CN106698368A - Nitric oxide wet oxidation process - Google Patents
Nitric oxide wet oxidation process Download PDFInfo
- Publication number
- CN106698368A CN106698368A CN201510789424.5A CN201510789424A CN106698368A CN 106698368 A CN106698368 A CN 106698368A CN 201510789424 A CN201510789424 A CN 201510789424A CN 106698368 A CN106698368 A CN 106698368A
- Authority
- CN
- China
- Prior art keywords
- acid
- nitric oxide
- nitrogen dioxide
- nitric
- tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Landscapes
- Treating Waste Gases (AREA)
Abstract
The invention relates to a nitric oxide wet oxidation process, and belongs to the technical field of nitric acid. The nitric oxide wet oxidation process includes the steps that in a nitric acid absorption tower, nitric oxide gas from a separator enters a mixed gas absorption section through the tower bottom, and after nitrogen dioxide is absorbed by nitric acid from a nitrogen dioxide absorption section, a finished acid product is generated and conveyed to an acid warehouse after going out of the tower; nitrogen dioxide gas which is not absorbed and nitric oxide gas enter an oxidation section, nitric oxide makes contact with air in a countercurrent mode to generate nitrogen dioxide, nitrogen dioxide enters the nitrogen dioxide absorption section and is absorbed by water sprayed from the tower top to generate dilute nitric acid, and dilute nitric acid goes down along the tower wall through an acid guiding pipe of a bottom layer sieve plate of the nitrogen dioxide absorption section and directly enters the mixed gas absorption section. The nitric oxide wet oxidation process is characterized in that nitric acid for cooling exists in the oxidation section. The temperature of the gas entering the nitrogen dioxide absorption section is controlled below 40 DEG C, so that the acid concentration in the acid absorption section is gradually reduced along with increase of the number of sieve plates, in this way, the output acid concentration at the tower bottom is larger than 50%, and the product quality is stable.
Description
Technical field
The present invention relates to chemical field, and in particular to a kind of nitric oxide wet process oxidation technology.
Background technology
Nitric acid is produced generally by ammoxidation, and its technical process is usually：Ammonia is catalyzed oxygen in high temperature by platinum-rhodium alloy net
Metaplasia into nitric oxide, after reclaiming heat through waste heat boiler, by entering acid absorption column after separator, in acid absorption column
Nitric oxide continues to aoxidize generation nitrogen dioxide, and absorbing nitrogen dioxide with water generates nitric acid, and acid absorption column tail gas is inhaled into alkali
Tower is received, neutralizer is produced, salt made from earth containing a comparatively high percentage of sodium chloride is further produced.
Nitric oxide production dry oxidation is typically used in the acid absorption column of prior art, below with 12 layers of acid absorption column of column plate
As a example by be specifically described：9 layers go out acid and have an acid tube to cause outside tower, and 4 layers are come downwards to subsequently into tower along wall, carry out
Acid is gone out by bottom of towe after bleaching.Absorption tower 5-8 layers without liquid exist, in this 4 layers of column plates, using air with do not absorb
Nitrogen oxide counter current contacting, by conversion of nitric oxide gas be nitrogen dioxide, in the step industry in this 4 layers claim
Make " oxidation of nitric oxide ".Because the reaction is exothermic reaction, gas can constantly bring the heat of generation into upper strata tower
Plate, causing 9-10 layers of acidity cannot improve, and occur in that 9,10 layers of acid concentration of column plate are less than 11,12 layers of column plate acid
The phenomenon of concentration, causes bottom of towe acid concentration to be often up to the requirement qualified less than design.
The content of the invention
The present invention is directed to problems of the prior art, there is provided a kind of nitric oxide wet process oxidation technology, main to utilize
The acid solution of low temperature solves the problems of the prior art in oxidation of nitric oxide section absorbing reaction liberated heat.
The present invention adopts the following technical scheme that realization：
Nitric oxide wet process oxidation technology, is included in nitric acid absorber, and the oxides of nitrogen gas from separator is by bottom of towe
Into mixed gas absorber portion, after absorbing nitrogen dioxide by the nitric acid from nitrogen dioxide absorber portion, the finished acid of generation,
Sour storehouse is delivered to after going out tower；Unabsorbed nitrogen dioxide gas enter oxidation panel, nitric oxide and air with nitric oxide gas
Counter current contacting generates nitrogen dioxide, subsequently into nitrogen dioxide absorber portion, after the water sprayed by tower top absorbs generation dust technology
Dust technology by nitrogen dioxide absorber portion bottom sieve plate acid guiding pipe, it is descending along tower wall, be directly entered mixed gas absorber portion,
It is characterized in that oxidation panel also has the nitric acid for cooling down.
Specific technical scheme of the invention is as follows：Nitric acid from cooler enters the superiors' sieve plate of oxidation of nitric oxide section,
After nitric oxide gas counter current contacting from bottom to top, and absorbing reaction heat, from the orlop tower of oxidation of nitric oxide section
Plate enters sour storage tank, and squeezes into cooler by sour pump, circulates according to this.
The temperature for cooling down nitric acid is 30-40 DEG C；Supplemented by the qualified finished acid from acid absorption column in sour storage tank；Sour pump
Another sour storehouse of outlet connection；Acid absorption column goes out acid concentration >=50%；The acid strength of upper absorber portion is with successively decreasing for pedal
It is incremented by.
The present invention is had advantageous effect in that：Gas temperature into nitrogen dioxide absorber portion is controlled in less than 40 DEG C,
(sieve plate number successively decreases 1 layer, and the concentration of nitric acid increases by one nitrogen dioxide absorber portion acid strength is incremented by with successively decreasing for sieve plate number
Percentage point), thus to bring, bottom of towe goes out acid concentration more than 50%, makes product quality stabilization.
Specific embodiment
Embodiment
The ammonia come by preliminary filtered air and liquefied ammonia evaporation is mixed according to the ratio of prior art in blender, so
Afterwards enter ammoxidation device, the nitrogen oxides of reaction, through waste heat boiler reclaim heat after, into acid absorption column, acid absorption column origin
The water of self-water-supplying operation carries out spray-absorption.
Absorption tower 1-4 layers of sieve plate is mixed gas absorber portion, and 5-8 layers of sieve plate is oxidation of nitric oxide section, and 9-12 sections is titanium dioxide
Nitrogen absorber portion.
9 layers of absorption tower go out acid has an acid tube to cause outside tower, and 4 layers of sieve plate are come downwards to along wall, subsequently into tower, further inhales
After receiving the nitrogen dioxide in mixed gas, bleaching generation finished acid is carried out, acid is gone out by bottom of towe.From the nitric acid of cooler, (temperature is
30-40 DEG C) enter 8 layers of sieve plate of oxidation of nitric oxide section, and nitric oxide gas counter current contacting from bottom to top, and absorb
After reaction heat, sour storage tank is entered from oxidation of nitric oxide 5 layers of sieve plate of section, and cooler is squeezed into by sour pump, circulated according to this；Acid storage
Supplemented by the qualified finished acid from acid absorption column in groove；The sour storehouse of another outlet connection of sour pump；Acid absorption column go out acid concentration >=
50%, bottom of towe goes out acid and squeezes into sour storehouse.
The tail gas that acid absorbs enters alkali adsorption tower by the top of tower, produces neutralizer, and neutralizer removes salt made from earth containing a comparatively high percentage of sodium chloride.
Claims (3)
1. nitric oxide wet process oxidation technology, is included in nitric acid absorber, and the oxides of nitrogen gas from separator enters mixed gas absorber portion by bottom of towe, and after absorbing nitrogen dioxide by the nitric acid from nitrogen dioxide absorber portion, the finished acid of generation delivers to sour storehouse after going out tower；Unabsorbed nitrogen dioxide gas enter oxidation panel with nitric oxide gas, nitric oxide contacts generation nitrogen dioxide with air inversion, subsequently into nitrogen dioxide absorber portion, after the water sprayed by tower top absorbs generation dust technology, dust technology by nitrogen dioxide absorber portion bottom sieve plate acid guiding pipe, it is descending along tower wall, it is directly entered mixed gas absorber portion, it is characterised in that oxidation panel also has the nitric acid for cooling down；Nitric acid from cooler enters the superiors' sieve plate of oxidation of nitric oxide section, after nitric oxide gas counter current contacting from bottom to top, and absorbing reaction heat, sour storage tank is entered from the orlop column plate of oxidation of nitric oxide section, and cooler is squeezed into by sour pump, circulate according to this.
2. nitric oxide wet process oxidation technology according to claim 1, it is characterised in that the temperature of cooling acid is 30-40 DEG C；Acid absorption column goes out acid concentration >=50%.
3. nitric oxide wet process oxidation technology according to claim 1, it is characterised in that supplemented by the qualified finished acid from acid absorption column in sour storage tank；The sour storehouse of another outlet connection of sour pump.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510789424.5A CN106698368A (en) | 2015-11-16 | 2015-11-16 | Nitric oxide wet oxidation process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510789424.5A CN106698368A (en) | 2015-11-16 | 2015-11-16 | Nitric oxide wet oxidation process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106698368A true CN106698368A (en) | 2017-05-24 |
Family
ID=58932490
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510789424.5A Pending CN106698368A (en) | 2015-11-16 | 2015-11-16 | Nitric oxide wet oxidation process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106698368A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108545710A (en) * | 2018-04-27 | 2018-09-18 | 胡自然 | A kind of industrial nitric acid preparation method |
| CN109795994A (en) * | 2019-03-22 | 2019-05-24 | 宁夏润夏能源化工有限公司 | A kind of technique that dust technology adds dehydrating agent to produce concentrated nitric acid |
-
2015
- 2015-11-16 CN CN201510789424.5A patent/CN106698368A/en active Pending
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108545710A (en) * | 2018-04-27 | 2018-09-18 | 胡自然 | A kind of industrial nitric acid preparation method |
| CN108545710B (en) * | 2018-04-27 | 2020-10-23 | 安徽汇川管理咨询有限公司 | Preparation method of industrial nitric acid |
| CN109795994A (en) * | 2019-03-22 | 2019-05-24 | 宁夏润夏能源化工有限公司 | A kind of technique that dust technology adds dehydrating agent to produce concentrated nitric acid |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102210964B (en) | Gas phase silicon dioxide tail gas treatment process and system | |
| CN103910333B (en) | A kind of hydrofluoric method in recovery hydrofluorination process tail gas | |
| CN104258690B (en) | The method that hydrochloric acid tail gas absorption produces byproduct hydrochloric acid in production processes of chloroacetic acid | |
| CN102872695A (en) | Method for sintering and desulfurizing enriched smoke to prepare sulfuric acid | |
| CN101112977B (en) | Nitric oxide wet process oxidation technology | |
| CA3113375A1 (en) | Nitrogen oxide absorption slurry and its preparation and use method thereof | |
| CN110683519A (en) | Method and device for treating lithium hexafluorophosphate synthesis tail gas | |
| CN106698368A (en) | Nitric oxide wet oxidation process | |
| CN105236451B (en) | Method and apparatus for continuous conversion production of sodium nitrate | |
| CN111115587A (en) | Method and system for preparing analytically pure sulfuric acid from smelting flue gas | |
| CN202146695U (en) | Gas-phase silicon dioxide tail gas treatment system | |
| CN105668590B (en) | The absorption process of unreacted ammonia in acrylonitrile reactor device | |
| CN110124510A (en) | A method of utilizing oxygen-enriched side-blowing smelting lead extracting sulfuric acid | |
| CN107626195A (en) | The tail gas treatment process of red phosphorus purification | |
| CN209740714U (en) | Device for preparing nitric acid by efficiently oxidizing and absorbing nitrogen oxides | |
| CN103011102B (en) | Cooling process for desalted water conveyed to nitric acid absorbing tower | |
| CN205109370U (en) | Kiln is volatilized including sulphur tail gas desulfurization device to gyration | |
| CN101428773A (en) | Purifying method for nitric oxide gas with 3N purity | |
| CN109232171B (en) | Method for completely removing acidic substances in crude vinyl chloride gas | |
| CN107867676A (en) | Nitric oxide wet process oxidation technology | |
| CN104671221A (en) | Method and device for preparing sulphuric acid by taking discharged sulfur dioxide as raw material | |
| CN113509811B (en) | Method and system for treating tail gas containing chloropropene and oxygen | |
| CN110170222B (en) | Treatment method and system for tungsten smelting waste gas | |
| CN103121664B (en) | Production technique of high-purity hydrofluoric acid | |
| CN201906547U (en) | Diluted ammonia water concentrating absorption tower |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20170524 |
|
| WD01 | Invention patent application deemed withdrawn after publication |