CN210656743U - Evaporation device for ortho-xylene - Google Patents
Evaporation device for ortho-xylene Download PDFInfo
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- CN210656743U CN210656743U CN201921606102.2U CN201921606102U CN210656743U CN 210656743 U CN210656743 U CN 210656743U CN 201921606102 U CN201921606102 U CN 201921606102U CN 210656743 U CN210656743 U CN 210656743U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
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Abstract
The utility model relates to an evaporation equipment for ortho-xylene. Is characterized by comprising a steam feed tank, a vapor phase heat exchanger, a flash tank, a solvent evaporator, a condenser and an o-xylene recovery tank; the steam feed tank is used for containing raw materials; the vapor phase heat exchanger is used for preheating the raw material, the flash tank is used for realizing vaporization and two-phase separation of the raw material, the solvent evaporator is used for realizing evaporation of the solvent, and the condenser is communicated with the vapor phase heat exchanger and is used for collecting the gas phase o-xylene from the vapor phase heat exchanger and condensing the gas phase o-xylene into liquid for recycling. The utility model discloses a combination of flash tank and solvent evaporator has realized the continuous evaporation separation of this three of o-xylene, acetone and acrylonitrile, and the waste heat that produces among the evaporation process is not only extravagant, has still carried out abundant recycle moreover, has very good energy-conserving effect.
Description
Technical Field
The utility model relates to an evaporation equipment, especially an evaporation equipment who is used for o-xylene in diacetone acrylamide production process.
Background
In the extraction process of diacetone acrylamide, o-xylene is required to be added to extract diacetone in water, and the o-xylene is separated and recycled after extraction. And the extracted material contains acetone and acrylonitrile besides o-xylene. Because o-xylene has different boiling points than acetone and acrylonitrile, acetone and acrylonitrile need to be separated before the o-xylene is separated.
In the prior art, the operation of the step is only to directly separate the three substances through a batch distillation tower, and the three substances have different boiling points, so that the separation cannot be completed simultaneously, and evaporation separation is needed to be performed respectively. The three substances need to be heated continuously in the separation process, the distillation process is complicated, the distillation effect is not ideal, continuous production cannot be realized, and the whole evaporation process is low in efficiency and high in energy consumption.
Disclosure of Invention
The utility model aims at providing an evaporation equipment for ortho-xylene, this equipment has realized the continuous evaporation separation of this three of ortho-xylene, acetone and acrylonitrile, has improved the separation effect, has promoted separation efficiency.
In order to achieve the above effect, the utility model discloses a technical scheme as follows:
the evaporation equipment for ortho-xylene is characterized by comprising a evaporation feed tank 10, a vapor phase heat exchanger 20, a flash tank 30, a solvent evaporator 40, a condenser 50 and an ortho-xylene recovery tank 60; wherein
The evaporation feed tank 10 is used for containing raw materials, and is provided with a raw material inlet 11 at the top and a raw material outlet 12 at the bottom;
the vapor-phase heat exchanger 20 is used for preheating raw materials and comprises a heat exchanger shell pass feed inlet 21, a heat exchanger shell pass discharge outlet 22, a heat exchanger tube pass feed inlet 23 and a heat exchanger tube pass discharge outlet 24; a shell side feed inlet 21 of the heat exchanger is communicated with a raw material outlet 12 of the evaporation feed tank 10 through a shell side feed pipeline L1 of the heat exchanger, and a shell side discharge outlet 22 of the heat exchanger is communicated with the flash tank 30 through a shell side discharge pipeline L2 of the heat exchanger;
the flash tank 30 is used for vaporizing raw materials and separating two phases, the tank body is internally divided into an upper layer filling cavity 30A and a lower layer material cavity 30B, the top of the lower layer material cavity 30B is provided with a flash material inlet 31, the bottom of the lower layer material cavity is provided with a flash material outlet 32, and the flash material inlet 31 is communicated with a shell pass discharge pipeline L2 and used for receiving materials from the shell pass of the vapor phase heat exchanger 20; the flash material outlet 32 is communicated with a flash liquid discharge pipeline L3 and is communicated with the solvent evaporator 40 through the flash liquid discharge pipeline L3, and the top of the flash tank 30 is provided with a flash vapor discharge pipeline L6 for discharging steam;
the solvent evaporator 40 is used for evaporating the solvent, an evaporator shell side feed inlet 41 is connected with a flash material outlet 32 of the flash tank 30 through a flash liquid discharge pipeline L3, and an evaporator shell side discharge outlet 42 is communicated with a tube side feed inlet 23 of the vapor-phase heat exchanger 20 through a gas-phase material output pipeline L4; the evaporator tube pass feeding port 43 and the evaporator tube pass discharging port 44 of the solvent evaporator 40 are externally connected with a high-temperature steam pipeline;
the condenser 50 is communicated with the vapor phase heat exchanger 20 and is used for collecting gas phase o-xylene from the vapor phase heat exchanger 20 and condensing the gas phase o-xylene into liquid for recovery, and the gas phase o-xylene comprises a condenser tube side feed inlet 51, a condenser tube side discharge outlet 52, a condenser shell side feed inlet 53 and a condenser shell side discharge outlet 54; wherein, the condenser shell pass feed inlet 53 and the condenser shell pass discharge outlet 54 are communicated with an external condensate pipeline; the condenser tube side feed port 51 is communicated with the heat exchanger tube side discharge port 24 of the vapor phase heat exchanger 20 through a gas phase o-xylene tube line L5, and the condenser tube side discharge port 52 is communicated with the o-xylene recovery tank 60 through a line.
A heat exchanger feed pump L1A is arranged on the heat exchanger shell side feed pipeline L1;
a flash evaporation discharging pump L3A is arranged on the flash evaporation liquid discharging pipeline L3;
the flash tank 30 and the solvent evaporator 40 are both connected with a vacuum device through vacuum pipelines.
The utility model discloses an evaporation equipment for ortho-xylene adopts the combination of flash tank and solvent evaporator, has realized the continuous evaporation separation of this three of ortho-xylene, acetone and acrylonitrile, and the high-temperature gas that the vapor phase heat exchanger produced through the solvent evaporator preheats the material that gets into in the vapor phase heat exchanger, and the waste heat that produces in the evaporation process is not only extravagant, but also has carried out abundant recycle, has very good energy-conserving effect. And the synchronous separation of o-xylene, acetone and acrylonitrile is realized through different temperature control, the working time is greatly shortened, and the working efficiency is improved.
Drawings
FIG. 1: the utility model is a schematic structural diagram of an evaporation device for ortho-xylene;
in the figure, 10, a evaporation feed tank, 11, a raw material inlet, 12, a raw material outlet, 20, a vapor phase heat exchanger, 21, a heat exchanger shell pass feed inlet, 22, a heat exchanger shell pass discharge outlet, 23, a heat exchanger tube pass feed inlet, 24, a heat exchanger tube pass discharge outlet, 30, a flash tank, 30A, an upper layer packing cavity, 30B, a lower layer material cavity, 31, a flash material inlet, 32, a flash material outlet, L1, a heat exchanger shell pass feed pipeline, L1A, a heat exchanger feed pump, L2, a heat exchanger shell pass discharge pipeline, L3, a flash liquid discharge pipeline, L3A, a flash discharge pump, L4, a vapor phase material output pipeline, L5, a vapor phase ortho-xylene pipeline, L6, a flash vapor phase discharge pipeline, 40, a solvent evaporator, 41, an evaporator shell pass feed inlet, 42, an evaporator shell pass discharge outlet, 43, an evaporator tube pass feed inlet, 44, an evaporator tube pass discharge outlet, 50. a condenser 51, a condenser tube side feed inlet, 52, a condenser tube side discharge outlet, 53, a condenser shell side feed inlet, 54, a condenser shell side discharge outlet, 60 and an o-xylene recovery tank.
Detailed Description
The following description is provided with reference to the accompanying drawings, which show the specific structural components, design principles, and operation and application processes of the evaporation apparatus of the present invention, so as to enable those skilled in the art to more fully understand the present invention.
Examples
The embodiment relates to evaporation equipment for ortho-xylene in diacetone production, which mainly comprises a evaporation feed tank 10, a vapor phase heat exchanger 20, a flash tank 30 and a solvent evaporator 40, wherein the top of the evaporation feed tank 10 is provided with a raw material inlet 11, and raw materials enter the evaporation feed tank 10 through the raw material inlet 11; the bottom of the evaporation feed tank 10 is provided with a raw material outlet 12, and the raw material is fed into the shell side of the vapor-phase heat exchanger 20 through the raw material outlet 12 via a heat exchanger shell side feed pipeline L1 and a heat exchanger feed pump L1A; the vapor-phase heat exchanger 20 is used for preheating raw materials and comprises a heat exchanger shell pass feed inlet 21, a heat exchanger shell pass discharge outlet 22, a heat exchanger tube pass feed inlet 23 and a heat exchanger tube pass discharge outlet 24; a shell side feed inlet 21 of the heat exchanger is communicated with a raw material outlet 12 of the evaporation feed tank 10 through a shell side feed pipeline L1 of the heat exchanger, and a shell side discharge outlet 22 of the heat exchanger is communicated with the flash tank 30 through a shell side discharge pipeline L2 of the heat exchanger; the flash tank 30 is used for vaporizing raw materials and separating two phases, the tank body is internally divided into an upper layer filling cavity 30A and a lower layer material cavity 30B, the top of the lower layer material cavity 30B is provided with a flash material inlet 31, the bottom of the lower layer material cavity is provided with a flash material outlet 32, and the flash material inlet 31 is communicated with a shell pass discharge pipeline L2 and used for receiving materials from the shell pass of the vapor phase heat exchanger 20; the flash material outlet 32 is communicated with a flash liquid discharge pipeline L3 and is communicated with the solvent evaporator 40 through the flash liquid discharge pipeline L3, and the top of the flash tank 30 is provided with a flash vapor discharge pipeline L6 for discharging steam. The solvent evaporator 40 is used for evaporating the solvent, the shell pass of the solvent evaporator is communicated with the flash tank 30, and the tube pass of the solvent evaporator is externally connected with high-temperature steam; a flash liquid discharge pipeline L3 and a flash discharge pump L3A are connected between an evaporator shell side feed inlet 41 of the shell side and a flash material outlet 32 of the flash tank 30, and an evaporator shell side discharge outlet 42 is communicated with a tube side feed inlet 23 of the vapor-phase heat exchanger 20 through a gas phase material output pipeline L4; the evaporator tube side feed inlet 43 of the tube side is connected with a high-temperature steam inlet, and the evaporator tube side discharge outlet 44 is connected with a high-temperature steam outlet. The condenser 50 is communicated with the vapor phase heat exchanger 20 and is used for collecting gas phase o-xylene from the vapor phase heat exchanger 20 and condensing the gas phase o-xylene into liquid for recovery, and the gas phase o-xylene comprises a condenser tube side feed inlet 51, a condenser tube side discharge outlet 52, a condenser shell side feed inlet 53 and a condenser shell side discharge outlet 54; wherein, the condenser shell pass feed inlet 53 and the condenser shell pass discharge outlet 54 are communicated with an external condensate pipeline; the condenser tube side feed port 51 is communicated with the heat exchanger tube side discharge port 24 of the vapor phase heat exchanger 20 through a gas phase o-xylene tube line L5, and the condenser tube side discharge port 52 is communicated with the o-xylene recovery tank 60 through a line. The flash tank 30 and the solvent evaporator 40 are both connected with a vacuum device through vacuum pipelines.
The raw material (containing diacetone acrylamide ortho-xylene solution) in the steam feed tank 10 is sent into the shell pass of the vapor phase heat exchanger 20 through a pipeline, the tube pass of the vapor phase heat exchanger 20 is communicated with the shell pass of the solvent evaporator 40, the high-temperature vaporized ortho-xylene is discharged from the shell pass of the solvent evaporator 40 and then enters the tube pass of the vapor phase heat exchanger 20, and the heat exchange is carried out on the raw material in the shell pass of the vapor phase heat exchanger 20; the preheated raw materials enter the flash tank 30 through a pipeline, the materials are vaporized in the flash tank 30 in a flash manner, and separated gaseous materials (mainly acetone and acrylonitrile) are collected through a flash vapor state discharge pipeline L6 at the top of the flash tank 30. The separated liquid material enters the shell pass of the solvent evaporator 40 through a pipeline, the tube pass of the solvent evaporator 40 is externally connected with high-temperature steam, the material in the shell pass of the solvent evaporator 40 is separated from the o-xylene in the shell pass thereof under the action of the high-temperature steam in the tube pass to generate gas-phase o-xylene, and the gas-phase o-xylene enters the tube pass of the vapor-phase heat exchanger 20 through a gas-phase material output pipeline L4, exchanging heat with the raw material in the shell pass of the vapor-phase heat exchanger 20, allowing the gas-phase o-xylene subjected to heat exchange to enter the condenser 50 through the heat exchanger tube pass discharge port 24, the gas-phase o-xylene pipeline L5 and the condenser tube pass feed inlet 51 of the vapor-phase heat exchanger 20, communicating the shell pass of the condenser 50 with an external condensate water pipeline, under the action of external condensate water, the gas-phase o-xylene in the tube pass of the condenser 50 is condensed, and the condensed liquid o-xylene is collected into an o-xylene recovery tank through a discharge hole 52 of the tube pass of the condenser.
Claims (4)
1. The evaporation equipment for the ortho-xylene is characterized by comprising a evaporation feed tank, a vapor phase heat exchanger, a flash tank, a solvent evaporator, a condenser and an ortho-xylene recovery tank; wherein
The evaporation feed tank is used for containing raw materials, the top of the evaporation feed tank is provided with a raw material inlet, and the bottom of the evaporation feed tank is provided with a raw material outlet;
the vapor-phase heat exchanger is used for preheating the raw materials and comprises a heat exchanger shell pass feeding hole, a heat exchanger shell pass discharging hole, a heat exchanger tube pass feeding hole and a heat exchanger tube pass discharging hole; the shell side feed inlet of the heat exchanger is communicated with the raw material outlet of the evaporation feed tank through a shell side feed pipeline of the heat exchanger, and the shell side discharge outlet of the heat exchanger is communicated with the flash tank through a shell side discharge pipeline of the heat exchanger;
the flash tank is used for realizing vaporization and two-phase separation of raw materials, the inside of the tank body of the flash tank is divided into an upper-layer filling cavity and a lower-layer material cavity, the top of the lower-layer material cavity is provided with a flash material inlet, the bottom of the lower-layer material cavity is provided with a flash material outlet, and the flash material inlet is communicated with a shell pass discharge pipeline and used for receiving materials from the shell pass of the vapor-phase heat exchanger; the flash material outlet is communicated with a flash liquid discharging pipeline and is communicated with the solvent evaporator through the flash liquid discharging pipeline, and the top of the flash tank is provided with a flash steam discharging pipeline for discharging steam;
the solvent evaporator is used for evaporating a solvent, an evaporator shell pass feed inlet is connected with a flash material outlet of the flash tank through a flash liquid discharge pipeline, and an evaporator shell pass discharge outlet is communicated with a tube pass feed inlet of the vapor-phase heat exchanger through a vapor-phase material output pipeline; the evaporator tube pass feeding port and the evaporator tube pass discharging port of the solvent evaporator are externally connected with a high-temperature steam pipeline;
the condenser is communicated with the vapor-phase heat exchanger and is used for collecting gas-phase o-xylene from the vapor-phase heat exchanger and condensing the gas-phase o-xylene into liquid for recovery, and the condenser comprises a condenser tube pass feeding port, a condenser tube pass discharging port, a condenser shell pass feeding port and a condenser shell pass discharging port; the condenser shell pass feeding port and the condenser shell pass discharging port are communicated with an external condensate pipeline; the condenser tube side feed inlet is communicated with a heat exchanger tube side discharge port of the vapor phase heat exchanger through a gas adjacent xylene pipeline, and the condenser tube side discharge port is communicated with an adjacent xylene recovery tank through a pipeline.
2. The vaporization apparatus for ortho-xylene according to claim 1, wherein,
and a heat exchanger feeding pump is arranged on the heat exchanger shell side feeding pipeline.
3. The vaporization apparatus for ortho-xylene according to claim 1, wherein,
and a flash evaporation discharging pump is arranged on the flash evaporation liquid discharging pipeline.
4. The vaporization apparatus for ortho-xylene according to claim 1, wherein,
the flash tank and the solvent evaporator are both externally connected with vacuum equipment through vacuum pipelines.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921606102.2U CN210656743U (en) | 2019-09-25 | 2019-09-25 | Evaporation device for ortho-xylene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921606102.2U CN210656743U (en) | 2019-09-25 | 2019-09-25 | Evaporation device for ortho-xylene |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN210656743U true CN210656743U (en) | 2020-06-02 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201921606102.2U Active CN210656743U (en) | 2019-09-25 | 2019-09-25 | Evaporation device for ortho-xylene |
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| Country | Link |
|---|---|
| CN (1) | CN210656743U (en) |
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2019
- 2019-09-25 CN CN201921606102.2U patent/CN210656743U/en active Active
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