CN209771782U - Pressurization deacidification ammonia distillation system - Google Patents
Pressurization deacidification ammonia distillation system Download PDFInfo
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- CN209771782U CN209771782U CN201920189242.8U CN201920189242U CN209771782U CN 209771782 U CN209771782 U CN 209771782U CN 201920189242 U CN201920189242 U CN 201920189242U CN 209771782 U CN209771782 U CN 209771782U
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Abstract
the utility model relates to a pressurized deacidification ammonia distillation system, wherein a deacidification tower is provided with an acid gas outlet, a mixed liquid inlet, a barren liquor side draw outlet, an ammonia distillation gas inlet and an ammonia water discharge port; the mixed liquid inlet is connected with the residual ammonia water pipeline and the rich liquid pipeline of the desulfurizing tower through a heat exchanger; the heat exchanger is connected with a lean solution side draw outlet; the ammonia still is provided with an ammonia still gas outlet, an ammonia water inlet, a reflux liquid inlet, an alkali liquor inlet, a steam inlet and an ammonia still wastewater outlet; an ammonia water outlet of the deacidification tower is connected with an ammonia water inlet of an ammonia still; an ammonia evaporation gas outlet of the ammonia evaporation tower is respectively connected with an ammonia evaporation gas inlet of the deacidification tower and an inlet of the condenser, a condensate outlet of the condenser is connected with a reflux liquid inlet of the ammonia evaporation tower, and an ammonia evaporation wastewater outlet of the ammonia evaporation tower is respectively connected with an ammonia evaporation wastewater conveying pipeline and a stripping water conveying pipeline. The utility model discloses a change rich solution desorption pressure, when the recovery of ammonia product is accomplished in the substep desorption, improve the barren solution quality, increase desulfurization effect.
Description
Technical Field
the utility model relates to a coke oven gas purifies technical field, especially relates to a pressurization deacidification ammonia distillation system.
background
The ammonia-water desulphurization process is a common process for removing hydrogen sulfide in raw gas. The process takes ammonia in the coal gas as an alkali source, takes an ammonia-containing water solution as a washing medium, and adopts an ammonia-sulfur combined washing (absorption) process to remove hydrogen sulfide in the coal gas. The method is characterized in that a washing device and a deacidification ammonia distilling device form an absorption and desorption process main body, and the ammonia and hydrogen sulfide washing and stripping desorption devices are tightly combined together. In the absorption unit, the deacidification ammonia still returns the deacidification lean solution with high ammonia content and the stripping water to absorb ammonia and hydrogen sulfide in the raw gas, so that rich solution containing ammonia and hydrogen sulfide is formed, and the purpose of removing hydrogen sulfide in the raw gas is achieved. In the desorption unit, the deacidified barren solution and stripped water (part of ammonia distillation wastewater) obtained by desorbing the rich solution by the deacidification and ammonia distillation device are sent back to the washing device for recycling.
Compared with other desulfurization processes, the ammonia desulfurization process only uses water as a washing medium and ammonia in the coal gas as an alkali source, does not generate desulfurization waste liquid, and has the advantages of short total coal gas purification process and low investment. However, in the prior art, a desorption unit (deacidification and ammonia distillation) desorbs ammonia gas and hydrogen sulfide together, and the desorbed gas is decomposed by ammonia and then subjected to sulfur recovery. In this process, ammonia, which can be a final chemical product, is directly decomposed as an impurity and is not effectively recovered.
The deacidification ammonia distillation process matched with the ammonia water method for desulfurization at present is difficult to independently control the desorption amount of hydrogen sulfide and ammonia because hydrogen sulfide and ammonia used in desulfurization rich solution are desorbed together. When the stripping load at the bottom of the deacidification ammonia still is increased, the escape amount of ammonia in the barren solution is increased, so that the barren solution contains insufficient ammonia, and the requirement of desulfurization is difficult to meet when the barren solution returns to the desulfurization tower. If the stripping load at the bottom of the deacidification ammonia still is reduced, the hydrogen sulfide can not be effectively extracted from the rich liquid, the hydrogen sulfide is insufficient to be extracted from the top of the tower, meanwhile, the lean liquid contains more hydrogen sulfide, and the desulfurization requirement in the desulfurization tower is difficult to meet.
SUMMERY OF THE UTILITY MODEL
The utility model provides a pressurization deacidification ammonia distillation system through changing rich solution desorption pressure, when the recovery of ammonia product is accomplished in the substep desorption, improves the barren solution quality, increases desulfurization effect.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
A pressurized deacidification ammonia distillation system comprises a deacidification tower, an ammonia distillation tower, a heat exchanger, a condenser and a pump; the top of the deacidification tower is provided with an acid gas outlet, the upper part of the deacidification tower is provided with a mixed liquid inlet, the middle part of the deacidification tower is provided with a lean liquid side draw outlet, the lower part of the deacidification tower is provided with an ammonia evaporation gas inlet, and the bottom of the deacidification tower is provided with an ammonia water outlet; the mixed liquid inlet is connected with a first heat exchange medium outlet of the heat exchanger, and a first heat exchange medium inlet of the heat exchanger is respectively connected with the residual ammonia water pipeline and the desulfurizing tower rich liquid pipeline; a second heat exchange medium inlet of the heat exchanger is connected with a lean solution side draw-out outlet, and a second heat exchange medium outlet is connected with a lean solution output pipeline; the top of the ammonia still is provided with an ammonia still gas outlet, the upper part is provided with an ammonia water inlet and a reflux liquid inlet, the middle part is provided with an alkali liquor inlet, the lower part is provided with a steam inlet, and the bottom is provided with an ammonia still wastewater outlet; an ammonia water outlet of the deacidification tower is connected with an ammonia water inlet of the ammonia still through a pump; an ammonia evaporation gas outlet of the ammonia evaporation tower is respectively connected with an ammonia evaporation gas inlet of the deacidification tower and an inlet of a condenser, a condensate outlet of the condenser is connected with a reflux liquid inlet of the ammonia evaporation tower, and a gas phase outlet of the condenser is connected with an ammonia gas conveying pipeline; an ammonia distillation wastewater outlet of the ammonia distillation tower is respectively connected with an ammonia distillation wastewater conveying pipeline and a stripping water conveying pipeline.
and a plurality of layers of fillers or trays are arranged in the deacidification tower between the mixed liquid inlet and the lean liquid side draw outlet, and a plurality of layers of fillers or trays are arranged in the deacidification tower between the lean liquid side draw outlet and the ammonia distillation gas inlet.
Compared with the prior art, the beneficial effects of the utility model are that:
1) the ammonia product is effectively recovered and the economic benefit is improved by changing the desorption pressure of the rich solution and desorbing step by step;
2) Improve the quality of the desulfurization barren solution and strengthen the desulfurization effect.
Drawings
fig. 1 is a schematic structural diagram of the pressurized deacidification ammonia distillation system of the present invention.
in the figure: 1. the system comprises a deacidification tower 11, an acid gas outlet 12, a mixed solution inlet 13, a barren liquor side draw-out port 14, an ammonia distillation gas inlet 15, an ammonia water discharge port 2, an ammonia distillation tower 21, an ammonia distillation gas outlet 22, an ammonia water inlet 23, a reflux liquid inlet 24, an alkali liquor inlet 25, a steam inlet 26, an ammonia distillation wastewater outlet 3, a pump 4, a condenser 5 and a heat exchanger
Detailed Description
the following description of the embodiments of the present invention will be made with reference to the accompanying drawings:
As shown in fig. 1, the system for deacidifying and distilling ammonia under pressure of the present invention comprises a deacidification tower 1, an ammonia distillation tower 2, a heat exchanger 5, a condenser 4 and a pump 3; the top of the deacidification tower 1 is provided with an acid gas outlet 11, the upper part is provided with a mixed liquid inlet 12, the middle part is provided with a lean liquid side draw outlet 13, the lower part is provided with an ammonia evaporation gas inlet 14, and the bottom is provided with an ammonia water outlet 15; the mixed liquid inlet 12 is connected with a first heat exchange medium outlet of the heat exchanger 5, and a first heat exchange medium inlet of the heat exchanger 5 is respectively connected with the residual ammonia water pipeline and the desulfurizing tower rich liquid pipeline; a second heat exchange medium inlet of the heat exchanger 5 is connected with a lean solution lateral line extraction outlet 13, and a second heat exchange medium outlet is connected with a lean solution output pipeline; the top of the ammonia still 2 is provided with an ammonia still gas outlet 21, the upper part is provided with an ammonia water inlet 22 and a reflux liquid inlet 23, the middle part is provided with an alkali liquor inlet 24, the lower part is provided with a steam inlet 25, and the bottom is provided with an ammonia still wastewater outlet 26; an ammonia water outlet 15 of the deacidification tower 1 is connected with an ammonia water inlet 22 of the ammonia still 2 through a pump 3; an ammonia evaporation gas outlet 21 of the ammonia evaporation tower 2 is respectively connected with an ammonia evaporation gas inlet 14 of the deacidification tower 1 and an inlet of a condenser 4, a condensate outlet of the condenser 4 is connected with a reflux inlet 23 of the ammonia evaporation tower 2, and a gas phase outlet of the condenser 4 is connected with an ammonia gas conveying pipeline; an ammonia distillation wastewater outlet 26 of the ammonia distillation tower 2 is respectively connected with an ammonia distillation wastewater conveying pipeline and a stripping water conveying pipeline.
And a plurality of layers of fillers or trays are arranged in the deacidification tower 1 between the mixed liquid inlet 12 and the lean liquid side draw outlet 13, and a plurality of layers of fillers or trays are arranged in the deacidification tower 1 between the lean liquid side draw outlet 13 and the ammonia distillation gas inlet 14.
The technical process of the pressurized deacidification ammonia distillation system is as follows:
1) Mixing the rich solution from the desulfurizing tower with the residual ammonia water, exchanging heat with the barren solution of the deacidification tower 1 through a heat exchanger 5, and then entering the upper part of the deacidification tower 1, wherein the top of the deacidification tower 1 inhibits the escape of ammonia gas through pressurization operation, so that the acid gas product at the tower top of the deacidification tower 1 only contains a small amount of ammonia gas;
2) Acid gas escapes from the top of the deacidification tower 1, and barren liquor collected from the side line of the deacidification tower 1 exchanges heat with rich liquor of the desulfurization tower and residual ammonia water and returns to the desulfurization tower for recycling;
3) Pressurizing the liquid phase at the bottom of the deacidification tower 1 by a pump 3, and then feeding the liquid phase into the top of an ammonia still 2 for ammonia distillation;
4) After the gas phase at the top of the ammonia still 2 escapes, one part returns to the bottom of the deacidification tower 1, and the other part enters a tower top condenser 4 for concentration treatment;
5) The gas phase after being concentrated by the condenser 4 escapes to form an ammonia product, and the liquid phase returns to the ammonia still 2 to be used as reflux;
6) Adding alkali liquor in the middle of the ammonia still 2 for removing fixed ammonia, and introducing steam at the bottom as a tower bottom heat source; and (3) discharging ammonia distillation wastewater from the bottom of the ammonia distillation tower 2, and returning part of the ammonia distillation wastewater to a desulfurization section to be used as stripping water for desulfurization and ammonia washing.
The tower top operating pressure of the deacidification tower 1 is 0.2-0.8 MPaG.
The above, only be the concrete implementation of the preferred embodiment of the present invention, but the protection scope of the present invention is not limited thereto, and any person skilled in the art is in the technical scope of the present invention, according to the technical solution of the present invention and the utility model, the concept of which is equivalent to replace or change, should be covered within the protection scope of the present invention.
Claims (2)
1. A pressurization deacidification ammonia distillation system is characterized by comprising a deacidification tower, an ammonia distillation tower, a heat exchanger, a condenser and a pump; the top of the deacidification tower is provided with an acid gas outlet, the upper part of the deacidification tower is provided with a mixed liquid inlet, the middle part of the deacidification tower is provided with a lean liquid side draw outlet, the lower part of the deacidification tower is provided with an ammonia evaporation gas inlet, and the bottom of the deacidification tower is provided with an ammonia water outlet; the mixed liquid inlet is connected with a first heat exchange medium outlet of the heat exchanger, and a first heat exchange medium inlet of the heat exchanger is respectively connected with the residual ammonia water pipeline and the desulfurizing tower rich liquid pipeline; a second heat exchange medium inlet of the heat exchanger is connected with a lean solution side draw-out outlet, and a second heat exchange medium outlet is connected with a lean solution output pipeline; the top of the ammonia still is provided with an ammonia still gas outlet, the upper part is provided with an ammonia water inlet and a reflux liquid inlet, the middle part is provided with an alkali liquor inlet, the lower part is provided with a steam inlet, and the bottom is provided with an ammonia still wastewater outlet; an ammonia water outlet of the deacidification tower is connected with an ammonia water inlet of the ammonia still through a pump; an ammonia evaporation gas outlet of the ammonia evaporation tower is respectively connected with an ammonia evaporation gas inlet of the deacidification tower and an inlet of a condenser, a condensate outlet of the condenser is connected with a reflux liquid inlet of the ammonia evaporation tower, and a gas phase outlet of the condenser is connected with an ammonia gas conveying pipeline; an ammonia distillation wastewater outlet of the ammonia distillation tower is respectively connected with an ammonia distillation wastewater conveying pipeline and a stripping water conveying pipeline.
2. The system of claim 1, wherein a plurality of layers of packing or trays are arranged in the deacidification tower between the mixed liquid inlet and the lean side draw outlet, and a plurality of layers of packing or trays are arranged in the deacidification tower between the lean side draw outlet and the ammonia distillation gas inlet.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201920189242.8U CN209771782U (en) | 2019-02-11 | 2019-02-11 | Pressurization deacidification ammonia distillation system |
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| CN201920189242.8U CN209771782U (en) | 2019-02-11 | 2019-02-11 | Pressurization deacidification ammonia distillation system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109647150A (en) * | 2019-02-11 | 2019-04-19 | 中冶焦耐(大连)工程技术有限公司 | A kind of pressurization deacidifion technique and system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109647150A (en) * | 2019-02-11 | 2019-04-19 | 中冶焦耐(大连)工程技术有限公司 | A kind of pressurization deacidifion technique and system |
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