separated in the liquid-liquid phase separation tank after liquid-liquid phase separation and enter a PSC intermediate storage tank and an IPA intermediate storage tank respectively, and the recovered substances in the IPA intermediate storage tank return to an oil phase partition of the oil-water phase separation tank through a reflux distribution pump and a distribution line I.
In the step 2, the flow of the water phase and the flow of the oil phase which return to the top of the azeotropic distillation tower from the oil-water phase-separating tank are equal under the control of a valve III.
The technical advantages of the utility model are embodied in that: the isopropyl acetate is used as the entrainer to realize low-energy-consumption continuous dehydration of the hydrous acetic acid, and the equipment investment and the production energy consumption are low.
Drawings
FIG. 1 is a schematic structural diagram of an azeotropic dehydration device for acetic acid suitable for producing trimellitic anhydride.
Detailed Description
The following describes the embodiments of the present invention with reference to the accompanying drawings.
As shown in fig. 1, the acetic acid azeotropic dehydration device suitable for producing trimellitic anhydride of the present invention comprises an azeotropic distillation column T1 and a solvent recovery column T2, wherein a condenser ie 1 is arranged above the azeotropic distillation column T1, the azeotropic distillation column T1 is connected with the condenser ie 1 through a pipeline at the top thereof, and the bottom of the azeotropic distillation column T1 is connected with an acetic acid product storage tank; the condenser I E1 is connected with an oil-water phase separation tank D2 through a pipeline, an oil phase partition of the oil-water phase separation tank D2 is connected with the azeotropic distillation tower T1 through a distribution line V X5, and an oil phase distribution pump P2 and a valve II V2 are arranged on the distribution line V X5; the water phase subarea of the oil-water phase separation tank D2 is connected with a distribution line IIIX 3 through a water phase distribution pump P3, one outlet of the distribution line IIIX 3 is connected with a pipeline of the distribution line VX 5 through a valve IIIV 3, and the other outlet is connected with a pipeline of the solvent recovery tower T2 through a valve IV V4; the top pipeline of the solvent recovery tower T2 is connected with a condenser II E2, and the condenser II E2 is connected with a liquid-liquid phase separation tank D3 through a pipeline; an outlet of the liquid-liquid phase separation tank D3 is connected with an IPA intermediate storage tank D1 through a valve V5, the IPA intermediate storage tank D1 is connected with a distribution line IX 1 through a reflux distribution pump P1, and the distribution line IX 1 is connected with an oil phase partition pipeline of the oil-water phase separation tank D2 through a valve IV 1; the other outlet of the liquid-liquid phase separation tank D3 is connected with a PSC intermediate storage tank D4 through a valve VI V6 by a pipeline.
The liquid-liquid phase separation tank D3 is disposed above the IPA intermediate tank D1 and the PSC intermediate tank D4, so that the liquid separated in the liquid-liquid phase separation tank D3 can flow into the two intermediate tanks by its own weight.
The utility model discloses an overall thinking is: the method comprises the following steps that aqueous acetic acid enters an azeotropic rectifying tower, water is carried to the tower top by IPA under the action of isopropyl acetate IPA, gas phase at the tower top is condensed and then enters an oil-water phase-splitting tank, after phase splitting is carried out in the oil-water phase-splitting tank, all oil phase is used as reflux and returns to the tower top of the azeotropic rectifying tower, part of water phase is used as reflux, part of water phase is used as wastewater, the wastewater is extracted from the oil-water phase-splitting tank and enters a solvent recovery tower T2, and acetic acid with qualified content is obtained at the.
The water phase extracted from the oil-water phase separation tank D2 contains a small amount of IPA and PSC, the water phase is separated again in a solvent recovery tower T2, IPA and PSC extracted from the tower top enter a liquid-liquid phase separation tank D3 for liquid-liquid phase separation, PSC and IPA are separated for recycling, and the wastewater in the tower bottom of the solvent recovery tower T2 is sent to a sewage treatment system.
The specific working process is as follows: an acetic acid azeotropic dehydration method suitable for producing trimellitic anhydride comprises the following steps:
step 1: preheating an azeotropic distillation dilute acetic acid raw material liquid with the concentration of 80-85% to 80 +/-5 ℃, then feeding the azeotropic distillation dilute acetic acid raw material liquid into an azeotropic distillation tower T1, simultaneously adding isopropyl acetate into the tower as an entrainer, controlling the pressure in a tower kettle to be 40-60 kpa, controlling the temperature at the top of the tower to be 52-60 ℃, and controlling the temperature in the tower kettle to be 100-110 ℃ through a reboiler so as to separate components with different boiling points.
Step 2: acetic acid with the concentration of 96 percent extracted from the bottom of an azeotropic distillation tower T1 enters an acetic acid product storage tank, gas-phase dilute acetic acid, water and an entrainer at the top of the azeotropic distillation tower T1 enter an oil-water phase-splitting tank D2 for phase splitting after being condensed by a condenser IE 1, an oil phase flows back to the azeotropic distillation tower T1 through an oil phase distribution pump P2 and a distribution line VX 5, a part of a water phase is controlled to return to the top of the azeotropic distillation tower T1 through a valve III V3 after being output by a reflux distribution pump P3, and the rest of the water phase enters a solvent recovery tower T2 through a valve IV V4 for re-separation;
and step 3: the gas phase at the top of the solvent recovery tower T2 enters a liquid-liquid phase separation tank D3 after being condensed by a condenser II E2, PSC and IPA are separated in the liquid-liquid phase separation tank D3 after liquid-liquid phase separation and enter a PSC intermediate storage tank D4 and an IPA intermediate storage tank D1 respectively, and the recovered substance of the IPA intermediate storage tank D1 returns to the oil phase partition of the oil-water phase separation tank D2 through a reflux distribution pump P1 and a distribution line I X1.
In the step 2, the flow rates of the water phase and the oil phase returned to the top of the azeotropic distillation tower T1 from the oil-water phase separation tank D2 are equal under the control of a valve III V3.
The utility model discloses realized successful application in my department's metaanhydride production line. Through actual operation, high-efficiency continuous operation is realized, equipment investment is effectively reduced, and energy consumption is reduced. A double-tower coupling operation mode is adopted before transformation, the investment of a single tower is about 600 ten thousand, the total investment is 1200 ten thousand yuan, and the total investment is about 900 ten thousand yuan after the equipment is developed; before modification, the unit hour treatment capacity of acetic acid is 10 tons, steam consumption is about 12 tons, and after modification, the azeotropic distillation tower consumes 8 tons of steam per hour. Therefore, the investment is reduced, and the low-cost continuous operation is realized.
The present invention is not limited to the above embodiments, and those skilled in the art can make various corresponding changes and modifications according to the present invention without departing from the spirit and the essential scope thereof, and still fall into the protection scope of the present invention.
Claims (1)
1. An acetic acid azeotropic dehydration device suitable for producing trimellitic anhydride, which comprises an azeotropic distillation tower (T1) and a solvent recovery tower (T2), and is characterized in that: a condenser I (E1) is arranged above the azeotropic distillation tower (T1), the top of the azeotropic distillation tower (T1) is connected with the condenser I (E1) through a pipeline, and the bottom of the azeotropic distillation tower (T1) is connected with an acetic acid product storage tank; the condenser I (E1) is connected with an oil-water phase separation tank (D2) through a pipeline, the oil phase partition of the oil-water phase separation tank (D2) is connected with the azeotropic distillation tower (T1) through a distribution line V (X5) through a pipeline, and an oil phase distribution pump (P2) and a valve II (V2) are arranged on the distribution line V (X5); the water phase partition of the oil-water phase separation tank (D2) is connected with a distribution line III (X3) through a water phase distribution pump (P3), one outlet of the distribution line III (X3) is connected with a pipeline of the distribution line V (X5) through a valve III (V3), and the other outlet is connected with a pipeline of the solvent recovery tower (T2) through a valve IV (V4); the solvent recovery tower (T2) is connected with a condenser II (E2) through a pipeline at the top part of the solvent recovery tower, and the condenser II (E2) is connected with a liquid-liquid phase separation tank (D3) through a pipeline; an outlet of the liquid-liquid phase separation tank (D3) is connected with an IPA intermediate storage tank (D1) through a valve V (V5), the IPA intermediate storage tank (D1) is connected with a distribution line I (X1) through a reflux distribution pump (P1), and the distribution line I (X1) is connected with an oil phase partition pipeline of the oil-liquid phase separation tank (D2) through a valve I (V1); the other outlet of the liquid-liquid phase separation tank (D3) is connected with a PSC intermediate storage tank (D4) through a valve VI (V6) by a pipeline.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021051150.2U CN212246831U (en) | 2020-06-10 | 2020-06-10 | Acetic acid azeotropic dehydration device suitable for producing trimellitic anhydride |
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| CN202021051150.2U CN212246831U (en) | 2020-06-10 | 2020-06-10 | Acetic acid azeotropic dehydration device suitable for producing trimellitic anhydride |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111606877A (en) * | 2020-06-10 | 2020-09-01 | 安庆亿成化工科技有限公司 | Acetic acid azeotropic dehydration device and method suitable for producing trimellitic anhydride |
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2020
- 2020-06-10 CN CN202021051150.2U patent/CN212246831U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111606877A (en) * | 2020-06-10 | 2020-09-01 | 安庆亿成化工科技有限公司 | Acetic acid azeotropic dehydration device and method suitable for producing trimellitic anhydride |
| CN111606877B (en) * | 2020-06-10 | 2023-04-25 | 安庆亿成化工科技有限公司 | Acetic acid azeotropic dehydration device and method suitable for producing trimellitic anhydride |
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