CN1061389A - The recovery and treatment method of ammonia during bicarbonate of ammonia is produced - Google Patents
The recovery and treatment method of ammonia during bicarbonate of ammonia is produced Download PDFInfo
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- CN1061389A CN1061389A CN 90106175 CN90106175A CN1061389A CN 1061389 A CN1061389 A CN 1061389A CN 90106175 CN90106175 CN 90106175 CN 90106175 A CN90106175 A CN 90106175A CN 1061389 A CN1061389 A CN 1061389A
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Abstract
The present invention is the recovery and treatment method of ammonia in a kind of bicarbonate of ammonia production process.To containing ammonia gas earlier with washing with quantitative soft water again after the weak ammonia washing.When washing with weak ammonia, by taking to keep the measure of part weak ammonia pump around circuit, ammonia in the gas was fully reclaimed, significantly reduced total bath water amount again, solve in the present bicarbonate of ammonia production the problem of environmental pollution that discharging caused because of various forms ammonia.
Description
What the present invention relates to is to containing the recovery and treatment method of ammonia in the ammonia gas in the bicarbonate of ammonia production process.
In the bicarbonate of ammonia production process, there are the tail gas of many places or discharging all to contain ammonia in the gas, for cutting the waste and to the pollution of air, water is as these ammonia in the absorption agent washing and recycling gas usually.Therefore in whole process of production, produce a large amount of weak ammonias because of the gas scrubbing meeting.For solving the pollution that produces once more and the recovery of ammonia, Chinese patent 85102791A and 86104483A have introduced the method for utilizing distillation or fractionation to reclaim ammonia in the weak ammonia.Its weak point need to be distillation plant and to consume heat energy." chemical industry environmental protection " 1986 the 6th volumes have been introduced another kind of method with " chemical industry environmental protection management and information " respectively on the 2nd phase of nineteen ninety, adopted a bit to add soft water, absorbed with the segmentation of different concns weak ammonia and differently contain ammonia gas and set up with limestone kiln kiln gas carbonization to make full use of the measure of weak ammonia.In this method, because the required soft water of entire treatment system all is from the exigent carbonization washing tail gas of ammonia wash degree is added, other nitrogenous gas is everywhere then only washed with the weak ammonia of different concns, therefore the ammonia in these gases can not absorb fully, finally still will enter atmosphere with discharging gas.Can realize " water balance " although it is so, but the ammonia in the gas do not reclaimed fully, thereby still had the pollution of ammonia air.On the other hand, in this method, because the used water yield of carbonization washing tail gas has been determined weak ammonia total amount in the whole gas scrubbing system, limestone kiln kiln gas carbonization realizes in " water balance " it then being an indispensable important ring making these weak ammonias be able to " digestion ".But can have utilizable limestone kiln kiln gas limited by objective condition.When the kiln gas of no utilizable limestone kiln, weak ammonia is inevitable superfluous, and problem of environmental pollution also will produce thereupon.
The production process that anatomizes weak ammonia is not difficult to find, be present in as volatile components the mass transfer process of between gas-liquid two-phase, carrying out when ammonia in the gas is washed except that the mass transfer direction on the contrary, its essence is identical with distillation or fractionation.In distillation, especially in fractionation and rectifying, improve and guarantee that the important measures of mass-transfer efficiency are the control reflux ratios, by the circulation of suitable phegma, volatile components all is in or between the partial gas-liquid two-phase of each mass transfer near equilibrium state.And at present in the gas washing absorption process of ammonia do not possess this condition, in fact only through once contact, the partial ammonia of each mass transfer all fails to reach equilibrium state between gas-liquid, mass-transfer efficiency is low, thereby produces the weak ammonia of a large amount of " thin ".Present various ammonia recovery methods are owing to be just to deal with after this weak ammonia produces in a large number all, thereby are difficult to deal with problems at all.
According to above-mentioned analysis, the present invention's purpose at first provides a kind of by improving the method that mass-transfer efficiency fully reclaims the ammonia in the bicarbonate of ammonia production process.Further object of the present invention provides and a kind ofly ammonia in the bicarbonate of ammonia production is fully reclaimed and solves the method for environmental pollution.
Method of the present invention has adopted containing ammonia gas earlier with the weak ammonia washing, and then the processing mode of washing with quantitative soft water.When washing with weak ammonia, make the part weak ammonia constantly carry out pump around circuit, rest part takes out and to use it for anything else in addition, constantly replenishes with the weak ammonia of the lower concentration weak ammonia of soft water washing process (for example from) simultaneously, to keep the stable flow that loops back.The weak ammonia that is removed can be used for the gas that carrying out washing treatment has higher ammonia quantity, or sends to preparation and produce required strong aqua.The pump around circuit of weak ammonia can realize by recycle pump.Owing in the weak ammonia washing process, set up the pump around circuit system, make between gas-liquid and can repeated multiple times contact, ammonia wherein just can be in gradually or near equilibrium state, realize best mass transfer effect.Under the situation of conditions permit, increase loops back flow and will help to realize balance, improves the assimilated efficiency of ammonia.The important evidence that detects assimilation effect and Control Circulation quantity of reflux in the washing process is the equilibrium of ammonia under the actually operating condition, temperature when though it will be operated, the influence that the conditions such as original concentration of pressure and ammonia change, but under certain operational condition, by calculating and/or surveying and be not difficult to obtain these data.
Mode difference when making the weak ammonia pump around circuit, effect are also different.A kind of is to make weak ammonia carry out the reflux type of globality systemic circulation in washing process, another kind is according to must change from high to low of ammonia content before and after the gas processing washing process to be divided into some concentration gradient sections, sets up round-robin locality reflux type in each section respectively.The latter's effect will obviously be better than the former.When adopting the latter's mode, can enter its next adjacent high density section successively by the weak ammonia that takes out in each section and use as keeping the additional liquid that loops back flow in this section.Therefore, the concentration gradient section being divided thin, reduce every adjacent two intersegmental concentration differences as far as possible, is favourable to the realization and the maintenance of ammonia absorption equilibrium in the washing process.
The weak ammonia that makes washing absorb usefulness has suitable degree of carbonisation, especially makes the weak ammonia in the maximum concentration section have high slightly degree of carbonisation when adopting segmentation pump around circuit mode, is to improve the ammonia assimilation effect and alleviate effective measure of each step washing load thereafter.But for avoiding bringing too much carbonic acid gas in the gas after washing, degree of carbonisation is to be no more than 70% for well.The short-cut method that makes weak ammonia have degree of carbonisation is the carbonization mother liquor that adds in weak ammonia as required behind an amount of filtering bicarbonate of ammonia product.
Reduce temperature and can increase the solubleness of ammonia in water, simultaneously because its dissolving itself also is an exothermic process, so to reduce wash temperature as far as possible during conditions permit be favourable.Consider the comprehensive utilization of the energy and cold in the production system, temperature can be controlled in the subambient scope at least.
Aforesaid method of the present invention except that can in production system, contain everywhere use respectively when ammonia gas is handled, also can be used for relatively focused on after ammonia gas and/or weak ammonia everywhere gather respectively dissimilar containing.Which kind of mode no matter, because ammonia can keep or all the time near best mass transfer conditions in the carrying out washing treatment process, so the ammonia in the gas can fully be reclaimed, and reduced the washing water yield simultaneously again to greatest extent.Both made and do not adopted limestone kiln kiln gas carbonization also can realize not having superfluous weak ammonia generation and discharging, problem of environmental pollution solves substantially.
Be that example further describes method of the present invention with the process of in the plate type washing absorption tower, handling carbonization tail gas below.But the scope of the inventive method is not limited in following example.
The middle and lower part of tower is the weak ammonia washing section, and top is the soft water washing section.Ammonia content is 30.95 gram/rice
3Carbonization tail gas at the bottom of tower, enter, soft water quantitatively adds from cat head by producing 0.25 ton of/ton required carbon ammonium of bicarbonate of ammonia.Every 2-3 piece column plate interval is a concentration gradient section in the weak ammonia washing section, and the weak ammonia in each section is kept 15-20 rice by recycle pump respectively under the prerequisite that liquid flooding does not take place
3The pump around circuit of/hour internal circulating load, except that keeping the part that loops back flow, the weak ammonia of rest part enters next adjacent high density section use successively in each section.The ammonia content of the weak ammonia in the tower bottom maximum concentration section is the 60-100 titre, wherein suitably adds carbonization mother liquor, and keeping degree of carbonisation is about 60%.Weak ammonia in this concentration section is except that the part of keeping above-mentioned internal circulating load, and rest part takes out, or enters other ammonia stripping system synthesis use, or sends to the preparation strong aqua.The service temperature of weak ammonia washing section should not be higher than 25 ℃.To the washing process actual detected, ammonia is the 20-40 titre in the liquid phase of weak ammonia washing section middle part, degree of carbonisation 10-15%; Ammonia is 11.2 gram/rice in the gas phase
3, carbonic acid gas≤0.3% is near equilibrium state.Gaseous ammonia content when going out the weak ammonia washing section is 4 gram/rice
3This gas is being lower than under 20 ℃ of conditions through the soft water washing section with soft water after the conventional carrying out washing treatment ammonia in the exhaust gas body＜0.2 gram/rice
3, carbonic acid gas＜0.2% can directly be made the synthetic ammonia unstripped gas and use.
Said process can be finished in a washing tower, also can finish continuously by the plurality of washing tower through setting gradually.In the treating processes, allly can be used as containing ammonia gas and all can incorporating carbonization tail gas into and together handle of syngas for synthetic ammonia; Weak ammonia in other washing system also can enter respectively by the difference of its concentration in the different pump around circuit sections in this process and comprehensively be used.
Below two tables we can say the influence that open fire temperature and degree of carbonisation absorb ammonia.
Table 1 water temperature and ammonia solubleness relation
| Water temperature (℃) | 0 | 10 | 20 | 30 | 40 | 50 |
| Dissolved ammonia (gram) in the 100 gram water | 87.5 | 67.9 | 52.6 | 40.3 | 30.7 | 22.9 |
Table 2 degree of carbonisation is to the influence (20 ℃, weak ammonia concentration is the 95-151 titre) of nitrogen balance dividing potential drop
| Degree of carbonisation (%) | 50 | 60 | 70 | 80 | 100 |
| Nitrogen balance dividing potential drop (mmHg) | 67 | 55 | 45 | 33 | 10 |
Claims (6)
1, a kind ofly reclaims the method that contains ammonia in the ammonia gas that produces in the bicarbonate of ammonia production process as the washing absorption liquid with soft water and weak ammonia, it is characterized in that to contain ammonia gas earlier with degree of carbonisation be lower than 70% pump around circuit weak ammonia washing absorb to ammonia be between gas-liquid two-phase or near balance after, part weak ammonia is removed, rest part mixes the back and continues pump around circuit with the weak ammonia of lower concentration, the quantitative soft water washing of the gas reusing after the weak ammonia washing.
2, the method for claim 1, it is characterized in that in the weak ammonia washing process, be divided into different concentration gradient sections according to ammonia content process from high to low in the gas before and after the washing, weak ammonia in each section carries out pump around circuit respectively, the weak ammonia that is removed in every section all enters the pump around circuit of its next adjacent high density section, rest part mixes the back to be continued to contain ammonia gas and wash through each concentration section from high to low successively in this section pump around circuit with weak ammonia from its adjacent last lower concentration section.
3, method as claimed in claim 2 is characterized in that the degree of carbonisation in the weak ammonia is also successively decreased successively in ammonia content each concentration gradient section from high to low.
4, method as claimed in claim 3 is characterized in that the degree of carbonisation in the said maximum concentration gradient section weak ammonia realizes by adding the carbonization mother liquor behind the filtering bicarbonate of ammonia.
5, the method for claim 1 is characterized in that whole washing process carries out under subambient condition.
6,, it is characterized in that the said ammonia gas that contains is a tail gas behind the carbonization process as the described method of one of claim 1 to 5.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 90106175 CN1061389A (en) | 1990-11-12 | 1990-11-12 | The recovery and treatment method of ammonia during bicarbonate of ammonia is produced |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 90106175 CN1061389A (en) | 1990-11-12 | 1990-11-12 | The recovery and treatment method of ammonia during bicarbonate of ammonia is produced |
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| CN1061389A true CN1061389A (en) | 1992-05-27 |
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| CN 90106175 Pending CN1061389A (en) | 1990-11-12 | 1990-11-12 | The recovery and treatment method of ammonia during bicarbonate of ammonia is produced |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1047366C (en) * | 1996-05-14 | 1999-12-15 | 中国石化茂名石油化工公司 | Technology for refining ammonia |
| CN1297520C (en) * | 2005-04-25 | 2007-01-31 | 明水化肥厂 | Technique for preparing joint product of ammonium hydrogen from triamine |
| CN107126826A (en) * | 2017-04-10 | 2017-09-05 | 天津凯赛特科技有限公司 | Ammonia-contained tail gas treating device and method in prepared by a kind of soda ash |
-
1990
- 1990-11-12 CN CN 90106175 patent/CN1061389A/en active Pending
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1047366C (en) * | 1996-05-14 | 1999-12-15 | 中国石化茂名石油化工公司 | Technology for refining ammonia |
| CN1297520C (en) * | 2005-04-25 | 2007-01-31 | 明水化肥厂 | Technique for preparing joint product of ammonium hydrogen from triamine |
| CN107126826A (en) * | 2017-04-10 | 2017-09-05 | 天津凯赛特科技有限公司 | Ammonia-contained tail gas treating device and method in prepared by a kind of soda ash |
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