CN218130926U - Urea production tail gas treatment system - Google Patents
Urea production tail gas treatment system Download PDFInfo
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- CN218130926U CN218130926U CN202222063123.2U CN202222063123U CN218130926U CN 218130926 U CN218130926 U CN 218130926U CN 202222063123 U CN202222063123 U CN 202222063123U CN 218130926 U CN218130926 U CN 218130926U
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Abstract
The utility model discloses a urea production tail gas treatment system, which comprises a hydrolysis water purification buffer tank, a pipeline pump, a hydrolysis water purification heat exchanger, a high-pressure absorption tower, a normal-pressure absorption tower, an emptying barrel and a dilute ammonia tank; the water outlet of the hydrolysis water purification buffer tank is communicated with the water inlet of the pipeline pump, the water outlet of the pipeline pump is communicated with the heat medium inlet of the hydrolysis water purification heat exchanger, and the heat medium outlet of the hydrolysis water purification heat exchanger is respectively communicated with the high-pressure absorption tower, the normal-pressure absorption tower and the absorption liquid inlet of the emptying barrel. Has the advantages that: the hydrolysis purified water with lower temperature is used as the ammonia absorption liquid, so that the ammonia absorption capacity is effectively improved, and the ammonia content in the discharged tail gas can be ensured to meet the environmental protection requirement; the hydrolyzed pure water obtained after the hydrolysis treatment of the urea production wastewater is used as the absorption liquid, so that the recycling of the production wastewater is realized, and the utilization rate of water resources is improved; the liquid ammonia obtained after the treatment of the dilute ammonia water collected in the dilute ammonia water tank can be used as a raw material for urea production, so that the raw material cost is saved.
Description
The technical field is as follows:
the utility model relates to a urea production tail gas treatment technical field especially relates to a urea production tail gas treatment system.
Background art:
urea, also known as carbamide, is one of the simplest organic compounds and is a chemical nitrogen fertilizer currently used in large quantities. The industrial synthesis of urea mainly uses ammonia and carbon dioxide under certain conditions, and in the process of producing urea, a high-pressure system, a low-pressure system, a hydrolysis system, an evaporation system, a matched dilute ammonia water tank, a urea liquid tank and the like in a urea production device all generate process tail gas. Because the process tail gas contains a certain amount of ammonia and can not be directly discharged, the ammonia in the process tail gas is absorbed and then discharged by mainly adopting a high-pressure absorption tower, a normal-pressure absorption tower and an emptying cylinder at present.
The top of the high-pressure absorption tower and the top of the emptying cylinder both adopt steam condensate generated in the urea production process as absorption liquid, and the absorption effect on ammonia is poor due to the higher temperature of the steam condensate; the weak aqua ammonia that the absorption liquid at ordinary pressure absorption tower top produced for high pressure absorption tower, it is limited to the absorptive capacity of ammonia, and self can volatilize partial ammonia yet, leads to the ammonia content too high in the tail gas that discharges in the urea production process from this, unsatisfied environmental protection requirement, has also caused the waste of raw materials ammonia, has increased the raw materials cost of urea.
The utility model has the following contents:
an object of the utility model is to provide a urea production tail gas treatment system.
The utility model discloses by following technical scheme implement: a urea production tail gas treatment system comprises a hydrolysis purified water buffer tank, a pipeline pump, a hydrolysis purified water heat exchanger, a high-pressure absorption tower, a normal-pressure absorption tower, an emptying cylinder and a dilute ammonia water tank;
the water outlet of the hydrolysis purified water buffer tank is communicated with the water inlet of the pipeline pump through a pipeline, the water outlet of the pipeline pump is communicated with the heat medium inlet of the hydrolysis purified water heat exchanger through a pipeline, the heat medium outlet of the hydrolysis purified water heat exchanger is divided into three paths, and the three paths are respectively communicated with the high-pressure absorption tower, the normal-pressure absorption tower and the absorption liquid inlet at the top of the emptying cylinder through pipelines;
a liquid outlet of the dilute ammonia water tank is communicated with an absorption liquid inlet in the middle of the high-pressure absorption tower through a pipeline, a dilute ammonia water outlet of the high-pressure absorption tower is communicated with an absorption liquid inlet in the middle of the normal-pressure absorption tower through a pipeline, and a dilute ammonia water outlet at the bottom of the normal-pressure absorption tower is communicated with a liquid inlet of the dilute ammonia water tank through a pipeline; the dilute ammonia water outlet of the emptying cylinder is communicated with the liquid inlet of the dilute ammonia water tank through a pipeline;
a tail gas outlet of a high-pressure system in the urea production device is communicated with a gas inlet at the bottom of the high-pressure absorption tower through a pipeline, and tail gas outlets of a low-pressure system, a hydrolysis system and an evaporation system in the urea production device are communicated with a gas inlet at the bottom of the normal-pressure absorption tower through pipelines; and tail gas outlets of a urea liquid tank and a dilute ammonia liquid tank in the urea production device are communicated with a gas inlet at the bottom of the emptying cylinder through pipelines.
Preferably, the system also comprises a dilute ammonia water heat exchanger and a dilute ammonia water pump; the dilute ammonia water outlet of the normal pressure absorption tower is communicated with the inlet of the dilute ammonia water pump through a pipeline, the outlet of the dilute ammonia water pump is communicated with the heat medium inlet of the dilute ammonia water heat exchanger through a pipeline, and the heat medium outlet of the dilute ammonia water heat exchanger is communicated with the circulating absorption liquid inlet at the middle part of the normal pressure absorption tower through a pipeline.
The utility model has the advantages that: 1. the hydrolysis purified water with lower temperature is used as the ammonia absorption liquid, so that the ammonia absorption amount is effectively improved, and the ammonia content in the discharged tail gas can be ensured to meet the environmental protection requirement; 2. compared with steam condensate, the initial temperature of the hydrolyzed purified water is lower, so that the consumption of circulating water for the temperature reduction treatment of the absorption liquid is reduced; 3. the hydrolyzed pure water obtained after the hydrolysis treatment of the urea production wastewater is used as the absorption liquid, so that the recycling of the production wastewater is realized, and the utilization rate of water resources is improved; 4. the liquid ammonia obtained after the treatment of the dilute ammonia water collected in the dilute ammonia water tank can be used as a raw material for urea production, so that the raw material cost is saved.
Description of the drawings:
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 description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
FIG. 1 is a schematic diagram showing the system connection in example 1;
in the figure: 1. hydrolysis water purification buffer tank, 2, pipeline pump, 3, hydrolysis water purification heat exchanger, 4, high-pressure absorption tower, 5, normal pressure absorption tower, 6, dilute ammonia water heat exchanger, 7, dilute ammonia water pump, 8, blow-down cylinder, 9, dilute ammonia water tank, 10, high-pressure system, 11, low-pressure system, 12, hydrolysis system, 13, evaporation system, 14, urea liquid tank.
The specific implementation mode is as follows:
the technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
Example 1:
as shown in fig. 1, a system for treating tail gas from urea production comprises a hydrolysis purified water buffer tank 1, a pipeline pump 2, a hydrolysis purified water heat exchanger 3, a high-pressure absorption tower 4, a normal pressure absorption tower 5, a dilute ammonia water heat exchanger 6, a dilute ammonia water pump 7, an emptying cylinder 8 and a dilute ammonia water tank 9;
the water outlet of the hydrolysis water purification buffer tank 1 is communicated with the water inlet of the pipeline pump 2 through a pipeline, the water outlet of the pipeline pump 2 is communicated with the heat medium inlet of the hydrolysis water purification heat exchanger 3 through a pipeline, the heat medium outlet of the hydrolysis water purification heat exchanger 3 is divided into three paths, and the three paths are respectively communicated with the high-pressure absorption tower 4, the normal-pressure absorption tower 5 and the absorption liquid inlet at the top of the emptying cylinder 8 through pipelines;
the dilute ammonia water outlet of the high-pressure absorption tower 4 is communicated with the absorption liquid inlet in the middle of the normal-pressure absorption tower 5, the dilute ammonia water outlet at the bottom of the normal-pressure absorption tower 5 is divided into two paths which are respectively communicated with the liquid inlet of the dilute ammonia water tank 9 and the inlet of the dilute ammonia water pump 7 through pipelines, the outlet of the dilute ammonia water pump 7 is communicated with the heat medium inlet of the dilute ammonia water heat exchanger 6 through pipelines, and the heat medium outlet of the dilute ammonia water heat exchanger 6 is communicated with the circulating absorption liquid inlet in the middle of the normal-pressure absorption tower 5. The dilute ammonia water outlet of the emptying cylinder 8 is communicated with the liquid inlet of the dilute ammonia water tank 9; the liquid outlet of the dilute ammonia water tank 9 is communicated with the absorption liquid inlet at the middle part of the high-pressure absorption tower 4.
A tail gas outlet of a high-pressure system 10 in the urea production device is communicated with a gas inlet at the bottom of the high-pressure absorption tower 4 through a pipeline, and tail gas outlets of a low-pressure system 11, a hydrolysis system 12 and an evaporation system 13 in the urea production device are communicated with a gas inlet at the bottom of the normal-pressure absorption tower 5 through pipelines; the tail gas outlets of the urea liquid tank 14 and the dilute ammonia liquid tank 9 in the urea production device are communicated with the gas inlet at the bottom of the emptying cylinder 8 through pipelines.
The working description is as follows:
after being hydrolyzed by a hydrolysis device, the wastewater generated in the urea production process obtains hydrolyzed purified water with the temperature of 50 ℃ and the pressure of 0.5MPa, the hydrolyzed purified water is temporarily stored in a hydrolyzed purified water buffer tank 1, is pressurized to 1.3MPa by a pipeline pump 2, enters a hydrolyzed purified water cooler and is cooled to 30 ℃, and is used as absorption liquid which is respectively conveyed to a high-pressure absorption tower 4, a normal-pressure absorption tower 5 and an emptying cylinder 8 through pipelines.
The process tail gas generated by a high-pressure system 10 in a urea production device is connected to the bottom of a high-pressure absorption tower 4, dilute ammonia water from a dilute ammonia water tank 9 is used as absorption liquid to carry out primary ammonia absorption on the process tail gas generated by the high-pressure system 10 in the lower half section of the high-pressure absorption tower 4, unabsorbed process tail gas enters the upper half section of the high-pressure absorption tower 4, hydrolysis purified water is used as absorption liquid to further absorb ammonia, the rest unabsorbed process tail gas is discharged from a gas outlet at the top of the high-pressure absorption tower 4, the absorption liquid in the upper half section and the absorption liquid in the lower half section of the high-pressure absorption tower 4 are discharged from a dilute ammonia water outlet at the bottom of the high-pressure absorption tower 4 and are sent to an atmospheric absorption tower 5 to be used as absorption liquid in the lower half section of the atmospheric absorption tower 5, the ammonia in the process tail gas from a low-pressure system 11, a hydrolysis system 12 and an evaporation system 13 in the urea production device is absorbed for the first time, the unabsorbed process tail gas enters the upper half section of an atmospheric absorption tower 5, the ammonia in the process tail gas is absorbed for the second time by hydrolysis purified water, the rest process tail gas is discharged from a gas outlet at the top of the atmospheric absorption tower 5, absorption liquid absorbing the ammonia is gathered at the bottom of the atmospheric absorption tower 5, one part of the absorption liquid is discharged into a dilute ammonia water tank 9, and the other part of the absorption liquid is cooled by a heat exchanger as circulating absorption liquid and then enters the lower half section of the atmospheric absorption tower 5 again as absorption liquid, so that the absorption liquid is fully utilized; the process tail gas from the dilute ammonia water tank 9 and the urea liquid tank 14 is connected to the bottom of the emptying cylinder 8, the hydrolyzed purified water is used as absorption liquid to absorb ammonia in the dilute ammonia water tank, the absorption liquid which absorbs the ammonia is discharged to the dilute ammonia water tank 9 from a dilute ammonia water outlet at the bottom of the emptying cylinder 8, and the residual tail gas is discharged from the top of the emptying cylinder 8. The liquid ammonia obtained by condensing the ammonia gas obtained by treating the dilute ammonia water collected in the dilute ammonia water tank 9 by an analytic hydrolysis system can be used as a raw material for urea production.
The embodiment is utilized to treat the tail gas in the urea production, the ammonia content of the tail gas discharged by the high-pressure absorption tower 4 is reduced to 1% from 7.24%, the ammonia content of the tail gas discharged by the normal-pressure absorption tower 5 is reduced to 0.13% from 0.3%, and the ammonia content of the tail gas discharged by the emptying cylinder 8 is reduced to 1.04% from 2.28%, so that the recovery rate of ammonia is improved and the production cost of urea is saved while the environmental protection requirement is met.
The above description is only a preferred embodiment of the present invention, and should not be taken as limiting the invention, and any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (2)
1. A urea production tail gas treatment system is characterized by comprising a hydrolysis purified water buffer tank, a pipeline pump, a hydrolysis purified water heat exchanger, a high-pressure absorption tower, a normal-pressure absorption tower, an emptying cylinder and a dilute ammonia water tank;
the water outlet of the hydrolysis water purification buffer tank is communicated with the water inlet of the pipeline pump through a pipeline, the water outlet of the pipeline pump is communicated with the heat medium inlet of the hydrolysis water purification heat exchanger through a pipeline, and the heat medium outlet of the hydrolysis water purification heat exchanger is divided into three paths and is respectively communicated with the high-pressure absorption tower, the normal-pressure absorption tower and the absorption liquid inlet at the top of the emptying cylinder through pipelines;
the dilute ammonia water outlet of the high-pressure absorption tower is communicated with the absorption liquid inlet in the middle of the normal-pressure absorption tower through a pipeline, and the dilute ammonia water outlet at the bottom of the normal-pressure absorption tower is communicated with the liquid inlet of the dilute ammonia water tank through a pipeline; a dilute ammonia water outlet of the emptying cylinder is communicated with a liquid inlet of the dilute ammonia water tank through a pipeline; the liquid outlet of the dilute ammonia water tank is communicated with the absorption liquid inlet in the middle of the high-pressure absorption tower through a pipeline;
a tail gas outlet of a high-pressure system in the urea production device is communicated with a gas inlet at the bottom of the high-pressure absorption tower through a pipeline, and tail gas outlets of a low-pressure system, a hydrolysis system and an evaporation system in the urea production device are communicated with a gas inlet at the bottom of the normal-pressure absorption tower through pipelines; the tail gas outlets of a urea liquid tank and a dilute ammonia water tank in the urea production device are communicated with the gas inlet at the bottom of the emptying cylinder through pipelines.
2. The urea production tail gas treatment system of claim 1, further comprising a dilute ammonia water heat exchanger and a dilute ammonia water pump; the dilute ammonia water outlet of the normal pressure absorption tower is communicated with the inlet of the dilute ammonia water pump through a pipeline, the outlet of the dilute ammonia water pump is communicated with the heat medium inlet of the dilute ammonia water heat exchanger through a pipeline, and the heat medium outlet of the dilute ammonia water heat exchanger is communicated with the circulating absorption liquid inlet in the middle of the normal pressure absorption tower through a pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222063123.2U CN218130926U (en) | 2022-08-05 | 2022-08-05 | Urea production tail gas treatment system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222063123.2U CN218130926U (en) | 2022-08-05 | 2022-08-05 | Urea production tail gas treatment system |
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| CN218130926U true CN218130926U (en) | 2022-12-27 |
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| CN202222063123.2U Active CN218130926U (en) | 2022-08-05 | 2022-08-05 | Urea production tail gas treatment system |
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- 2022-08-05 CN CN202222063123.2U patent/CN218130926U/en active Active
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