CN216737642U - High-efficiency energy-saving ammonia distillation system - Google Patents
High-efficiency energy-saving ammonia distillation system Download PDFInfo
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- CN216737642U CN216737642U CN202123315543.7U CN202123315543U CN216737642U CN 216737642 U CN216737642 U CN 216737642U CN 202123315543 U CN202123315543 U CN 202123315543U CN 216737642 U CN216737642 U CN 216737642U
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Abstract
The utility model relates to the technical field of coking residual ammonia water treatment equipment, in particular to an efficient energy-saving ammonia distillation system. The deamination tower section and the deacidification gas tower section are in a tower shape, one path of the bottom of the deamination tower section is connected with the bottom of the acid mist removing tower, and the other path of the bottom of the deamination tower section is connected with the ammonia water heat exchanger; the residual ammonia water pipeline is connected with an ammonia water heat exchanger, and the ammonia water heat exchanger is connected with the deacidification gas tower section; the bottom of the acid gas removal tower section is connected with a pipeline mixer, and the pipeline mixer is connected with the top of the ammonia removal tower section; the top of the deamination tower section is connected with the bottom of an ammonia absorption tower, the bottom of the ammonia absorption tower is connected with an ammonium sulfate process, and the top of the ammonia absorption tower is connected with the bottom of an acid mist removal tower; the ammonia water heat exchanger is connected with the waste water cooler; one path of the acid mist removing tower is connected with the acid gas removing tower section, and the other path of the acid mist removing tower is connected with the deamination tower section; the deacidification gas tower section is connected with a gas pipeline before desulfurization or an ammonium sulfate saturator pipeline in an ammonium sulfate process. The utility model efficiently utilizes ammonia resources, greatly reduces energy consumption and greatly reduces equipment investment.
Description
Technical Field
The utility model relates to the technical field of coking residual ammonia water treatment equipment, in particular to an efficient energy-saving ammonia distillation system.
Background
The coking residual ammonia water has complex components, wherein the impurity ammonia exists in three forms: free NH3Volatile ammonium salts and fixed ammonium salts. The volatile ammonium salt is mainly ammonium carbonate, ammonium sulfide, ammonium cyanide and the like, and is easily decomposed into gases such as ammonia, hydrogen sulfide, carbon dioxide, hydrogen cyanide and the like by heating, but the fixed ammonium salt can be decomposed by adding alkali.
At present, the residual ammonia water in coking is mostly deaminated by a steam stripping method, and the evaporated ammonia gas is sent to a gas pipeline or a saturator before a desulfurization unit, or is made into concentrated ammonia water for sale and the like. The steam stripping deamination process is mature and widely applied, but the method has high steam consumption (170 kg-200 kg steam/ton residual ammonia water), so how to improve the utilization rate of the steam ammonia energy and reduce the energy unit consumption becomes a problem which is generally concerned by people.
CN 202808402U discloses a residual ammonia water heat pump distillation system, in order to reduce the energy consumption of the stripping deamination, a second type absorption heat pump is adopted to recover the latent heat of ammonia steam at the top of an ammonia still for heating waste water at the bottom of a tower, thereby providing a part of heat source and saving the energy consumption of ammonia still. However, by adopting the heat pump ammonia distillation process, the heat pump can only recover 43-49% of latent heat of the ammonia steam at the tower top, and the heat brought by the ammonia steam at the tower top accounts for about 70% of the heat source at the tower bottom, so that the second absorption heat pump ammonia distillation process only saves about 30% of steam consumption compared with the traditional ammonia distillation process. And the second type of heat pump ammonia distillation process still needs to consume the circulating water quantity which is approximately equal to that of the traditional ammonia distillation process, and does not have the function of water conservation.
CN 102674489B discloses a method for treating high-concentration ammonia-containing wastewater based on steam compression, and CN103964528B discloses a method for heat pump rectification stripping deamination, wherein ammonia steam at the top of a deamination tower is pressurized and heated by a compressor and then exchanges heat with wastewater at the bottom of a reboiler at the bottom of the tower kettle, so that a part of energy is provided for the deamination process, and the energy consumption is saved. However, the steam consumption of the deamination method is still about 95 kg/ton of ammonia-containing wastewater, and the steam consumption is still relatively high. And the ammonia-containing steam is corrosive, and has higher requirements on the materials of the compressor and the reboiler. If the treated wastewater also contains acidic components such as hydrogen sulfide, the requirements on equipment materials are more severe.
CN 102190341B discloses a heat pump flash evaporation stripping deamination method, which is characterized in that ammonia gas at the top of a deamination tower is compressed by a compressor, then the ammonia is absorbed and removed, and then the ammonia enters the deamination tower, so that most of steam energy is saved. However, the process route of the method of the utility model is complex, the operation difficulty is high, and the process is only suitable for the working condition that only ammonia is contained in the wastewater, and the applicability to the wastewater treatment containing acidic components is poor.
SUMMERY OF THE UTILITY MODEL
In order to overcome the defects of the prior art, the utility model provides an efficient energy-saving ammonia distillation system, which efficiently utilizes ammonia resources, greatly reduces energy consumption and greatly reduces equipment investment.
In order to achieve the purpose, the utility model adopts the following technical scheme:
an efficient energy-saving ammonia distillation system comprises a deamination tower section, a deacidification gas tower section, a waste water pump, a circulating washing pump, a vacuum pump, an ammonia absorption tower, an ammonia water heat exchanger, a waste water cooler, an ammonium sulfate mother liquid pump and a pipeline mixer.
The deamination tower section and the deacidification tower section are in a tower shape, the deacidification tower section is arranged above the deamination tower section, and the deamination tower section is arranged below the deacidification tower section.
The bottom of the deamination tower section is connected with an inlet pipeline of a wastewater pump; the outlet end pipeline of the waste water pump is divided into two paths, one path is connected with the bottom pipeline of the acid mist removing tower, and the other path is connected with the ammonia water heat exchanger pipeline.
The residual ammonia water pipeline is connected with an ammonia water inlet pipeline of the ammonia water heat exchanger; and an ammonia water outlet of the ammonia water heat exchanger is connected with a pipeline at the top of the deacidification gas tower section.
The bottom of the deacidification gas tower section is connected with a pipeline of a pipeline mixer; the pipeline mixer is connected with a pipeline at the top of the deamination tower section.
The top of the deamination tower section is connected with a pipeline at the bottom of the ammonia absorption tower; the bottom of the ammonia absorption tower is connected with a pump pipeline of ammonium sulfate mother liquor; an outlet of the ammonium sulfate mother liquor pump is connected with an ammonium sulfate process pipeline; the top of the ammonia absorption tower is connected with the bottom pipeline of the acid mist removing tower.
The top of the acid mist removing tower is connected with an inlet pipeline of the vacuum pump; the bottom of the acid mist removing tower is connected with an inlet pipeline of a circulating washing pump; the outlet of the circulating washing pump is connected with a pipeline at the top of the acid mist removing tower; the outlet pipeline of the circulating washing pump is provided with a small-flow liquid discharge pipeline which is connected with the top pipeline of the deamination tower section; the waste water outlet of the ammonia water heat exchanger is connected with a waste water inlet pipeline of the waste water cooler; the waste water outlet of the waste water cooler is connected with a phenol-cyanogen waste water treatment device pipeline.
The pipeline at the outlet end of the vacuum pump is divided into two paths, one path is connected with the pipeline at the bottom of the deacidification tower section, and the other path is connected with the pipeline at the bottom of the deamination tower section.
The outlet at the top of the deacidification gas tower section is connected with a gas pipeline before desulfurization or an ammonium sulfate saturator pipeline in an ammonium sulfate procedure.
Compared with the prior art, the utility model has the beneficial effects that:
1. in the aspect of energy consumption, the system is adopted to treat the residual ammonia water, the ammonia resource can be efficiently utilized, the steam consumption is saved, the circulating water consumption is low, the power consumption is low, and the overall operation cost is greatly reduced.
2. In the aspect of equipment investment, the requirement on the material of the vacuum pump is reduced, the equipment investment is reduced, and meanwhile, the reliable guarantee is provided for the continuous and stable operation of the equipment; and the top part of the tower such as an ammonia dephlegmator and the like is not required to be cooled and refluxed, and equipment such as a reboiler and the like is not required, so that the equipment investment is reduced, and the process flow is simplified.
3. In the aspect of ammonia resource utilization, 95 percent of ammonia in the residual ammonia water is converted into ammonium sulfate products, and the product benefits are increased.
Drawings
FIG. 1 is a schematic diagram of the structure and process of the present invention.
In the figure: 1-deammoniation tower section 2-deacidification gas tower section 3-circulating washing pump 4-vacuum pump 5-ammonia absorption tower 6-acid mist removing tower 7-waste water pump 8-ammonia water heat exchanger 9-waste water cooler 10-thiamine mother liquor pump 11-pipeline mixer
Detailed Description
The following further describes embodiments of the present invention with reference to the accompanying drawings:
as shown in fig. 1, an efficient energy-saving ammonia distillation system comprises a deamination tower section 1, a deacidification gas tower section 2, an acid mist removing tower 6, a waste water pump 7, a circulating washing pump 3, a vacuum pump 4, an ammonia absorption tower 5, an ammonia water heat exchanger 8, a waste water cooler 9, an ammonium sulfate mother liquor pump 10 and a pipeline mixer 11.
The deamination tower section 1 and the deacidification gas tower section 2 are in a tower shape, the deacidification gas tower section 2 is arranged above, and the deamination tower section 1 is arranged below.
The bottom of the deamination tower section 1 is connected with an inlet pipeline of a waste water pump 7; the pipeline at the outlet end of the waste water pump 7 is divided into two paths, one path is connected with the pipeline at the bottom of the acid mist removing tower 6, and the other path is connected with the pipeline of the ammonia water heat exchanger 8.
The residual ammonia water pipeline is connected with an ammonia water inlet pipeline of an ammonia water heat exchanger 8; an ammonia water outlet of the ammonia water heat exchanger 8 is connected with a pipeline at the top of the deacidification gas tower section 2.
The bottom of the deacidification gas tower section 2 is connected with a pipeline mixer 11 through a pipeline; the pipeline mixer 11 is connected with the pipeline at the top of the deamination tower section 1.
The top of the deamination tower section 1 is connected with a pipeline at the bottom of an ammonia absorption tower 5; the bottom of the ammonia absorption tower 5 is connected with a pipeline of an ammonium sulfate mother liquor pump 10; an outlet of the ammonium sulfate mother liquor pump 10 is connected with an ammonium sulfate process pipeline; the top of the ammonia absorption tower 5 is connected with a pipeline at the bottom of an acid mist removing tower 6.
The top of the acid mist removing tower 6 is connected with an inlet pipeline of the vacuum pump 4; the bottom of the acid mist removing tower 6 is connected with an inlet pipeline of the circulating washing pump 3; the outlet of the circulating washing pump 3 is connected with a pipeline at the top of the acid mist removing tower 6; the outlet pipeline of the circulating washing pump 3 is provided with a small-flow liquid discharge pipeline which is connected with the pipeline at the top of the deamination tower section 1; a waste water outlet of the ammonia water heat exchanger 8 is connected with a waste water inlet pipeline of a waste water cooler 9; the waste water outlet of the waste water cooler 9 is connected with a phenol-cyanogen waste water treatment device through a pipeline.
The pipeline at the outlet end of the vacuum pump 4 is divided into two paths, one path is connected with the pipeline at the bottom of the deacidification tower section 2, and the other path is connected with the pipeline at the bottom of the deamination tower section 1.
The outlet at the top of the deacidification gas tower section 2 is connected with a gas pipeline before desulfurization or an ammonium sulfate saturator pipeline in an ammonium sulfate procedure.
In the aspect of energy consumption, the method for treating the residual ammonia water can efficiently utilize ammonia resources, save steam consumption, and greatly reduce the total operation cost, and the circulating water consumption is low and the power consumption is low. In the aspect of equipment investment, the utility model reduces the requirements on the material of the vacuum pump, reduces the equipment investment and simultaneously provides reliable guarantee for the continuous and stable operation of the equipment; and the top part of the tower such as an ammonia dephlegmator and the like is not required to be cooled and refluxed, and equipment such as a reboiler and the like is not required, so that the equipment investment is reduced, and the process flow is simplified. In the aspect of ammonia resource utilization, 95 percent of ammonia in the residual ammonia water is converted into an ammonium sulfate product, so that the product income is increased.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and equivalent alternatives or modifications according to the technical solution of the present invention and the inventive concept thereof should be covered by the scope of the present invention.
Claims (5)
1. The utility model provides an energy-efficient type ammonia distillation system which characterized in that: comprises a deamination tower section, a deacidification gas tower section, an ammonia absorption tower, an ammonia water heat exchanger, a waste water cooler and a pipeline mixer;
the deamination tower section and the deacidification gas tower section are in a tower shape, the deacidification gas tower section is arranged above, and the deamination tower section is arranged below;
one path of the bottom of the deamination tower section is connected with a pipeline at the bottom of the acid mist removing tower, and the other path of the bottom of the deamination tower section is connected with a pipeline of an ammonia water heat exchanger;
the residual ammonia water pipeline is connected with an ammonia water inlet pipeline of an ammonia water heat exchanger, and an ammonia water outlet of the ammonia water heat exchanger is connected with a pipeline at the top of the deacidification gas tower section;
the bottom of the acid gas removal tower section is connected with a pipeline of a pipeline mixer, and the pipeline mixer is connected with a pipeline at the top of the deamination tower section;
the top of the deamination tower section is connected with a pipeline at the bottom of an ammonia absorption tower, the bottom of the ammonia absorption tower is connected with a pipeline at the ammonium sulfate process, and the top of the ammonia absorption tower is connected with a pipeline at the bottom of an acid mist removal tower;
the bottom of the acid mist removing tower is connected with a pipeline at the top of the acid mist removing tower; the waste water outlet of the ammonia water heat exchanger is connected with a waste water inlet pipeline of a waste water cooler, and the waste water outlet of the waste water cooler is connected with a phenol-cyanogen waste water treatment device pipeline;
one path of the top of the acid mist removing tower is connected with a pipeline at the bottom of the acid removing gas tower section, and the other path of the top of the acid mist removing tower is connected with a pipeline at the bottom of the deamination tower section;
the outlet at the top of the deacidification gas tower section is connected with a gas pipeline before desulfurization or an ammonium sulfate saturator pipeline in an ammonium sulfate procedure.
2. The energy-efficient ammonia distillation system of claim 1, wherein: the bottom of the deamination tower section is connected with an inlet pipeline of the wastewater pump; the outlet end pipeline of the waste water pump is divided into two paths, one path is connected with the bottom pipeline of the acid mist removing tower, and the other path is connected with the ammonia water heat exchanger pipeline.
3. The energy-efficient ammonia distillation system of claim 1, wherein: the bottom of the ammonia absorption tower is connected with an ammonium sulfate mother liquor pump pipeline; the outlet of the ammonium sulfate mother liquor pump is connected with an ammonium sulfate process pipeline.
4. The energy-efficient ammonia distillation system of claim 1, wherein: the top of the acid mist removing tower is connected with an inlet pipeline of the vacuum pump; the pipeline at the outlet end of the vacuum pump is divided into two paths, one path is connected with the pipeline at the bottom of the deacidification tower section, and the other path is connected with the pipeline at the bottom of the deamination tower section.
5. The energy-efficient ammonia distillation system of claim 1, wherein: the bottom of the acid mist removing tower is connected with an inlet pipeline of the circulating washing pump; the outlet of the circulating washing pump is connected with a pipeline at the top of the acid mist removing tower; and the outlet pipeline of the circulating washing pump is provided with a liquid discharge pipeline connected with the top pipeline of the deamination tower section.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202123315543.7U CN216737642U (en) | 2021-12-27 | 2021-12-27 | High-efficiency energy-saving ammonia distillation system |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202123315543.7U CN216737642U (en) | 2021-12-27 | 2021-12-27 | High-efficiency energy-saving ammonia distillation system |
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| CN216737642U true CN216737642U (en) | 2022-06-14 |
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| CN202123315543.7U Active CN216737642U (en) | 2021-12-27 | 2021-12-27 | High-efficiency energy-saving ammonia distillation system |
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2021
- 2021-12-27 CN CN202123315543.7U patent/CN216737642U/en active Active
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