CN218811220U - Ammonia recovery system of phenol ammonia recovery device - Google Patents
Ammonia recovery system of phenol ammonia recovery device Download PDFInfo
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- CN218811220U CN218811220U CN202223159695.7U CN202223159695U CN218811220U CN 218811220 U CN218811220 U CN 218811220U CN 202223159695 U CN202223159695 U CN 202223159695U CN 218811220 U CN218811220 U CN 218811220U
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Abstract
The application relates to an ammonia recovery system of a phenol-ammonia recovery device, which comprises a deacidification tower, an deamination tower, an extraction tower, a water tower and a phenol tower, wherein the deacidification tower is communicated with the deamination tower, the deamination tower is communicated with the extraction tower, a deamination water cooler, a static mixer and an oil-water separator are connected in series between the deamination tower and the extraction tower, the extraction tower is communicated with the water tower, the water tower is communicated with a diluted phenol water-gas water separation pipeline, and the diluted phenol water is communicated with a biochemical treatment device; the oil-water separator is also communicated with the phenol tower and is connected with a No. 2 extract tank in series, the upper end of the phenol tower is provided with a reflux pipeline, a solvent circulating tank is arranged on the reflux pipeline, and the solvent circulating tank is communicated with the extraction tower; the extraction tower is communicated with the No. 1 extract tank, and the No. 1 extract tank is communicated with a pipeline between the deamination water cooler and the static mixer; the top of the water tower is provided with a condensation port which is communicated with an extract inlet of a condenser, and the condenser is communicated with a No. 1 extract tank. This application is retrieved outward and is sent out washing water technology to current phenol ammonia and improves, replaces rare phenol water to send to transform cooling device through the deamination water after using the deacidification deamination, improves phenol ammonia recovery unit's processing load and efficiency, reduces running cost.
Description
Technical Field
The application relates to an ammonia recovery system of a phenol ammonia recovery device.
Background
The wastewater treatment process of the phenol ammonia recovery device in the prior art has the following defects: 1. the washing water is qualified dilute phenol water, and the solvent and steam consumption in the wastewater treatment process is high, so that the cost is high. 2. In the wastewater treatment process of the phenol ammonia recovery device in the prior art, the wastewater circulation volume is large due to the large amount of washing water delivered outside, and the wastewater treatment efficiency of the phenol ammonia recovery device is low. 3. In the wastewater treatment process of the phenol-ammonia recovery device in the prior art, the load of an extraction and solvent recovery system is high, so that the total phenol content and COD content of dilute phenol water are high. 4. In the wastewater treatment process of the phenol-ammonia recovery device in the prior art, produced substances (solvent and water) at the top of a water tower enter a solvent circulating tank after being condensed, so that the purity of the solvent in the solvent circulating tank is reduced, and the dephenolizing effect of solvent extraction is reduced. 5. In the wastewater treatment process of the phenol-ammonia recovery device in the prior art, after a solvent with water enters a phenol tower as the top reflux of the phenol tower, the phenol tower is over-heated and over-pressurized, the purity of the solvent extracted from the gas phase at the top of the phenol tower is reduced, the purity of the solvent in a solvent circulation tank is further influenced, and the extraction effect is deteriorated. 6. In the wastewater treatment process of the phenol-ammonia recovery device in the prior art, the tower top of the phenol tower exceeds Wen Chaoya due to the fact that the solvent contains water, and the solvent consumption is high. 7. In the wastewater treatment process of the phenol-ammonia recovery device in the prior art, during the system startup and shutdown and the cold circulation process, the wastewater carries the solvent of the extraction system to return to the gas water-gas device, so that the solvent loss is high. 8. The wastewater treatment process of the phenol-ammonia recovery device in the prior art, and in the system starting process, the deamination water is cut to the extraction system, and the solvent recovery system can be heated and pressurized, so that the starting time is long. 9. The wastewater of the phenol-ammonia recovery device in the prior art comes from a gas-water separation device, suspended matters and oil substances contained in the wastewater can be gathered inside the device, particularly, a deacidification and deamination system is taken as a main part, the production capacity and the product quality are influenced, the device is stopped and overhauled when the wastewater is serious, and the production is extremely unstable. 10. The deamination tower kettle wastewater of the phenol ammonia recovery device in the prior art enters a deamination water cooler after being pressurized by a deamination tower kettle phenol water pump, and through research and demonstration and actual operation inspection, when the deamination tower normally operates, the operating pressure is 0.37-0.42Mpa, the deamination water can be directly pressed to a back system by utilizing the self pressure, and the necessity of conveying the deamination water by the deamination tower kettle pump is not adopted.
Disclosure of Invention
In view of the above-mentioned conventional drawbacks, the present application is directed to a phenol ammonia recovery system that improves wastewater treatment capacity and reduces solvent and steam consumption of washing water.
The purpose of the application is realized as follows: an ammonia recovery system of a phenol ammonia recovery device comprises a deacidification tower, a deamination tower, an extraction tower, a water tower and a phenol tower, wherein the outlet end of the deacidification tower is communicated with the inlet end of the deamination tower through a pipeline, the outlet end of the deamination tower is communicated with the inlet end of the extraction tower through a pipeline, a deamination water cooler, a static mixer and an oil-water separator are connected in series on the pipeline, the outlet end of the extraction tower is communicated with the inlet end of the water tower through a pipeline, and the outlet end of the water tower is communicated with a pipeline from dilute phenol water to gas-water separation pipeline and from dilute phenol water to a biochemical treatment device; the outlet end of the oil-water separator is also communicated with the inlet end of the phenol tower through a pipeline, a 2# extract tank is connected in series on the pipeline, the upper end of the phenol tower is provided with a return pipeline, a solvent circulating tank is arranged on the return pipeline, and the outlet end of the solvent circulating tank is communicated with the solvent inlet end of the extraction tower; an extraction opening of the extraction tower is communicated with a feed inlet of the No. 1 extract tank, and a discharge end of the No. 1 extract tank is communicated with a pipeline between the deamination water cooler and the static mixer; and the top of the water tower is provided with a condensation port which is communicated with an extract inlet of the condenser, and an extract outlet of the condenser is communicated with a feed inlet of the No. 1 extract tank.
Furthermore, the washing water of the outward-feeding conversion device and the hypergravity dust removal device is changed from the diluted phenol water at the tower bottom of the water tower into the ammonia removal water at the tower bottom of the ammonia removal tower 2, namely two washing water pipelines which are respectively communicated with the outward-feeding conversion device and the hypergravity dust removal device are led out from a pipeline between the ammonia removal water cooler and the static mixer.
Furthermore, a waste water circulating pipeline is added, when the dilute phenol water is not sent to the biochemical treatment device, the dilute phenol water in the tower kettle of the water tower is sent to the inlet of the extraction system which is changed from a gas-water separation device, namely, the deammoniation water is led out from the pipeline between the deammoniation water cooler and the static mixer and returned to the incoming waste water pipeline to be communicated with the inlet of the extraction system.
Furthermore, a deamination water return to incoming material waste water pipeline is added, namely the outlet end of the water tower is communicated with a pipeline from dilute phenol water to gas water separation and a pipeline from dilute phenol water to a biochemical treatment device, and a simple and efficient process equipment cleaning flow is added.
Furthermore, a deamination tower kettle phenol water pump is connected in series on a pipeline between the extraction tower and the deamination water cooler, a deamination tower kettle phenol water pump bypass pipeline is added on the pipeline in front of the inlet of the deamination tower kettle phenol water pump, and the outlet of the deamination tower kettle phenol water pump bypass pipeline is communicated with the inlet end of the deamination water cooler so as to stop the deamination tower kettle pump during normal operation.
Due to the adoption of the technical scheme, the existing phenol ammonia recycling and washing water external feeding process is improved, and the deacidified and deaminated water is used for replacing dilute phenol water and is fed to the conversion cooling device, so that the treatment load and efficiency of the phenol ammonia recycling device are improved, and the operation cost is reduced; by improving the process flow of a gas phase extraction pipeline at the top of the water tower, the solvent purity of the solvent circulation tank is improved, the extraction effect is improved, and the solvent consumption in the extraction process is reduced; by adding a pipeline communicated from the outlet of the water tower to the inlet of the extraction system, the solvent loss in the cold circulation and start-up and stop processes of the phenol-ammonia recovery device is reduced, the start-up time is shortened, and the operation cost of the phenol-ammonia recovery device is reduced; the deacidification and deamination system is added to clean pipelines, so that the manual cleaning times are reduced, the service cycle of equipment is prolonged, the device is prevented from being stopped and overhauled, and the starting and stopping cost is reduced; through stopping the operation of deamination tower cauldron pump, adopt deamination tower cauldron self pressure to carry deamination water to the back system, reduce the maintenance cost of the maintenance of the power consumption cost of pump operation and equipment operation.
Drawings
The specific structure of the application is given by the following figures and examples:
fig. 1 is a schematic diagram of the system architecture of the present application.
Legend: 1. a deacidification tower; 2. a deamination tower; 3. an extraction tower; 4. a water tower; 5. a phenol column; 6. a deamination water cooler; 7. a static mixer; 8. an oil-water separator; 9. 1# extract tank; 10. a solvent circulation tank; 11. 2# extract tank; 12. a condenser at the top of the water tower; 13. an acid gas line; 14. an ammonia gas line; 15. a ammonia water removal return gas water pipeline; 16. a liquid level regulating valve set of a tower kettle of the water tower; 17. dilute phenol water is delivered to a gas-water separation pipeline; 18. dilute phenol water to the shift converter line; 19. dilute phenol water is delivered to a pipeline of the supergravity dust removal device; 20. dilute phenol water is sent to a biochemical treatment device pipeline; 21. an alkaline liquor feed line of the deamination tower; 22. a condenser outlet line at the top of the water tower; 23. a phenol water pump at the bottom of the deamination tower; 24. the diluted phenol water returns to the inlet pipeline of the static mixer; 25. the deamination water returns to an incoming material waste water pipeline; 26. a phenol water pump bypass pipeline at the bottom of the deamination tower.
Detailed Description
The present application is not limited by the following examples, and specific embodiments may be determined according to the technical solutions and practical situations of the present application.
Example (b): as shown in fig. 1, an ammonia recovery system of a phenol-ammonia recovery device comprises a deacidification tower 1, a deamination tower 2, an extraction tower 3, a water tower 4 and a phenol tower 5, wherein the outlet end of the deacidification tower 1 is communicated with the inlet end of the deamination tower 2 through a pipeline, the outlet end of the deamination tower 2 is communicated with the inlet end of the extraction tower 3 through a pipeline, a deamination water cooler 6, a static mixer 7 and an oil-water separator 8 are connected in series on the pipeline, the outlet end of the extraction tower 3 is communicated with the inlet end of the water tower 4 through a pipeline, and the outlet end of the water tower 4 is communicated with a pipeline 20 from dilute phenol water to a gas-water separation pipeline and from the dilute phenol water to a biochemical treatment device; the outlet end of the oil-water separator 8 is also communicated with the inlet end of the phenol tower 5 through a pipeline, a 2# extract tank 11 is connected in series on the pipeline, the upper end of the phenol tower 5 is provided with a return pipeline, a solvent circulating tank 10 is arranged on the return pipeline, and the outlet end of the solvent circulating tank 10 is communicated with the solvent inlet end of the extraction tower 3; an extraction opening of the extraction tower 3 is communicated with a feed inlet of a No. 1 extract tank 9, and a discharge end of the No. 1 extract tank 9 is communicated with a pipeline between the deamination water cooler 6 and the static mixer 7; the top of the water tower 4 is provided with a condensation port which is communicated with an extract inlet of the condenser, and an extract outlet of the condenser is communicated with a feed inlet of the No. 1 extract tank 9.
Furthermore, the washing water of the external feeding conversion device and the hypergravity dust removal device is changed from the diluted phenol water at the tower bottom of the water tower 4 to the ammonia removal water at the tower bottom of the ammonia removal tower 2, namely two washing water pipelines which are respectively communicated with the external feeding conversion device and the hypergravity dust removal device are led out from the pipeline between the ammonia removal water cooler 6 and the static mixer 7.
Furthermore, a waste water circulating pipeline is added, when the diluted phenol water is not sent to the biochemical treatment device, the diluted phenol water in the tower kettle 4 of the water tower is sent to the inlet of the extraction system changed from the gas-water separation device, namely, the deammoniation water is led out from the pipeline between the deammoniation water cooler 6 and the static mixer 7 and returns to the waste water pipeline 25 of the incoming material to be communicated with the inlet of the extraction system.
Furthermore, a deamination water return to incoming wastewater pipeline is added, namely the outlet end of the water tower 4 is communicated with a diluted phenol water to gas water separation pipeline and a diluted phenol water to biochemical treatment device pipeline 20, so that a simple and efficient process equipment cleaning flow is added.
Further, a deamination tower kettle phenol water pump 23 is connected in series on a pipeline between the extraction tower 3 and the deamination water cooler 6, a deamination tower kettle phenol water pump bypass pipeline 26 is added on the pipeline in front of the inlet of the deamination tower kettle phenol water pump 23, and the outlet of the deamination tower kettle phenol water pump bypass pipeline 26 is communicated with the inlet end of the deamination water cooler 6 so as to stop the deamination tower kettle pump 23 in normal operation.
When the ammonia recovery system of the phenol ammonia recovery device is used, the method comprises the following steps:
step 1, after acid gas and ammonia in wastewater from a gas water separation device are removed by a deacidification tower and a deamination tower, one part of deamination water cooled to 40-60 ℃ by a deamination water cooler is used as washing water and sent to a supergravity dust removal device and a conversion cooling device, and the other part of wastewater is sent to an extraction system;
and 2, recovering the solvent in the wastewater by the water tower, cooling a gas phase containing the solvent and water vapor extracted from the tower top by a condenser at the top of the water tower through a gas phase pipeline at the tower top, and then feeding the gas phase into a No. 1 extract tank. Cooling the diluted phenol water at the tower bottom, and then sending the cooled diluted phenol water to a biochemical treatment device;
step 4, when the device is in cold circulation, the wastewater at the tower bottom of the deamination tower enters a subsequent system after being pressurized by a phenol water pump at the tower bottom of the deamination tower; when the device normally operates, the operation pressure of the tower kettle of the deamination tower is 0.37-0.42MPa, the pump of the tower kettle of the deamination tower is stopped, a bypass of the pump of the tower kettle of the deamination tower is opened, and the deamination water is sent to a rear system by utilizing the self operation pressure of the deamination tower.
Further, in step 3, the wastewater is deacidified and deaminated during cold running, cooled by a deamination water cooler and then returned to a gas water separation device, and phenol water in a tower kettle of the water tower is returned to an inlet pipeline of the extraction system; the deacidification and deamination system heats and boosts the pressure, a water tower heats and boosts the pressure, and a deacidification tower and a deamination tower remove acid gas and ammonia in the wastewater; a water tower recovers a small amount of solvent in the wastewater; adding the solvent in the solvent circulating tank into the extraction tower after the deamination water index at the outlet of the deamination water cooler is qualified; after the solvent phase on the upper part of the extraction tower overflows to the No. 1 extract tank, the diluted phenol water in the tower kettle of the water tower is switched to a biochemical treatment device, the deamination water is switched to an inlet pipeline of an extraction system, the deamination water is mixed and contacted with the solvent from the No. 1 extract tank through a static mixer and enters an oil-water separator, and the solvent phase on the upper layer overflows to the No. 2 extract tank; and (3) starting the temperature and pressure rise of the phenol tower, sending the solvent phase in the No. 2 extract tank to the phenol tower, separating the mixed phenol and the solvent by using a rectification principle, recovering the solvent extracted from the tower top to a solvent circulation tank for recycling, and producing a byproduct of the mixed phenol in the tower kettle.
Further, the application can also realize online cleaning, and the specific measures are as follows:
step 1, when oil stains of a deacidification and deamination system are gathered to cause equipment to deviate from a normal operation index, closing a feed water boundary area valve, switching deamination water at an outlet of a deamination water cooler to a feed wastewater inlet pipeline, and by utilizing the circulation scheme of the extraction system and the solvent recovery system provided by the technical scheme of the invention, closing a valve from an outlet of a tower kettle of a water tower to a sewage treatment boundary area, and switching diluted phenol water at the outlet of the tower kettle of the water tower to an inlet of the extraction system;
step 2, increasing the dosage of alkali liquor of the deamination tower, improving the pH value of the wastewater, returning the wastewater with high pH value to a raw material wastewater inlet pipeline from an outlet of a deamination water cooler, and cleaning each device which cannot normally run due to oil contamination in a deacidification and deamination system; after the circular cleaning is finished, conveying the wastewater containing the oil stains to a gas-water separation device, and removing dust and oil again;
and 3, sending the de-ammonia water containing oil stains in the de-acidification and de-amination system to a gas water separation device, and restarting the device according to the technical scheme of the invention until the de-ammonia water index is qualified.
The improvement of the process of delivering washing water outside reduces the load of an extraction system and a solvent recovery system, and can improve the wastewater treatment capacity of the phenol ammonia recovery device by 20 percent; the consumption of the solvent and the steam of the washing water is reduced, the steam consumption of the technical scheme of the invention is reduced by 10 to 15 percent compared with that of the prior art, and the solvent consumption is reduced by 15 to 20 percent compared with that of the prior art; by improving the process flow of the gas phase extraction pipeline at the top of the water tower, the solvent in the solvent circulating tank is prevented from carrying water, the problem of over-temperature and over-pressure of the phenol tower is solved, and the solvent consumption is further reduced; the problem of low extraction efficiency is solved, the extraction dephenolization effect is improved, and the annual yield of the byproduct mixed phenol is increased by 2 percent. The pipeline for communicating the water tower outlet with the extraction system inlet is added, so that the process flow of each internal circulation is realized, and the solvent loss during starting and stopping is avoided. The cleaning pipeline of the deacidification and deamination system is added, the manual cleaning frequency is reduced, the service life of the equipment is prolonged, and the starting and stopping cost of the device is further reduced. The deamination tower kettle phenol water pump bypass pipeline is added, when the deamination tower is in normal process operation, the conveying mode of tower kettle phenol water is changed from centrifugal pump conveying to pressure conveying through equipment, the maintenance and overhaul cost of pump operation is reduced, and the power consumption can be saved by 264 ten thousand KWh per year.
The foregoing description is by way of example only and is not intended as limiting the embodiments of the present application. Obvious changes or modifications to the invention are intended to be covered by the appended claims.
Claims (5)
1. The utility model provides a phenol ammonia recovery unit ammonia recovery system which characterized in that: the device comprises a deacidification tower, a deamination tower, an extraction tower, a water tower and a phenol tower, wherein the outlet end of the deacidification tower is communicated with the inlet end of the deamination tower through a pipeline, the outlet end of the deamination tower is communicated with the inlet end of the extraction tower through a pipeline, a deamination water cooler, a static mixer and an oil-water separator are connected in series on the pipeline, the outlet end of the extraction tower is communicated with the inlet end of the water tower through a pipeline, and the outlet end of the water tower is communicated with a diluted phenol water-gas water separation pipeline and a diluted phenol water-biochemical treatment device through a pipeline; the outlet end of the oil-water separator is also communicated with the inlet end of the phenol tower through a pipeline, a No. 2 extract tank is connected in series on the pipeline, the upper end of the phenol tower is provided with a return pipeline, the return pipeline is provided with a solvent circulation tank, and the outlet end of the solvent circulation tank is communicated with the solvent inlet end of the extraction tower; an extraction opening of the extraction tower is communicated with a feed inlet of the No. 1 extract tank, and a discharge end of the No. 1 extract tank is communicated with a pipeline between the deamination water cooler and the static mixer; and the top of the water tower is provided with a condensation port which is communicated with an extract inlet of the condenser, and an extract outlet of the condenser is communicated with a feed inlet of the No. 1 extract tank.
2. The ammonia recovery system of the phenol ammonia recovery device according to claim 1, wherein: the washing water of the external feeding conversion device and the hypergravity dust removal device is changed from the diluted phenol water at the tower bottom of the water tower to the ammonia removal water at the tower bottom of the ammonia removal tower, namely two washing water pipelines which are respectively communicated with the external feeding conversion device and the hypergravity dust removal device are led out from a pipeline between the ammonia removal water cooler and the static mixer.
3. The ammonia recovery system of the phenol ammonia recovery device according to claim 1, wherein: when the diluted phenol water is not sent to the biochemical treatment device, the diluted phenol water in the tower kettle of the water tower is sent to the inlet of the extraction system changed from the gas water separation device, namely, the deammoniation water is led out from the pipeline between the deammoniation water cooler and the static mixer, and the wastewater returning pipeline is communicated with the inlet of the extraction system.
4. The ammonia recovery system of the phenol ammonia recovery device according to claim 1, wherein: the deamination water is added and returned to an incoming wastewater pipeline, namely the outlet end of the water tower is communicated with a pipeline from dilute phenol water to gas-water separation and a pipeline from dilute phenol water to a biochemical treatment device.
5. The ammonia recovery system of the phenol ammonia recovery device according to claim 1, wherein: the deamination tower kettle phenol water pump is connected in series on a pipeline between the extraction tower and the deamination water cooler, a deamination tower kettle phenol water pump bypass pipeline is added on the pipeline in front of the inlet of the deamination tower kettle phenol water pump, and the outlet of the deamination tower kettle phenol water pump bypass pipeline is communicated with the inlet end of the deamination water cooler so as to stop the deamination tower kettle pump during normal operation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN202223159695.7U CN218811220U (en) | 2022-11-29 | 2022-11-29 | Ammonia recovery system of phenol ammonia recovery device |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202223159695.7U CN218811220U (en) | 2022-11-29 | 2022-11-29 | Ammonia recovery system of phenol ammonia recovery device |
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| CN218811220U true CN218811220U (en) | 2023-04-07 |
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| CN202223159695.7U Active CN218811220U (en) | 2022-11-29 | 2022-11-29 | Ammonia recovery system of phenol ammonia recovery device |
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