CN110054201B - Process for producing refined ammonia water by deacidifying residual ammonia water and simultaneously realizing heat coupling - Google Patents
Process for producing refined ammonia water by deacidifying residual ammonia water and simultaneously realizing heat coupling Download PDFInfo
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- CN110054201B CN110054201B CN201910300066.5A CN201910300066A CN110054201B CN 110054201 B CN110054201 B CN 110054201B CN 201910300066 A CN201910300066 A CN 201910300066A CN 110054201 B CN110054201 B CN 110054201B
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/10—Separation of ammonia from ammonia liquors, e.g. gas liquors
Abstract
The invention relates to a process for producing refined ammonia water by deacidifying residual ammonia water and realizing heat coupling at the same time, wherein the residual ammonia water exchanges heat with ammonia distillation wastewater and is mixed with an acid solution and then enters a deacidification tower, free ammonia in the residual ammonia water is changed into fixed ammonia, acid gas escapes from the top of the deacidification tower, and part of ammonia water after the acid gas is removed is mixed with alkali liquor and enters the top of the ammonia distillation tower for ammonia distillation treatment; the other part of ammonia water enters a condenser at the top of the ammonia still and returns to the bottom of the deacidification tower after being heated to supply heat to the deacidification tower; the fixed ammonia in the ammonia water is changed into free ammonia under the action of alkali liquor, the ammonia gas escapes from the top of the ammonia still, and the ammonia gas is condensed by a condenser to form an ammonia product. According to the invention, the acid addition operation is carried out in the deacidification tower, so that the escape of ammonia gas is inhibited, and the ammonia product is effectively recovered; the temperature of the top of the ammonia still is controlled to be higher than the temperature of the bottom of the deacidification tower, so that the condenser at the top of the ammonia still can supply heat for the desulfurization tower while the ammonia is concentrated, and the overall energy consumption of the process is reduced in a heat coupling mode.
Description
Technical Field
The invention relates to the technical field of coke oven gas purification and ammonia recovery, in particular to a process for producing refined ammonia water by deacidifying residual ammonia water and realizing heat coupling.
Background
In the production process of the coke oven, after the raw coke oven gas is sprayed and cooled by circulating ammonia water, condensate in the raw coke oven gas is mixed with the circulating ammonia water, wherein most of the condensate is used as the circulating ammonia water for recycling, and the rest of the condensate is used as the residual ammonia water and sent to an ammonia distillation section, and the oil is filtered out and then the ammonia water is distilled. The residual ammonia water contains a certain amount of free ammonia and fixed ammonia, and a small amount of hydrogen cyanide, hydrogen sulfide and carbon dioxide, the acid components and ammonia are distilled out together by adding alkali at a reasonable position in the existing residual ammonia water treatment process, ammonia distillation wastewater at the bottom of the tower enters a sewage treatment workshop for purification treatment, but ammonia products at the top of the tower contain a certain amount of hydrogen cyanide, hydrogen sulfide and carbon dioxide. Along with the increasingly strict environmental protection requirements of the national environment, the flue gas desulfurization and denitration process becomes a common process, the demand of ammonia products is gradually increased, but the ammonia product prepared from the residual ammonia water contains a large amount of acidic components, and the application of the ammonia product is greatly limited. In addition, a large amount of energy is consumed in the deacidification and ammonia distillation process of the residual ammonia water, and social benefits and enterprise economic benefits are greatly influenced.
Disclosure of Invention
The invention provides a process for producing refined ammonia water by deacidifying residual ammonia water and realizing heat coupling, which comprises the steps of converting the form of ammonia in a liquid phase by carrying out acid adding operation in a deacidification tower, inhibiting ammonia gas from escaping, completing step-by-step desorption of hydrogen sulfide and ammonia, and effectively recovering ammonia products; the temperature of the top of the ammonia still is controlled to be higher than the temperature of the bottom of the deacidification tower, so that the condenser on the top of the ammonia still can supply heat for the desulfurization tower while the ammonia is concentrated, and the overall energy consumption of the process is reduced in a heat coupling mode.
In order to achieve the purpose, the invention adopts the following technical scheme:
a process for producing refined ammonia water by deacidifying residual ammonia water and simultaneously realizing heat coupling comprises the following steps:
1) Exchanging heat between the residual ammonia water from the condensation blowing section and the ammonia distillation wastewater through a heat exchanger, mixing the heat and the acidic solution, and then entering the top of a deacidification tower;
2) The bottom of the deacidification tower is supplied with heat by a condenser at the top of the ammonia still, and free ammonia in the residual ammonia water is changed into fixed ammonia due to the addition of the acidic solution, so that the escape of ammonia gas is inhibited; the acid gas escapes from the top of the deacidification tower and is sent to a crude gas pipeline at the upstream of the desulfurization section;
3) The liquid phase at the bottom of the deacidification tower after removing the acid gas is ammonia water, after the ammonia water pump is used for pressurizing, a part of the ammonia water and alkali liquor are mixed and enter from the top of the ammonia still for ammonia distillation treatment; the other part of ammonia water enters a condenser at the top of the ammonia still and returns to the bottom of the deacidification tower after being heated to supply heat to the deacidification tower;
4) The top operating pressure of the ammonia still is 0.15Mpa (a) -1 Mpa (a), and the top pressure of the ammonia still is greater than the bottom pressure of the deacidification tower; the bottom of the ammonia still supplies heat through a heat source, the fixed ammonia in the ammonia water is changed into free ammonia under the action of alkali liquor, and the ammonia gas escapes from the top of the ammonia still and enters a condenser at the top of the ammonia still for concentration treatment;
5) The gas phase after being concentrated by the condenser escapes to form an ammonia product, and the liquid phase returns to the ammonia still to be used as reflux;
6) And (4) the ammonia distillation wastewater discharged from the tower bottom of the ammonia distillation tower exchanges heat with the residual ammonia water through a heat exchanger, and is sent to a sewage treatment working section.
And adding the acidic solution into the residual ammonia water pipeline before the residual ammonia water enters the deacidification tower, or simultaneously entering the deacidification tower together with the residual ammonia water at the top of the deacidification tower.
And the alkali liquor is added into an ammonia water pipeline before ammonia water at the bottom of the deacidification tower enters an ammonia still to distill ammonia, or enters the ammonia still together with the ammonia water at the top of the ammonia still.
The heat source at the bottom of the ammonia still is steam delivered by a reboiler of the ammonia still or an external steam pipeline.
Compared with the prior art, the invention has the beneficial effects that:
1) The acid adding operation is carried out in the acid removing tower, the form of ammonia in a liquid phase is changed, the ammonia gas is inhibited from escaping, the stepwise desorption of hydrogen sulfide and ammonia is completed, and the ammonia product is effectively recovered;
2) The pressure at the top of the ammonia still is increased, so that the temperature at the top of the ammonia still is higher than the temperature at the bottom of the deacidification tower, and a condenser at the top of the ammonia still serves as a reboiler of the desulfurization tower to supply heat to the desulfurization tower while ammonia gas is concentrated;
3) The overall energy consumption of the process is reduced by a heat coupling mode;
4) The deacidification tower does not need to be provided with a reboiler, and the area required by the reboiler at the bottom of the ammonia still is reduced.
Drawings
Fig. 1 is a flow chart of a process for producing refined ammonia water by deacidifying residual ammonia water and simultaneously realizing heat coupling according to the invention.
In the figure: 1. deacidifying tower 2, heat exchanger 3, ammonia still 4, ammonia water pump 5, ammonia still waste water pump 6, condenser 7, ammonia still reboiler
Detailed Description
The following further describes embodiments of the present invention in conjunction with the attached figures:
as shown in figure 1, the process for deacidifying the residual ammonia water to produce the refined ammonia water and simultaneously realize heat coupling comprises the following steps of:
1) The residual ammonia water from the condensation blowing section and the ammonia distillation wastewater exchange heat through a heat exchanger 2, and then are mixed with an acid solution to enter the top of a deacidification tower 1;
2) The heat is supplied from a condenser 6 at the top of the ammonia still 3 at the bottom of the deacidification tower 1, and free ammonia in the residual ammonia water is changed into fixed ammonia due to the addition of the acidic solution, so that the escape of ammonia gas is inhibited; the acid gas escapes from the top of the deacidification tower 1 and is sent to a crude gas pipeline at the upstream of the desulfurization section;
3) The liquid phase at the bottom of the deacidification tower after removing the acid gas is ammonia water, after the ammonia water is pressurized by an ammonia water pump 4, a part of the ammonia water and alkali liquor are mixed from the top of an ammonia still 3 to enter for ammonia distillation treatment; the other part of ammonia water enters a condenser 6 at the top of the ammonia still 3, and returns to the bottom of the deacidification tower 1 after being heated to supply heat to the deacidification tower 1;
4) The top operating pressure of the ammonia still 3 is 0.15Mpa (a) -1 Mpa (a), and the top pressure of the ammonia still 3 is greater than the bottom pressure of the deacidification tower 1; the bottom of the ammonia still 3 supplies heat through a heat source, the fixed ammonia in the ammonia water is changed into free ammonia under the action of alkali liquor, and the ammonia gas escapes from the top of the ammonia still 3 and enters a condenser 6 at the top of the ammonia still for concentration treatment;
5) The gas phase condensed by the condenser 6 escapes to become ammonia products, and the liquid phase returns to the ammonia still 3 as reflux;
6) And the ammonia distillation wastewater discharged from the tower bottom of the ammonia distillation tower 3 is subjected to heat exchange with the residual ammonia water through the heat exchanger 2 and then is sent to a sewage treatment working section.
The acidic solution is added into the residual ammonia water pipeline before the residual ammonia water enters the deacidification tower 1, or enters the deacidification tower 1 together with the residual ammonia water at the top of the deacidification tower.
The alkali liquor is added into an ammonia water pipeline before ammonia water at the bottom of the deacidification tower 1 enters the ammonia still 3 for ammonia distillation, or enters the ammonia still 3 together with the ammonia water at the top of the ammonia still.
The heat source at the bottom of the ammonia still 3 is steam delivered from an ammonia still reboiler 7 or an external steam pipeline.
The key operation steps of the process for producing refined ammonia water by deacidifying the residual ammonia water and simultaneously realizing heat coupling are that firstly, an acid solution is added into the residual ammonia water before deacidifying the residual ammonia water, and secondly, an alkali liquor is added into the ammonia water before ammonia water at the bottom of the deacidification tower is distilled.
Fig. 1 shows a specific composition mode of a system capable of implementing the process of the invention, and the system comprises a deacidification tower 1, an ammonia still 3, a condenser 6, an ammonia still reboiler 7, a heat exchanger 2, an ammonia water pump 4 and an ammonia distillation wastewater pump 5. The top of the deacidification tower 1 is provided with an acid gas outlet and a mixed liquid inlet of the residual ammonia water and the acidic solution, the lower part of the deacidification tower is provided with a gas-liquid phase return port, and the bottom of the deacidification tower is provided with an ammonia water outlet; wherein, the mixed liquid inlet of the residual ammonia water and the acidic solution in the deacidification tower 1 is connected with the first heat exchange medium outlet of the heat exchanger 2 through a mixed liquid pipeline, and the mixed liquid pipeline at the section is provided with an acidic solution inlet connected with an acidic solution conveying pipeline; a first heat exchange medium inlet of the heat exchanger 2 is connected with a residual ammonia water conveying pipeline; and a second heat exchange medium inlet of the heat exchanger 2 is connected with an outlet of an ammonia distillation wastewater pump 5, an inlet of the ammonia distillation wastewater pump 5 is connected with an ammonia distillation wastewater outlet at the bottom of the ammonia distillation tower through an ammonia distillation wastewater pipeline, and a second heat exchange medium outlet of the heat exchanger 2 is connected with an ammonia distillation wastewater conveying pipeline.
The top of the ammonia still 3 is provided with an ammonia gas outlet, the upper part is provided with an ammonia water inlet and a reflux liquid inlet, the lower part is provided with an ammonia still reboiler 7, and the bottom is provided with an ammonia still wastewater outlet; wherein, the ammonia evaporation wastewater outlet is connected with the inlet of an ammonia evaporation wastewater pump 5 through an ammonia evaporation wastewater pipeline; an ammonia water outlet at the bottom of the deacidification tower 1 is connected with an inlet of an ammonia water pump 4 through an ammonia water pipeline, an outlet of the ammonia water pump 4 is respectively connected with an ammonia water inlet of an ammonia still 3 and a first heat exchange medium inlet of a condenser 6 through an ammonia water pipeline, and an alkali liquor inlet arranged on the ammonia water pipeline in front of the ammonia still 3 is connected with an alkali liquor conveying pipeline; a first heat exchange medium outlet of the condenser 6 is connected with a gas-liquid phase return port at the lower part of the deacidification tower 1. An ammonia gas outlet of the ammonia still 3 is connected with a second heat exchange medium inlet of the condenser 6 through an ammonia gas pipeline, and a second heat exchange medium outlet of the condenser 6 is connected with an ammonia gas product pipeline. A condensate outlet of the condenser 6 is connected with a reflux inlet at the top of the ammonia still 3 through a condensate pipeline.
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 as the technical solutions and the inventive concepts of the present invention within the technical scope of the present invention.
Claims (2)
1. A process for producing refined ammonia water and simultaneously realizing heat coupling by deacidifying residual ammonia water is characterized by comprising the following steps:
1) Exchanging heat between the residual ammonia water from the condensation blowing section and the ammonia distillation wastewater through a heat exchanger, mixing the heat and the acidic solution, and then entering the top of a deacidification tower; the acidic solution is added into the residual ammonia water pipeline before the residual ammonia water enters the deacidification tower, or enters the deacidification tower together with the residual ammonia water at the top of the deacidification tower;
2) The bottom of the deacidification tower is supplied with heat by a condenser at the top of the ammonia still, and free ammonia in the residual ammonia water is changed into fixed ammonia due to the addition of the acidic solution, so that the escape of ammonia gas is inhibited; the acid gas escapes from the top of the deacidification tower and is sent to a crude gas pipeline at the upstream of the desulfurization section;
3) The liquid phase at the bottom of the deacidification tower after removing the acid gas is ammonia water, after the ammonia water pump is used for pressurizing, a part of the ammonia water and alkali liquor are mixed and enter from the top of the ammonia still for ammonia distillation treatment; the other part of ammonia water enters a condenser at the top of the ammonia still and returns to the bottom of the deacidification tower after being heated to supply heat to the deacidification tower; the alkali liquor is added into an ammonia water pipeline before ammonia water at the bottom of the deacidification tower enters an ammonia still for ammonia distillation, or enters the ammonia still together with the ammonia water at the top of the ammonia still;
4) The top operating pressure of the ammonia distillation tower is 0.15-1 Mpa, and the pressure is absolute pressure; the pressure at the top of the ammonia still is higher than the pressure at the bottom of the deacidification tower; the bottom of the ammonia still supplies heat through a heat source, the fixed ammonia in the ammonia water is changed into free ammonia under the action of alkali liquor, and the ammonia gas escapes from the top of the ammonia still and enters a condenser at the top of the ammonia still to be concentrated;
5) The gas phase after being concentrated by the condenser escapes to form an ammonia product, and the liquid phase returns to the ammonia still to be used as reflux;
6) And (4) the ammonia distillation wastewater discharged from the tower bottom of the ammonia distillation tower exchanges heat with the residual ammonia water through a heat exchanger, and is sent to a sewage treatment working section.
2. The process of claim 1, wherein the heat source at the bottom of the ammonia still is from the reboiler of the ammonia still or from steam delivered from an external steam pipeline.
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| CN112023651A (en) * | 2020-09-08 | 2020-12-04 | 四川省达州钢铁集团有限责任公司 | Method and system for desulfurization and denitrification of coke oven flue gas by using residual ammonia water |
| CN112551793B (en) * | 2020-12-10 | 2022-11-08 | 天津大学 | Ammonia distillation method and device for ammonia-containing wastewater |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4240808A (en) * | 1977-10-03 | 1980-12-23 | Metallgesellschaft Aktiengesellschaft | Processing aqueous effluent liquors from degasification or gasification of coal |
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| CN101717096B (en) * | 2009-12-29 | 2012-01-11 | 中钢集团天澄环保科技股份有限公司 | Technology for preparing desulfurizing agent ammonia water in sintering flue gas desulfurization by coking residual ammonia water |
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Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4240808A (en) * | 1977-10-03 | 1980-12-23 | Metallgesellschaft Aktiengesellschaft | Processing aqueous effluent liquors from degasification or gasification of coal |
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