CN101585520A - Method for preparing nitric acid - Google Patents
Method for preparing nitric acid Download PDFInfo
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- CN101585520A CN101585520A CNA200910054256XA CN200910054256A CN101585520A CN 101585520 A CN101585520 A CN 101585520A CN A200910054256X A CNA200910054256X A CN A200910054256XA CN 200910054256 A CN200910054256 A CN 200910054256A CN 101585520 A CN101585520 A CN 101585520A
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Abstract
The invention relates to a method for preparing nitric acid, comprising the following steps: filtering air through a filtering device (1); using a cooling device to cool the air with relative humidity of between 60% and 100% from the temperature of between 25 and 40 DEG C to the temperature of between 10 and 20 DEG C; deforming with a demister (3); extracting condensed water in the air through a drainage pipe (6) to reduce the absolute air humidity to a range of between 9.4 and 17.8 g/m<3>; compressing the air with an air compressor (5); after mixing with ammonia gas, sending to a sequent reactor for reacttion, and then obtaining nitric acid with weight concentration higher than 68%. The method provided by the invention is simple and easy. Using the method, nitric acid with a weight concentration higher than 68% especially can be produced steadily and singly in summer at relatively high temperature and humidity, satisfying the requirements of related industrial departments.
Description
Technical field
The present invention relates to the method that ammonia adopts the atmospheric oxidation nitric acid synthesis, the removal method that relates in particular to water in air part.
Background technology
What industrial production nitric acid adopted is oxidation proceses of ammonia, and this method utilizes three main chemical reactions to obtain nitric acid:
I)4NH
3+5O
2→4NO+6H
2O(g)
II)2NO+O
2(g)→2NO
2(g)
III)3NO
2(g)+H
2O→2HNO
3+NO(g)
Existing manufacturing technique has adopted different oxidative ammonolysis pressure and nitrogen oxide absorption pressure to produce nitric acid.More advanced process using be " two pressurization " technology, promptly under the pressure of 2～3.5bar, carry out oxidative ammonolysis, and under the pressure of 9.5～11.5bar, carry out absorption reaction.
Air and ammonia through overdraft are mixed into reactor, and the energy of the high-temperature gas after the ammonia oxidation is progressively reclaimed in one group of interchanger, and after temperature reduces, water wherein will form weak acid with nitrogen oxide, will be pumped into the absorption tower by weak acid then.The oxidized nitrogen compressor of other gases further compresses, and enters the absorption tower after reclaiming through another group interchanger heat.Absorbing cat head adding process water, adverse current fully contacts with the gas that is rich in nitrogen oxide, absorbs.The nitric acid that generates becomes finished product nitric acid at bleaching tower after bleaching from the secondary air of air compressor equally.
The nitric acid that adopts the consistent ground of existing processes to produce 68% (w/w) concentration separately is that the weight concentration of very difficult, the present nitric acid that technology obtained is generally 50～65%, can not satisfy the needs of the parties concerned.
Summary of the invention
The purpose of this invention is to provide a kind of method for preparing nitric acid, to overcome the above-mentioned defective that prior art exists.
Method of the present invention, comprise the steps: air is passed through filtration unit earlier, and then enter refrigerating unit, with temperature is that 25～40 ℃ and relative humidity are that the temperature of 60～100% air is reduced to 10～20 ℃, airborne moisture content is condensed, and then enter scum dredger, the moisture content that is condensed in the air is discharged from by drainage pipeline, make air absolute humidity be reduced to 9.4～17.8g/m3, and then enter air compressor compression, mix with ammonia then, be sent to follow-up reactor and react, the acquisition weight concentration is the nitric acid more than 68%.
Described relative humidity is defined as follows:
In the air water content and synthermal under the per-cent of saturation moisture content.
Method of the present invention, essence have provided a kind of by at air compressor inlet the method that the air cooling dehumidification system improves nitric acid synthesis concentration being installed.This method can be cooled off the atmosphere of heat after filtering, remove water of condensation drop wherein then, thereby improve the concentration of product nitric acid, and do not influence the work of air filtering system.
Method of the present invention, simple, especially can be in summer, under the temperature and humidity condition with higher, stably independent production weight is the nitric acid more than 68%, can satisfy the needs of relevant branch of industry.
Description of drawings
Fig. 1 is a schema of the present invention.
Embodiment
Referring to Fig. 1, method of the present invention, comprise the steps: air earlier by filtration unit 1, and then enter refrigerating unit 2, with temperature is that 25～40 ℃ and relative humidity are that the temperature of 60～100% air is reduced to 10～20 ℃, airborne moisture content is condensed, and then enter scum dredger 3, the moisture content that is condensed in the air is discharged from by drainage pipeline 6, make air absolute humidity be reduced to 9.4～17.8g/m3, and then enter air compressor 5 compressions, mix with ammonia then, be sent to follow-up reactor and react, the acquisition weight concentration is 68% nitric acid.
Referring to Fig. 1, described filtration unit 1 is the two-stage filtration net, and the front one-level is filtered large size impurity, and the back one-level is filtered meticulous impurity;
Described refrigerating unit 2 adopts interchanger, and described interchanger preferably adopts finned heat exchanger, is the general product in this area, can adopt GEA company finned tube heat exchanger product;
Described scum dredger adopts the baffling template, is the general product in this area, and can adopt the ALUPRO company trade mark is the WS-A product; The drop elimination factor reaches 98%.
The form of described filtering net, interchanger and scum dredger is unimportant, all can adopt the general product in this area.
Preferably, described drainage pipeline 6 is provided with fluid-tight member 4.Because filtering net, the pressure drop that equipment such as interchanger produce, the system behind the interchanger is little negative pressure, when above-mentioned water of condensation is discharged into extraneous storm-water system, described fluid-tight member 4 can prevent that the atmosphere of extraneous filtered from leaking to advance in the system from these pipelines.Described fluid-tight member 4 is a U type pipe.
Embodiment 1
Adopt the device of Fig. 1.
Operational condition:
The temperature of air is 38.2 ℃, and relative humidity is 91%, and absolute humidity is 6.19g/m3;
The temperature of cooling back air is 13.5 ℃, and relative humidity is 100%, and absolute humidity is 1.52g/m3
Interchanger adopts finned heat exchanger, and adopting the GEA company trade mark is FT-1.1-5000 finned tube heat exchanger product;
Scum dredger adopts the baffling template, and adopting the ALUPRO company trade mark is the WS-A product;
Cooled air mixes with ammonia after so entering the air compressor compression, is sent to follow-up reactor and reacts, adopt conventional method, carry out oxidative ammonolysis under the pressure of 3.0bar, carry out absorption reaction under the pressure of 11.15bar, the acquisition weight concentration is 68.2% nitric acid.
Embodiment 2
Adopt the device of Fig. 1.
Operational condition:
The temperature of air is 36.7 ℃, and relative humidity is 87%, and absolute humidity is 5.40g/m3;
The temperature of cooling back air is 15.2 ℃, and relative humidity is 100%, and absolute humidity is 1.69g/m3;
Interchanger adopts finned heat exchanger, and adopting the GEA company trade mark is FT-1.1-5000 finned tube heat exchanger product;
Scum dredger adopts the baffling template, and adopting the ALUPRO company trade mark is the WS-A product;
Cooled air mixes with ammonia after so entering the air compressor compression, is sent to follow-up reactor and reacts, adopt conventional method, carry out oxidative ammonolysis under the pressure of 2.8bar, carry out absorption reaction under the pressure of 10.8bar, the acquisition weight concentration is 68.0% nitric acid.
Claims (7)
1. the method for preparing nitric acid, it is characterized in that, comprise the steps: air earlier by filtration unit (1), and then enter refrigerating unit (2), with temperature is that 25～40 ℃ and relative humidity are that the temperature of 60～100% air is reduced to 10～20 ℃, and then enter scum dredger (3), the moisture content that is condensed in the air is discharged from by drainage pipeline (6), make air absolute humidity be reduced to 9.4～17.8g/m3, and then enter air compressor (5) compression, mix with ammonia then, be sent to follow-up reactor and react, the acquisition weight concentration is 68% nitric acid.
2. method according to claim 1 is characterized in that, described filtration unit (1) is the two-stage filtration net.
3. method according to claim 1 is characterized in that, described refrigerating unit (2) is an interchanger.
4. method according to claim 1 is characterized in that, described interchanger adopts finned heat exchanger.
5. method according to claim 1 is characterized in that, described scum dredger adopts the baffling template.
6. method according to claim 1 is characterized in that, described drainage pipeline (6) is provided with fluid-tight member (4).
7. method according to claim 1 is characterized in that, described fluid-tight member (4) is a U type pipe.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910054256XA CN101585520B (en) | 2009-07-01 | 2009-07-01 | Method for preparing nitric acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910054256XA CN101585520B (en) | 2009-07-01 | 2009-07-01 | Method for preparing nitric acid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101585520A true CN101585520A (en) | 2009-11-25 |
| CN101585520B CN101585520B (en) | 2011-12-21 |
Family
ID=41369979
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200910054256XA Active CN101585520B (en) | 2009-07-01 | 2009-07-01 | Method for preparing nitric acid |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102502541A (en) * | 2011-10-21 | 2012-06-20 | 天津华景化工新技术开发有限公司 | Production method of high-concentration dilute nitric acid |
| CN103072962A (en) * | 2011-10-26 | 2013-05-01 | 上海巴斯夫聚氨酯有限公司 | Preparation method of electronic grade nitric acid |
| CN105134560A (en) * | 2015-08-23 | 2015-12-09 | 安徽金禾实业股份有限公司 | Method for freezing and dehumidifying air of inlet of compressor in nitric acid production |
-
2009
- 2009-07-01 CN CN200910054256XA patent/CN101585520B/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102502541A (en) * | 2011-10-21 | 2012-06-20 | 天津华景化工新技术开发有限公司 | Production method of high-concentration dilute nitric acid |
| CN103072962A (en) * | 2011-10-26 | 2013-05-01 | 上海巴斯夫聚氨酯有限公司 | Preparation method of electronic grade nitric acid |
| CN105134560A (en) * | 2015-08-23 | 2015-12-09 | 安徽金禾实业股份有限公司 | Method for freezing and dehumidifying air of inlet of compressor in nitric acid production |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101585520B (en) | 2011-12-21 |
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