CN103663395B - A kind of method reducing oxynitride and prepare Sodium Nitrite energy consumption - Google Patents
A kind of method reducing oxynitride and prepare Sodium Nitrite energy consumption Download PDFInfo
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Abstract
The present invention relates to a kind of method reducing oxynitride and prepare Sodium Nitrite energy consumption, it comprises the steps: (1) 30 ~ 40 DEG C prepare the soda ash solution that mass percent concentration is 10% ~ 30% once joining in alkali still; (2), after being collected by the oxynitride produced in factory, tail gas absorber is introduced; (3) soda ash solution that (1) step prepares is invested in Alkali absorption tower, the tail gas after tail gas absorber process in (2) step is introduced the reaction of Alkali absorption tower, generate Sodium Nitrite; (4) when the reaction of Alkali absorption tower is 5 ~ 8 to solution ph, the sodium nitrite solution of generation is delivered to secondary again and joins in alkali still, be mixed with the secondary soda ash solution containing Sodium Nitrite.The invention has the beneficial effects as follows: to greatly reduce in traditional method evaporation of water amount, greatly reduce the steam consumption producing Sodium Nitrite, do not need newly to drop into any cost, and on Sodium Nitrite quality without impact; Security is high, easy to operate, very easily promotes.
Description
[technical field]
The present invention relates to technical field of fine, be specially a kind of method reducing oxynitride and prepare Sodium Nitrite energy consumption.
[background technology]
Sodium Nitrite is important inorganic chemical product, has been widely used in industries such as dyestuff, medicine, metallurgy, glass and food-processings.In recent years, along with the continuous increase of domestic and international market demand, the development of Sodium Nitrite product is very fast, especially under the form gone up steadily at a lot of price of chemical products in recent years, the price of Sodium Nitrite product is also relatively stable, export volume constantly increases, for enterprise brings considerable economic benefit.And due to features such as the investment of its production equipment is not too large, the construction period is short, instant effects, thus much originally had the factory of this product constantly to expand production capacity and using the pillar product of Sodium Nitrite as enterprise.
Industrial, the preparation of Sodium Nitrite is more, but at present domestic prepare Sodium Nitrite with the most widely method for " direct method ", namely utilize soda ash solution, with nitrogen-containing oxide (NO, NO
2) tail gas in absorption tower, carry out contact reacts, generate Sodium Nitrite and SODIUMNITRATE, then through pervaporation, crystallization, separation, obtain required Sodium Nitrite product.
Reaction principle is:
2NO
2+Na
2CO
3==HNO
2+NaNO
3+CO
2
NO
2+NO+Na
2CO
3==2NaNO
2+CO
2
The maximum shortcoming of this method is power consumption, namely in evaporative process, consumes a large amount of steam, and energy dissipation is very big, adds the cost of product, and be both unfavorable for producing, its a large amount of condensed water elimination also easily pollutes.
High about the energy consumption why preparing Sodium Nitrite, steam consumption is large, mainly contains two reasons:
One, due to soda ash (Na own
2cO
3) solubleness lower (see the solubility table of following sodium carbonate in water) in water, the concentration of lye of preparation is not high, and the Sodium Nitrite concentration thus generated is lower, need evaporate large quantity of moisture time concentrated, and consumption quantity of steam is large.
The solubility table of sodium carbonate in water
From in upper table, can be clearly seen that: 35 DEG C time, soda ash has maxima solubility, its maximum saturation concentration is 33%, in industry generates, generally all can not join alkali to the highest saturation concentration, because, if temperature slightly changes and is just easy to crystallization of solution and causes equipment or line clogging, and produces industrial accident;
Two, because soda ash is at initial reaction stage and oxynitride (NO, NO
2) reaction time, except part producing Sodium Nitrite, also generate sodium bicarbonate in a large number:
2H
++Na
2CO
3→2NaHCO
3
And the saturation concentration of sodium bicarbonate is when normal temperature (25 DEG C), only have 9.4%(see the solubility table of following sodium bicarbonate in water), more much lower than 23% of soda ash.Therefore, in actual industrial production, a large amount of sodium bicarbonate crystal occluding device or pipeline is produced in order to prevent initial reaction stage, the soda ash solution concentration of preparation is generally about 15%, maximum saturation concentration more than soda ash is low, the Sodium Nitrite concentration more causing generation is low, needs to evaporate a large amount of moisture.
The solubility table of sodium bicarbonate in water
In order to solve steam consumption in Sodium Nitrite production process, a lot of data provides some ways.The technique that a kind of direct crystallization method provided as the patent publication No. application for a patent for invention that is CN101337662A produces Sodium Nitrite is the soda ash solution of compounding high concentration (being wherein expressed as the concentration of 51Be), directly Sodium Nitrite crystal is generated with after reaction of nitrogen oxides, its centrifuge mother liquor continues to join soda ash solution and reaction of nitrogen oxides, so repeatedly.But this method exists larger drawback, first, when suitability for industrialized production, the soda ash solution of high density very solution Yin Wendu, moisture volatilization and there is crystal settling, blocking pipeline or equipment; Secondly, at the initial stage of soda ash and reaction of nitrogen oxides, temporarily can there is the generation of a large amount of sodium bicarbonates, the solubleness of sodium bicarbonate in water lower (see the solubility table of sodium bicarbonate in water), the sodium carbonate solution of high density more easily temporarily brings a large amount of sodium bicarbonate precipitations, cause the blocking of equipment and pipeline, and then likely cause industrial accident; Its three because the solubleness of Sodium Nitrite very high (see the solubility table of following Sodium Nitrite in water), be not difficult to by concentrated with direct crystallization in actual production.Therefore, in the industrial production, oxynitride is utilized to produce Sodium Nitrite, the compound concentration general all lower (great majority are about 15%) of soda ash.Therefore, the method that provides for CN101337662A application for a patent for invention of patent publication No. is not too applicable for suitability for industrialized production.
The solubility table of Sodium Nitrite in water
[summary of the invention]
The object of the invention is the deficiency existed for the above prior art, in water, there is high resolution according to Sodium Nitrite, and soda ash solvability this feature poor, actual in conjunction with production, a kind of method reducing oxynitride and prepare Sodium Nitrite energy consumption is provided.
For achieving the above object, technical scheme of the present invention is: a kind of method reducing oxynitride and prepare Sodium Nitrite energy consumption, it comprises the steps:
(1) under 30 ~ 40 DEG C of conditions, the soda ash solution that mass percent concentration is 10% ~ 30% is prepared once joining in alkali still
(2), after being collected by the oxynitride produced in factory, introduce tail gas absorber and process, tail gas absorber is that medium absorbs oxynitride with water, removes most of NO
2, remaining NO, NO
2introduce Alkali absorption tower, tail gas absorber is traditionally arranged to be 2 ~ 4 grades;
(3) soda ash solution that (1) step prepares is invested in Alkali absorption tower, the tail gas after tail gas absorber process in (2) step is introduced the reaction of Alkali absorption tower, generate Sodium Nitrite;
(4) when the reaction of Alkali absorption tower is 5 ~ 8 to solution ph, reaction reaches terminal, the sodium nitrite solution of generation being delivered to secondary joins in alkali still, be warming up to 30 ~ 40 DEG C, under agitation add anhydrous sodium carbonate or the sodium bicarbonate of sodium nitrite solution weight 5-15%, be mixed with the secondary soda ash solution containing Sodium Nitrite;
(5) secondary soda ash solution is reentered in Alkali absorption tower, continues the tail gas introduced in (2) step after tail gas absorber process and react, generate Sodium Nitrite;
(6) when the reaction of Alkali absorption tower is 5 ~ 8 to solution ph, reaction reaches terminal, the sodium nitrite solution of generation is delivered to again and joins for three times in alkali still, be warming up to 30 ~ 40 DEG C, add anhydrous sodium carbonate or the sodium bicarbonate of described sodium nitrite solution weight 5-15% under stirring, be mixed with three soda ash solutions containing Sodium Nitrite;
(7) three soda ash solutions are reentered in Alkali absorption tower, continue to introduce tail gas (NO, the NO in (2) step after tail gas absorber process
2) react, generate Sodium Nitrite;
(8) above (4) step and (5) step is repeated, until when sodium nitrite solution mass percent concentration reaches 40% ~ 50%, sodium nitrite solution is delivered in concentration kettle, evaporates remaining moisture content, decrease temperature crystalline, obtains the Sodium Nitrite product of more than 98%.
By aforesaid method, utilize the Sodium Nitrite absorption liquid that reaction generates, repeatedly prepare NO, NO in soda ash solution and tail gas
2reaction, progressively improves the concentration of Sodium Nitrite absorption liquid, to greatly reduce in traditional method evaporation of water amount, greatly reduces the steam consumption producing Sodium Nitrite.Be proven, according to the Sodium Nitrite absorption liquid that method of the present invention is obtained, concentration can reach 40% ~ 50%, and during evaporative crystallization, the water yield of required evaporation greatly reduces, and compared with traditional " direct method ", steam consumption reduces by 30% ~ 60%; Do not need newly to drop into any cost, and on Sodium Nitrite quality without impact; Security is high, easy to operate, very easily promotes.
Described soda ash solution can use Na
2cO
3, NaHCO
3, NaHO one or more configure, preferred Na
2cO
3, the best in quality percentage concentration of soda ash solution is 10% ~ 20%, and joining alkali temperature is 30 DEG C ~ 100 DEG C, and it is 30 DEG C ~ 40 DEG C that the best joins alkali temperature.
The oxynitride produced in factory is behind water absorption tower, and the remaining tail gas overwhelming majority is NO and NO
2, then react through Alkali absorption tower and soda ash and generate Sodium Nitrite.It answers terminal control to be preferably 6 ~ 7 built in pH, and wherein optimum response terminal point control is at pH=6.
Repeatedly join in alkali above-mentioned, utilizing sodium nitrite solution as joining alkali lye, after being warming up to 30 ~ 40 DEG C, rejoining soda ash, be mixed with new soda ash solution.Repeatedly join alkali and be generally less than 10 times, the best is 5 times.The raw material of joining alkali can be Na
2cO
3, NaHCO
3, NaHO a kind of or wherein two kinds or three kinds arbitrary combination, the best selects Na
2cO
3, it is 10% ~ 30% that alkali lye mass percent concentration is joined by institute, and optimum concn is 10% ~ 20%, and joining alkali temperature is 30 DEG C ~ 100 DEG C, and optimum temps is 30 DEG C ~ 40 DEG C.
The sodium nitrite solution that the present invention utilizes reaction to generate, as absorption liquid, prepares NO, the NO in soda ash solution and tail gas repeatedly
2reaction, progressively improves the concentration of Sodium Nitrite absorption liquid, to greatly reduce in traditional method evaporation of water amount, greatly reduces the steam consumption producing Sodium Nitrite.Be proven, according to the Sodium Nitrite absorption liquid that method of the present invention is obtained, concentration can reach 40% ~ 50%, and during evaporative crystallization, the water yield of required evaporation greatly reduces, and compared with traditional " direct method ", steam consumption reduces by 30% ~ 60%; Do not need newly to drop into any cost, and on Sodium Nitrite quality without impact; Security is high, easy to operate, very easily promotes.
Compared with preparing Sodium Nitrite with traditional " direct method ", feature of the present invention is: utilize Sodium Nitrite solubleness in water large and characteristic contrast that soda ash solubleness in water is little, the sodium nitrite solution generated with reaction, as absorption liquid, prepares NO, the NO in soda ash solution and tail gas repeatedly
2reaction, progressively improve the concentration of Sodium Nitrite absorption liquid, greatly reduce in traditional method evaporation of water amount, greatly reduce the steam consumption producing Sodium Nitrite, be proven, according to the Sodium Nitrite absorption liquid that method of the present invention is obtained, concentration can reach 40% ~ 50%, during evaporative crystallization, the water yield of required evaporation greatly reduces, and compared with traditional " direct method ", steam consumption reduces by 30% ~ 60%; Do not need newly to drop into any cost, and on Sodium Nitrite quality without impact; Security is high, easy to operate, very easily promotes.
In addition, the present invention also has following features:
(1) do not need newly to drop into any cost, and on Sodium Nitrite quality without impact;
(2) security is high, easy to operate, very easily promotes.
[accompanying drawing explanation]
Fig. 1 is a kind of system schematic reducing oxynitride and prepare the method for Sodium Nitrite energy consumption of the present invention.
[embodiment]
The invention will be further elaborated by the following examples, but be not limited to the technical scheme of the present invention's record.
Embodiment 1
Reduce the method that oxynitride prepares Sodium Nitrite energy consumption, it comprises the steps:
(1) under 30 ~ 40 DEG C of conditions, the soda ash solution that mass percent concentration is 10% ~ 25% is prepared once joining in alkali still, (once joining alkali), for subsequent use;
(2), after being collected by the oxynitride produced in factory, introduce tail gas absorber and process, tail gas absorber, to be that medium absorbs oxynitride with water, removes most of NO
2, remaining NO, NO
2introduce Alkali absorption tower, tail gas absorber is traditionally arranged to be 2 ~ 4 grades;
(3) be invested in Alkali absorption tower by the soda ash solution that (1) step prepares, the tail gas after tail gas absorber process in (2) step is introduced the reaction of Alkali absorption tower, generate Sodium Nitrite, chemical equation is as follows:
NO
2+NO+Na
2CO
3==2NaNO
2+CO
2
(4) when the reaction of Alkali absorption tower is 6 ~ 7 to solution ph, reaction reaches terminal, the sodium nitrite solution of generation being delivered to again secondary joins in alkali still, be warming up to 30 ~ 40 DEG C, under agitation add anhydrous sodium carbonate or the sodium bicarbonate of sodium nitrite solution weight 10%, be mixed with the secondary soda ash solution containing Sodium Nitrite;
(5) secondary soda ash solution is reentered in Alkali absorption tower, continues to introduce tail gas (NO, the NO in (2) step after tail gas absorber process
2) react, generate Sodium Nitrite;
(6) when the reaction of Alkali absorption tower is 6 ~ 7 to solution ph, reaction reaches terminal, the sodium nitrite solution of generation is delivered to again and joins for three times in alkali still, be warming up to 30 ~ 40 DEG C, add anhydrous sodium carbonate or the sodium bicarbonate of described sodium nitrite solution weight 10% under stirring, be mixed with three soda ash solutions containing Sodium Nitrite;
(7) three soda ash solutions are reentered in Alkali absorption tower, continue to introduce tail gas (NO, the NO in (2) step after tail gas absorber process
2) react, generate Sodium Nitrite;
(8) above (4) step and (5) step is repeated, until when sodium nitrite solution mass percent concentration reaches 40% ~ 50%, sodium nitrite solution is delivered in concentration kettle, evaporates remaining moisture content, decrease temperature crystalline, obtains the Sodium Nitrite product of more than 98%.
As shown in Figure 1, the oxynitride produced in factory inputs tail gas absorber after collecting, and described tail gas absorber arranges minimum two groups, wherein, comprises multiple water cycle and absorb sub-tower in described tail gas absorber, all can be made up of stainless steel or polypropylene PP material; And diameter 600-4500mm is not etc., height is at 8-15m.PP corrugated plate packing is equipped with on the tower body top of described tail gas absorber, and below tower body, column foot is used for splendid attire circulation feed liquid, and the offgas outlet of previous stage top of tower is connected with the column foot gas feed of rear stage tower.Every first stage tower all configures a corrosion protection pump, for water or alkali lye being delivered to tower top by column foot when tail gas absorption, the feed liquid of such circulation conveying constantly absorbs nitrogen protoxide in tail gas or nitrogen dioxide gas, to make the final qualified discharge of the tail gas containing oxynitride.Described tail gas absorber is connected with Alkali absorption tower, described Alkali absorption tower classification is arranged, the tower top discharge port of described first step Alkali absorption tower is connected with feeding mouth at the bottom of the tower of second stage Alkali absorption tower, and described first step Alkali absorption tower with once join alkali still and be connected, described second stage Alkali absorption tower is joined alkali still with secondary and is connected, by that analogy.Last step Alkali absorption tower is connected with vaporizer, for described sodium nitrite solution input vaporizer is carried out evaporation process.
Embodiment 2
1, under 30 ~ 40 DEG C of conditions, once join in alkali still what be equipped with 1000L water, under stirring, add 150kg anhydrous sodium carbonate (i.e. soda ash), the soda ash solution (once joining alkali) of preparation about 13%, for subsequent use;
2, the soda ash solution prepared is put into two-stage Alkali absorption tower, introduce the tail gas after tail gas absorber process, at normal temperatures (25 DEG C) reaction;
3, when to react to solution ph be 6 ~ 7, reaction reaches terminal, is delivered in concentration kettle, evaporates remaining moisture content, decrease temperature crystalline by the sodium nitrite solution of generation, centrifugal obtain 155kg, more than 98% Sodium Nitrite product.
Through statistics, ton steam that Sodium Nitrite consumes about 6.0 tons.
Embodiment 3
1, under 30 ~ 40 DEG C of conditions, once join in alkali still what be equipped with 2000L water, under stirring, add 300kg anhydrous sodium carbonate (i.e. soda ash), the soda ash solution (once joining alkali) of preparation about 13%, for subsequent use;
2, the soda ash solution prepared is put into two-stage Alkali absorption tower, introduce the tail gas after tail gas absorber process, at normal temperatures (25 DEG C) reaction;
3, when to react to solution ph be 6 ~ 7, reaction reaches terminal, the sodium nitrite solution of generation is delivered to secondary again and joins in alkali still, be warming up to 30 ~ 40 DEG C, add 300kg anhydrous sodium carbonate (i.e. soda ash) under stirring, be mixed with the secondary soda ash solution containing Sodium Nitrite;
4, be reentered in Alkali absorption tower by secondary soda ash solution, continue to introduce the tail gas after tail gas absorber process, (25 DEG C) reaction, generates Sodium Nitrite at normal temperatures;
5, when to react to solution ph be 6 ~ 7, reaction reaches terminal, is delivered in concentration kettle, evaporates remaining moisture content, decrease temperature crystalline by the sodium nitrite solution of generation, centrifugal obtain 650kg, more than 98% Sodium Nitrite product.
Through statistics, ton steam that Sodium Nitrite consumes about 4.0 tons, reduces steam consumption about 33%.
Embodiment 4
1, under 30 ~ 40 DEG C of conditions, once join in alkali still what be equipped with 2000L water, under stirring, add 300kg anhydrous sodium carbonate (i.e. soda ash), the soda ash solution (once joining alkali) of preparation about 13%, for subsequent use;
2, the soda ash solution prepared is put into two-stage Alkali absorption tower, with the tail gas of introducing after tail gas absorber process, (25 DEG C) reaction at normal temperatures;
3, when to react to solution ph be 6 ~ 7, reaction reaches terminal, the sodium nitrite solution of generation is delivered to secondary again and joins in alkali still, be warming up to 30 ~ 40 DEG C, add 300kg anhydrous sodium carbonate (i.e. soda ash) under stirring, be mixed with the secondary soda ash solution containing Sodium Nitrite;
4, be reentered in Alkali absorption tower by secondary soda ash solution, continue to introduce the tail gas after tail gas absorber process, (25 DEG C) reaction, generates Sodium Nitrite at normal temperatures;
5, when to react to solution ph be 6 ~ 7, reaction reaches terminal, the sodium nitrite solution of generation is delivered to three times again and joins in alkali still, be warming up to 30 ~ 40 DEG C, add 300kg anhydrous sodium carbonate (i.e. soda ash) under stirring, be mixed with three soda ash solutions containing Sodium Nitrite;
6, three soda ash solutions are reentered in Alkali absorption tower, continue to introduce the tail gas after tail gas absorber process, at normal temperatures (25 DEG C) reaction, generate Sodium Nitrite;
7, when to react to solution ph be 6 ~ 7, reaction reaches terminal, is delivered in concentration kettle, evaporates remaining moisture content, decrease temperature crystalline by the sodium nitrite solution of generation, centrifugal obtain 950kg, more than 98% Sodium Nitrite product.
Through statistics, ton steam that Sodium Nitrite consumes about 3.2 tons, reduces steam consumption about 46.7%.
Embodiment 5
1, under 30 ~ 40 DEG C of conditions, once join in alkali still what be equipped with 2000L water, under stirring, add 300kg anhydrous sodium carbonate (i.e. soda ash), the soda ash solution (once joining alkali) of preparation about 13%, for subsequent use;
2, the soda ash solution prepared is put into two-stage Alkali absorption tower, introduce the tail gas after tail gas absorber process, at normal temperatures (25 DEG C) reaction;
3, when to react to solution ph be 6 ~ 7, reaction reaches terminal, the sodium nitrite solution of generation is delivered to secondary again and joins in alkali still, be warming up to 30 ~ 40 DEG C, add 300kg anhydrous sodium carbonate (i.e. soda ash) under stirring, be mixed with the secondary soda ash solution containing Sodium Nitrite;
4, be reentered in Alkali absorption tower by secondary soda ash solution, continue to introduce the tail gas after tail gas absorber process, (25 DEG C) reaction, generates Sodium Nitrite at normal temperatures;
5, when to react to solution ph be 6 ~ 7, reaction reaches terminal, the sodium nitrite solution of generation is delivered to three times again and joins in alkali still, be warming up to 30 ~ 40 DEG C, add 300kg anhydrous sodium carbonate (i.e. soda ash) under stirring, be mixed with three soda ash solutions containing Sodium Nitrite;
6, be reentered in Alkali absorption tower by three soda ash solutions, continue to introduce the tail gas after tail gas absorber process, (25 DEG C) reaction, generates Sodium Nitrite at normal temperatures;
7, when to react to solution ph be 6 ~ 7, reaction reaches terminal, the sodium nitrite solution of generation is delivered to four times and joins in alkali still, be warming up to 30 ~ 40 DEG C, add 300kg anhydrous sodium carbonate (i.e. soda ash) under stirring, be mixed with four soda ash solutions containing Sodium Nitrite;
8, be reentered in Alkali absorption tower by four soda ash solutions, continue to introduce the tail gas after tail gas absorber process, (25 DEG C) reaction, generates Sodium Nitrite at normal temperatures;
9, when to react to solution ph be 6 ~ 7, reaction reaches terminal, the sodium nitrite solution of generation is delivered to five times and joins in alkali still, be warming up to 30 ~ 40 DEG C, add 300kg anhydrous sodium carbonate (i.e. soda ash) under stirring, be mixed with five soda ash solutions containing Sodium Nitrite;
10, be reentered in Alkali absorption tower by five soda ash solutions, continue to introduce the tail gas after tail gas absorber process, (25 DEG C) reaction, generates Sodium Nitrite at normal temperatures;
11, when to react to solution ph be 6 ~ 7, reaction reaches terminal, is delivered in concentration kettle, evaporates remaining moisture content, decrease temperature crystalline by the sodium nitrite solution of generation, centrifugal obtain 1600kg, more than 98% Sodium Nitrite product.
Through statistics, ton steam that Sodium Nitrite consumes about 2.4 tons, reduces steam consumption about 60%.
Embodiment 6
1, under 30 ~ 40 DEG C of conditions, once join in alkali still what be equipped with 2000L water, under stirring, add 500kg anhydrous sodium carbonate (i.e. soda ash), the soda ash solution (once joining alkali) of preparation about 13%, for subsequent use;
2, the soda ash solution prepared is put into two-stage Alkali absorption tower, introduce the tail gas after tail gas absorber process, at normal temperatures (25 DEG C) reaction;
3, when to react to solution ph be 6 ~ 7, reaction reaches terminal, the sodium nitrite solution of generation is delivered to secondary again and joins in alkali still, be warming up to 30 ~ 40 DEG C, add 500kg anhydrous sodium carbonate (i.e. soda ash) under stirring, be mixed with the secondary soda ash solution containing Sodium Nitrite;
4, be reentered in Alkali absorption tower by secondary soda ash solution, continue to introduce the tail gas after tail gas absorber process, (25 DEG C) reaction, generates Sodium Nitrite at normal temperatures;
5, when to react to solution ph be 6 ~ 7, reaction reaches terminal, the sodium nitrite solution of generation is delivered to three times again and joins in alkali still, be warming up to 30 ~ 40 DEG C, add 500kg anhydrous sodium carbonate (i.e. soda ash) under stirring, be mixed with three soda ash solutions containing Sodium Nitrite;
6, be reentered in Alkali absorption tower by three soda ash solutions, continue to introduce the tail gas after tail gas absorber process, (25 DEG C) reaction, generates Sodium Nitrite at normal temperatures;
7, when to react to solution ph be 6 ~ 7, reaction reaches terminal, is delivered in concentration kettle, evaporates remaining moisture content, decrease temperature crystalline by the sodium nitrite solution of generation, centrifugal obtain 1600kg, more than 98% Sodium Nitrite product.
Through statistics, ton steam that Sodium Nitrite consumes about 3.0 tons, reduces steam consumption about 50%.
More than show and describe ultimate principle of the present invention and principal character and advantage of the present invention; a described example wish is as the single example of illustrating all respects of the present invention; without departing from the spirit and scope of the present invention; also comprise the various changes and modifications of functional equivalent in the scope of the invention, these changes and improvements all fall within the claimed scope of the invention.
Claims (3)
1. reduce the method that oxynitride prepares Sodium Nitrite energy consumption, it is characterized in that, step comprises:
(1) under 30 ~ 40 DEG C of conditions, the soda ash solution that mass percent concentration is 10% ~ 30% is prepared once joining in alkali still;
(2), after being collected by the oxynitride produced in factory, tail gas absorber is introduced;
(3) soda ash solution that (1) step prepares is invested in Alkali absorption tower, the tail gas after tail gas absorber process in (2) step is introduced the reaction of Alkali absorption tower, generate Sodium Nitrite;
(4) when the reaction of Alkali absorption tower is 5 ~ 8 to solution ph, reaction reaches terminal, the sodium nitrite solution of generation being delivered to again secondary joins in alkali still, be warming up to 30 ~ 40 DEG C, under agitation add anhydrous sodium carbonate or the sodium bicarbonate of sodium nitrite solution weight 5-15%, be mixed with the secondary soda ash solution containing Sodium Nitrite;
(5) secondary soda ash solution is reentered in Alkali absorption tower, continues the tail gas introduced in (2) step after tail gas absorber process and react, generate Sodium Nitrite;
(6) when the reaction of Alkali absorption tower is 5 ~ 8 to solution ph, reaction reaches terminal, the sodium nitrite solution of generation is delivered to again and joins for three times in alkali still, be warming up to 30 ~ 40 DEG C, add anhydrous sodium carbonate or the sodium bicarbonate of described sodium nitrite solution weight 5-15% under stirring, be mixed with three soda ash solutions containing Sodium Nitrite;
(8) above (4) step and (5) step is repeated, until when sodium nitrite solution mass percent concentration reaches 40% ~ 50%.
2. according to a kind of method reducing oxynitride and prepare Sodium Nitrite energy consumption according to claim 1, it is characterized in that, control of reaction end point is 6 ~ 7 at pH.
3. according to a kind of method reducing oxynitride and prepare Sodium Nitrite energy consumption according to claim 2, it is characterized in that, control of reaction end point is 6 at pH.
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| CN101095998A (en) * | 2006-06-26 | 2008-01-02 | 山东金城医药化工有限公司 | Recovery utilization method of furfuran amine salt waste gases |
| CN101648104A (en) * | 2008-08-13 | 2010-02-17 | 北京格瑞华阳科技发展有限公司 | Technology for reclaiming hydrogen chloride tail gas in chemical production |
| CN101565191A (en) * | 2009-06-01 | 2009-10-28 | 湖南永清环保股份有限公司 | Method for preparing anhydrous sodium sulfite by circularly absorbing sulfur dioxide in exhaust gas |
| CN103212280A (en) * | 2012-08-14 | 2013-07-24 | 襄阳泽东化工有限公司 | Heat recovery system for high temperature flue gas at ammoxidation section |
| CN103111178A (en) * | 2013-02-27 | 2013-05-22 | 东华大学 | Absorption system and method for catalytic oxidation of tail gas NOx |
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