CN112439304A - Method for utilizing energy of feed lean water of absorption tower of acrylonitrile device - Google Patents
Method for utilizing energy of feed lean water of absorption tower of acrylonitrile device Download PDFInfo
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- CN112439304A CN112439304A CN201910837016.0A CN201910837016A CN112439304A CN 112439304 A CN112439304 A CN 112439304A CN 201910837016 A CN201910837016 A CN 201910837016A CN 112439304 A CN112439304 A CN 112439304A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
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Abstract
The invention relates to a method for utilizing energy of feed lean water of an absorption tower of an acrylonitrile device, which comprises the steps of feeding the lean water pumped out from the side line of a recovery tower and tower bottom liquid pumped out from a tower bottom of the absorption tower into a heat exchanger for heat exchange; then the lean water is sent to the top of the absorption tower from the lean water outlet pipeline of the heat exchanger, and the tower bottom liquid of the absorption tower is sent to a recovery tower from the rich water outlet pipeline of the heat exchanger. The method for utilizing the energy of the lean water fed into the absorption tower of the acrylonitrile device can fully utilize the heat of the lean water, and replaces the original mode of heating the tower bottom liquid of the absorption tower through steam and cooling the lean water through cooling water, thereby reducing the energy consumption.
Description
Technical Field
The invention belongs to the technical field of acrylonitrile production, and particularly relates to a method for utilizing energy of feed lean water of an absorption tower of an acrylonitrile device.
Background
In the acrylonitrile device, reaction gas cooled by a cooler after a quench tower enters the bottom of an absorption tower and is subjected to countercurrent absorption with water, the operation temperature of the top of the absorption tower is about 33-41 ℃, and the temperature of a tower kettle is 8-20 ℃. The tower bottom liquid of the absorption tower needs to be pumped to the recovery tower through the tower bottom liquid (rich water) of the absorption tower, the tower top operating temperature of the recovery tower is about 84-92 ℃, and the tower bottom is about 116-. In the prior art, the temperature of the tower bottom liquid of the absorption tower is increased by adopting a steam heating mode so as to meet the temperature condition of entering the recovery tower.
Meanwhile, the water for countercurrent absorption of the reaction gas entering the absorption tower comes from the side line of the recovery tower, and the lean water is generally extracted from the side line of the recovery tower and sent to the top of the absorption tower so as to realize countercurrent absorption of the reaction gas. However, the temperature of the lean water extracted from the side line of the recovery tower is about 116 ℃ to 124 ℃, and the temperature is still about 92 ℃ to 99 ℃ after passing through a dehydrocyanation tower reboiler and a finished product tower reboiler. The operation temperature of the top of the absorption tower is about 33-41 ℃, that is, the lean water extracted from the side line of the recovery tower needs to be cooled before entering the top of the absorption tower, and the lean water is cooled by circulating cooling water in the prior art.
In summary, in the prior art, steam is required to heat up the tower bottom liquid of the absorption tower, and circulating cooling water is required to cool down the lean water extracted from the side line of the recovery tower, so that the consumption of steam and circulating water is greatly increased, and a large amount of heat in the lean water is wasted.
Disclosure of Invention
The invention aims to provide a method for utilizing energy of feed lean water of an absorption tower of an acrylonitrile device, which solves the problem of heat waste in the lean water.
In order to achieve the purpose, the invention provides a method for utilizing energy of feed lean water of an absorption tower of an acrylonitrile device, which comprises the following steps:
feeding the lean water pumped out from the side line of the recovery tower and the tower bottom liquid pumped out from the tower bottom of the absorption tower into a heat exchanger for heat exchange;
then the lean water is sent to the top of the absorption tower from the lean water outlet pipeline of the heat exchanger, and the tower bottom liquid of the absorption tower is sent to a recovery tower from the rich water outlet pipeline of the heat exchanger.
According to one aspect of the invention, a three-way regulating valve is arranged on a pipeline for conveying the lean water extracted from the side line of the absorption tower to the heat exchanger, the three-way regulating valve divides the lean water into a first lean water flow and a second lean water flow, the first lean water flow enters the heat exchanger, and the second lean water flow bypasses the heat exchanger and is mixed with the first lean water flow flowing out from the lean water outlet pipeline of the heat exchanger and then is conveyed to the top of the absorption tower.
According to one aspect of the invention, a liquid level controller for controlling the tower liquid flow of the absorption tower and a temperature controller connected with the three-way regulating valve are arranged on the rich water outlet pipeline of the heat exchanger.
According to one aspect of the invention, the temperature of the tower bottom liquid of the absorption tower is increased from 15-34 ℃ to 58-74 ℃ after the heat exchange.
According to one aspect of the invention, preferably, the temperature of the tower bottom liquid of the absorption tower is increased from 21-26 ℃ to 64-68 ℃ after the heat exchange.
According to one aspect of the invention, the temperature of the first and second streams of lean water after mixing is 55-75 ℃.
According to one aspect of the present invention, preferably, the temperature of the first and second streams of lean water after mixing is in the range of 62-68 ℃.
According to one aspect of the present invention, the temperature of the lean water withdrawn from the side line of the absorption tower is 85-105 ℃.
According to one aspect of the invention, the first lean water and the second lean water are mixed and then divided into a first lean water flow and a second lean water flow by a second three-way regulating valve;
the first lean water flow is cooled by an absorption water cooler and then is sent to the top of the absorption tower;
and the second water-poor stream is sent to the top of the recovery tower through a solvent water cooler.
According to one aspect of the present invention, the temperature of the first lean water stream is reduced from 55-71 ℃ to 30-44 ℃ after passing through the absorption water cooler;
the temperature of the second lean water stream is reduced from 55-71 ℃ to 41-57 ℃ after passing through the solvent water cooler;
and a flow controller connected with the second tee joint is arranged on a pipeline from the absorption water cooler to the bottom of the absorption tower and is used for controlling the flow of the first lean water flow entering the absorption water cooler and finally sent to the top of the absorption tower.
According to one aspect of the present invention, the lean water withdrawn from the side of the recovery column is fed to the top of the absorption column as washing water to be brought into countercurrent contact with the reaction gas, and the operation temperature at the top of the absorption column is low and lower than the lean water temperature. And the tower bottom liquid of the absorption tower needs to be pumped into a recovery tower for further treatment, the tower bottom liquid of the absorption tower has lower temperature, and the operation temperature of the recovery tower is higher than that of the tower bottom liquid of the absorption tower. According to the scheme of the invention, high-temperature lean water and low-temperature absorption tower bottom liquid are sent to a heat exchanger for heat exchange, so that the temperature of the lean water is reduced and sent to the top of the absorption tower, and the temperature of the absorption tower bottom liquid is increased and sent to the absorption tower. Compared with the mode that the tower bottom liquid of the absorption tower needs to be heated up through steam and the lean water needs to be cooled down through condensed water in the prior art, the energy of the lean water is fully utilized, the utilization rate of the lean water is improved, and the energy consumption is reduced.
According to one scheme of the invention, a liquid level controller for controlling the tower bottom liquid flow of the absorption tower and a temperature controller connected with a three-way regulating valve are arranged on a rich water outlet pipeline of the heat exchanger. Thus, in the actual operation process, the amount of the tower bottom liquid of the absorption tower sent to the heat exchanger and the amount of the first strand of lean water sent to the heat exchanger can be controlled according to the finally required temperature of the tower bottom liquid of the absorption tower entering the recovery tower, so that the temperature can be accurately controlled.
According to one scheme of the invention, a flow controller connected with a second three-way valve is arranged on a pipeline between the self-absorption water cooler and the top of the absorption tower and is used for controlling the flow of the first lean water flow finally sent to the top of the absorption tower. Therefore, the accurate control of the feeding amount of the top of the absorption tower can be realized, and the absorption effect of the gas in the absorption tower is ensured while the energy is saved.
Drawings
FIG. 1 schematically shows a flow diagram of a process for energy utilization of a lean water feed to an absorption column of an acrylonitrile plant according to one embodiment of the present invention.
The reference numerals in the drawings represent the following meanings:
1. an absorption tower. 2. And (4) recovering a side line of the tower. 3. A heat exchanger. 4. And (5) a recovery tower. 5. Three-way regulating valve. 6. The first stream is lean in water. 7. The second stream is lean. 8. A liquid level controller. 9. A temperature controller. 10. And a second three-way regulating valve. 11. A first lean water stream. 12. A second lean water stream. 13. An absorption water cooler. 14. A solvent water cooler. 15. A flow controller.
Detailed Description
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the embodiments will be briefly described below. It is obvious that the drawings in the following description are only some embodiments of the invention, and that for a person skilled in the art, other drawings can be derived from them without inventive effort.
In describing embodiments of the present invention, the terms "longitudinal," "lateral," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," and the like are used in an orientation or positional relationship that is based on the orientation or positional relationship shown in the associated drawings, which is for convenience and simplicity of description only, and does not indicate or imply that the referenced device or element must have a particular orientation, be constructed and operated in a particular orientation, and thus, the above-described terms should not be construed as limiting the present invention.
The present invention is described in detail below with reference to the drawings and the specific embodiments, which are not repeated herein, but the embodiments of the present invention are not limited to the following embodiments.
As shown in FIG. 1, the method for utilizing the energy of the feed water-poor of the absorption tower of the acrylonitrile device comprises the following steps: and (3) feeding the lean water pumped out from the side line 2 of the recovery tower and the tower bottom liquid pumped out from the tower bottom of the absorption tower 1 into a heat exchanger 3 for heat exchange. Then the lean water is sent to the top of the absorption tower 1 from the lean water outlet pipeline of the heat exchanger 2, and the tower bottom liquid of the absorption tower 1 is sent to the recovery tower from the rich water outlet pipeline of the heat exchanger 3.
Specifically, in the acrylonitrile plant, the lean water withdrawn from the side 2 of the recovery column needs to be fed to the top of the absorption column 1 as washing water to be brought into countercurrent contact with the reaction gas, and the operation temperature at the top of the absorption column is low and lower than the lean water temperature. And the tower bottom liquid of the absorption tower needs to be pumped into a recovery tower for further treatment, the tower bottom liquid of the absorption tower has lower temperature, and the operation temperature of the recovery tower is higher than that of the tower bottom liquid of the absorption tower. According to the scheme of the invention, high-temperature lean water and low-temperature absorption tower bottom liquid are sent to the heat exchanger 3 for heat exchange, so that the temperature of the lean water is reduced and sent to the top of the absorption tower, and the temperature of the absorption tower bottom liquid is increased and sent to the absorption tower. Compared with the mode that the tower bottom liquid of the absorption tower needs to be heated up through steam and the lean water needs to be cooled down through condensed water in the prior art, the energy of the lean water is fully utilized, the utilization rate of the lean water is improved, and the energy consumption is reduced.
According to one embodiment of the present invention, a three-way regulating valve 5 is provided on a line for feeding the lean water extracted from the side stream 2 of the recovery column to the heat exchanger 3 in the present invention. The three-way regulating valve 5 divides the lean water extracted from the side line of the recovery tower into a first part of lean water 6 and a second part of lean water 7, wherein the first part of lean water 6 is sent to the heat exchanger 3 to exchange heat with tower bottom liquid from the tower bottom of the absorption tower 1. The second stream of lean water 7 bypasses the heat exchanger 3 and is mixed with the first stream of lean water 6 flowing out from the lean water outlet pipeline of the heat exchanger 3 and then is sent to the top of the absorption tower 1.
In the invention, a liquid level controller 8 for controlling the tower bottom liquid flow of the absorption tower and a temperature controller 9 connected with a three-way regulating valve 5 are arranged on a rich water outlet pipeline of a heat exchanger 3. In this way, in the actual operation process, the amount of the tower bottom liquid of the absorption tower sent to the heat exchanger 3 and the amount of the first strand of lean water 6 sent to the heat exchanger 3 can be controlled according to the temperature which is finally required to be reached when the tower bottom liquid of the absorption tower enters the recovery tower, so that the temperature can be accurately controlled.
In the invention, the temperature of the tower bottom liquid of the absorption tower after passing through the heat exchanger 3 is increased to 58-74 ℃ from the original 13-34 ℃. Preferably, the temperature of the tower bottom liquid of the absorption tower after passing through the heat exchanger 3 is increased from the original 18-29 ℃ to 61-71 ℃. More preferably, the temperature of the tower bottom liquid of the absorption tower after passing through the heat exchanger 3 is increased from the original 21-26 ℃ to 64-68 ℃.
In the present invention, the temperature of the lean water withdrawn from the recovery column side line 2 is 85 ℃ to 105 ℃. Preferably, the temperature of the lean water withdrawn from the recovery column side line 2 is 90 ℃ to 100 ℃. More preferably, the temperature of the lean water withdrawn from the recovery column side line 2 is from 92 ℃ to 99 ℃.
In the present invention, the temperature of the first stream of lean water 6 after passing through the heat exchanger 3 and mixing with the second stream of lean water 7 is 55-75 ℃. Preferably, the temperature of the first stream of lean water 6 after passing through the heat exchanger 3 and mixing with the second stream of lean water 7 is 60-70 ℃. More preferably, the temperature of the first stream of lean water 6 after passing through the heat exchanger 3 and mixing with the second stream of lean water 7 is 62-68 ℃.
As shown in FIG. 1, the tower bottom liquid of the absorption tower of the present invention is sent to the recovery tower after passing through the heat exchanger 3, and the first lean water 6 and the second lean water 7 are mixed and sent to the top of the absorption tower 1. In the invention, a second three-way valve 10 is arranged on a pipeline for mixing the first lean water 6 and the second lean water 7 and sending the mixture to the top of the absorption tower 1, and the first lean water 6 and the second lean water 7 are mixed and then are divided into a first lean water flow 11 and a second lean water flow 12 through the second three-way valve 10. The first lean water stream 11 is cooled by an absorption water cooler 13 and then sent to the top of the absorption tower. The second lean aqueous stream 12 is passed through a solvent water cooler 14 and then to the top of the recovery column.
In the invention, the temperature of the first lean water stream 11 is reduced to 30-44 ℃ from 55-71 ℃ after being cooled by the absorption water cooler 13. Preferably, the temperature of the first lean water stream 11 is reduced from 58 ℃ to 69 ℃ to 33 ℃ to 41 ℃ after being cooled by the absorption water cooler 13. More preferably, the temperature of the first lean water stream 11 is reduced from 62 ℃ to 66 ℃ to 35 ℃ to 39 ℃ after being cooled by the absorption water cooler 13.
In the present invention, the temperature of the second lean water stream 12 is reduced from 55 ℃ to 71 ℃ to 41 ℃ to 57 ℃ after passing through the solvent water cooler 14. Preferably, the temperature of the second lean water stream 12 is reduced from 58 ℃ to 69 ℃ to 43 ℃ to 54 ℃ after passing through the solvent water cooler 14. More preferably, the temperature of the second lean water stream 12 is reduced from 62 ℃ to 66 ℃ to 45 ℃ to 51 ℃ after passing through the solvent water cooler 14.
In the present invention, a flow controller 15 connected to the second three-way valve 10 is provided in the line from the absorption water cooler 13 to the top of the absorption tower, for controlling the flow rate of the first lean water stream 11 finally sent to the top of the absorption tower. Therefore, the accurate control of the feeding amount of the top of the absorption tower can be realized, and the absorption effect of the gas in the absorption tower is ensured while the energy is saved.
The above description is only one embodiment of the present invention, and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A method for utilizing energy of feed lean water of an absorption tower of an acrylonitrile device comprises the following steps:
feeding the lean water pumped out from the side line of the recovery tower and the tower bottom liquid pumped out from the tower bottom of the absorption tower into a heat exchanger for heat exchange;
then the lean water is sent to the top of the absorption tower from the lean water outlet pipeline of the heat exchanger, and the tower bottom liquid of the absorption tower is sent to a recovery tower from the rich water outlet pipeline of the heat exchanger.
2. The method for utilizing the energy of the lean water fed from the absorption tower of the acrylonitrile device as claimed in claim 1, wherein a three-way regulating valve is arranged on a pipeline for feeding the lean water extracted from the side line of the absorption tower to a heat exchanger, the three-way regulating valve divides the lean water into a first lean water stream and a second lean water stream, the first lean water stream enters the heat exchanger, and the second lean water stream bypasses the heat exchanger and is mixed with the first lean water stream flowing out from the lean water outlet pipeline of the heat exchanger and then is fed to the top of the absorption tower.
3. The method for utilizing the energy of the feed water-poor of the absorption tower of the acrylonitrile device as claimed in claim 2, wherein a liquid level controller for controlling the tower bottom liquid flow of the absorption tower and a temperature controller connected with the three-way regulating valve are arranged on the rich water outlet pipeline of the heat exchanger.
4. The method for utilizing the energy of the feed lean water of the absorption tower of the acrylonitrile device as claimed in claim 3, wherein the temperature of the tower bottom liquid of the absorption tower is increased from 15-34 ℃ to 58-74 ℃ after the heat exchange.
5. The method for utilizing the energy of the feed lean water of the absorption tower of the acrylonitrile device as claimed in claim 4, wherein the temperature of the tower bottom liquid of the absorption tower is preferably raised from 21-26 ℃ to 64-68 ℃ after the heat exchange.
6. The acrylonitrile plant absorption tower feed water-deficient energy utilization process of claim 4 or 5, wherein the temperature of the first stream of lean water and the second stream of lean water after mixing is 55-75 ℃.
7. The acrylonitrile plant absorption tower feed water-deficient energy utilization process according to claim 6, wherein the temperature of the first stream of lean water and the second stream of lean water after mixing is preferably 62-68 ℃.
8. The acrylonitrile plant absorption tower feed water-depleted energy utilization method according to claim 7, characterized in that the temperature of the lean water withdrawn from the side of the absorption tower is 85-105 ℃.
9. The acrylonitrile plant absorption tower feed water-depleted energy utilization method according to claim 2 or 8, wherein the first lean water and the second lean water are mixed and then divided into a first lean water stream and a second lean water stream by a second three-way regulating valve;
the first lean water flow is cooled by an absorption water cooler and then is sent to the top of the absorption tower;
and the second water-poor stream is sent to the top of the recovery tower through a solvent water cooler.
10. The acrylonitrile plant absorber feed water-depleted energy utilization process of claim 9, wherein the temperature of the first water-depleted stream is reduced from 55-71 ℃ to 30-44 ℃ after passing through the absorption water cooler;
the temperature of the second lean water stream is reduced from 55-71 ℃ to 41-57 ℃ after passing through the solvent water cooler;
and a flow controller connected with the second tee joint is arranged on a pipeline from the absorption water cooler to the bottom of the absorption tower and is used for controlling the flow of the first lean water flow entering the absorption water cooler and finally sent to the top of the absorption tower.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201910837016.0A CN112439304A (en) | 2019-09-05 | 2019-09-05 | Method for utilizing energy of feed lean water of absorption tower of acrylonitrile device |
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| CN201910837016.0A CN112439304A (en) | 2019-09-05 | 2019-09-05 | Method for utilizing energy of feed lean water of absorption tower of acrylonitrile device |
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| CN112439304A true CN112439304A (en) | 2021-03-05 |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4434029A (en) * | 1980-12-03 | 1984-02-28 | Asahi Kasei Kogyo Kabushiki Kaisha | Process for producing unsaturated nitrile |
| US6364938B1 (en) * | 2000-08-17 | 2002-04-02 | Hamilton Sundstrand Corporation | Sorbent system and method for absorbing carbon dioxide (CO2) from the atmosphere of a closed habitable environment |
| CN103463955A (en) * | 2013-09-16 | 2013-12-25 | 湖南大学 | Technology for separating and recovering carbon dioxide from industrial tail gas |
| CN110152453A (en) * | 2019-05-16 | 2019-08-23 | 清华大学 | Use the method and apparatus of sour gas in solvent absorption captured gas mixture |
-
2019
- 2019-09-05 CN CN201910837016.0A patent/CN112439304A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4434029A (en) * | 1980-12-03 | 1984-02-28 | Asahi Kasei Kogyo Kabushiki Kaisha | Process for producing unsaturated nitrile |
| US6364938B1 (en) * | 2000-08-17 | 2002-04-02 | Hamilton Sundstrand Corporation | Sorbent system and method for absorbing carbon dioxide (CO2) from the atmosphere of a closed habitable environment |
| CN103463955A (en) * | 2013-09-16 | 2013-12-25 | 湖南大学 | Technology for separating and recovering carbon dioxide from industrial tail gas |
| CN110152453A (en) * | 2019-05-16 | 2019-08-23 | 清华大学 | Use the method and apparatus of sour gas in solvent absorption captured gas mixture |
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