CN201793380U - Ammonium hydrogen carbonate pyrolysis ammonia production system - Google Patents
Ammonium hydrogen carbonate pyrolysis ammonia production system Download PDFInfo
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- CN201793380U CN201793380U CN2010205227790U CN201020522779U CN201793380U CN 201793380 U CN201793380 U CN 201793380U CN 2010205227790 U CN2010205227790 U CN 2010205227790U CN 201020522779 U CN201020522779 U CN 201020522779U CN 201793380 U CN201793380 U CN 201793380U
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- ammonia
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Abstract
The utility model belongs to the field of chemical ammonia production systems, and particularly relates to an ammonium hydrogen carbonate pyrolysis ammonia production system. The ammonium hydrogen carbonate pyrolysis ammonia production system comprises a powder bin; and the powder bin is connected in series with a powder feeder, a Venturi mixer, a pyrolysis chamber, a buffer tank, an ammonia-air mixer, an ammonia spraying grille and a selective catalytic reduction (SCR) reactor. By direct pyrolysis of ammonium hydrogen carbonate granules, the system reduces a dissolution system of an urea reducer, saves the floor area of equipment, reduces system complexity, avoids the potential safety hazards of reducers such as liquid ammonia, aqueous ammonia and the like during transportation and storage, simplifies system design, and further improves the economical efficiency; and the whole denitration system is compact and efficient.
Description
One, technical field:
The utility model belongs to chemistry system ammonia system field, especially relates to a kind of ammonium bicarbonate pyrolysis ammonia production system.
Two, background technology:
Along with the raising of environmental protection standard, country is to the oxynitride (NO of thermal power plant
X) discharging proposed strict requirement, numerous thermal power plants require denitrification apparatus is installed, and in the middle of numerous method of denitration, the SCR denitrating technique becomes the first-selection of thermal power plant's denitrification apparatus with its unique advantage, and SCR technology utilization denitrification reducing agent is prepared NH
3Utilize ammonia-spraying grid to mix, under catalyst action, be reduced to N with flue gas
2
The reductive agent of SCR denitrating flue gas generally has three kinds: liquefied ammonia, ammoniacal liquor and urea.Liquefied ammonia generally adopts the ammonia of purity 99.8%, inclusion-free; Ammoniacal liquor [NH
4OH] commercial general utilization concentration is 20%～30% ammoniacal liquor, needs to consume a large amount of electric power in the evaporative process; Urea [CO (NH
2)
2] be particulate state, need be dissolved into the aqueous solution during evaporation.
Three kinds of reductive agents, the expense of the reagent expense of liquid ammonia process for caustic soda purification, initial cost, operation is minimum, but ammonia is the Class B hazardous substance of national regulation, all has certain danger in the transportation of liquefied ammonia and storage process, and the transportation of liquefied ammonia and storing all needs examining of national departments concerned and permits.The storage capacity of liquefied ammonia surpasses 40 tons can be listed in major hazard source.
The ammoniacal liquor massfraction that the ammoniacal liquor method is used is 20%～30%, and than liquefied ammonia safety, but ammoniacal liquor also is a kind of dangerous substances, has toxicity and corrodibility, and the ammonia of lower concentration stimulates eyes, skin and nose, and transportation volume is big, the pure relatively ammonia height of transportation cost.
The urea that Wyler's process uses stores as particulate form, and reductive agent is safe and harmless, but urea system ammonia system complexity, floor space are big, initial cost and working cost are very high, and urea has the deliquescence problem as reductive agent, and urea addn influences SCR catalyzer work-ing life.
In a word, three kinds of methods respectively have quality, bicarbonate of ammonia stores for particulate form at normal temperatures and pressures, does not have toxicity, is China's second largest nitrogenous fertilizer except urea, so wide material sources, storage and transportation aspect do not have safety problem yet, compare with urea, because bicarbonate of ammonia can generate ammonia in the particulate form pyrolysis, and bicarbonate of ammonia does not have corrodibility yet, so bicarbonate of ammonia system ammonia system economy is better.Comprehensive each side considers that bicarbonate of ammonia is suitable as denitrification reducing agent.Therefore, the present invention proposes the system and the technology of bicarbonate of ammonia pyrolysis system ammonia.
Three, summary of the invention:
The utility model is in order to solve the weak point in the above-mentioned background technology, provide a kind of system succinct, produce ammonium bicarbonate pyrolysis ammonia production system efficiently.
For achieving the above object, the technical solution adopted in the utility model is: a kind of ammonium bicarbonate pyrolysis ammonia production system, comprise the powder storehouse, it is characterized in that: described powder storehouse is serially connected with machine supplying powder, venturi mixing tank, pyrolysis chamber, surge tank, ammonia air mixer, ammonia-spraying grid and SCR reactor successively.
Also be connected with the powder feeding blower fan on the described venturi mixing tank.
Also be connected in series in the described pyrolysis chamber and be provided with well heater and warm air blower fan.
Also be provided with variable valve between described surge tank and the ammonia air mixer, also be provided with the dilution blower fan on the ammonia air mixer.
Described pyrolysis chamber is vertical rectangular parallelepiped jar, and described vertical rectangular parallelepiped tank bottom is provided with two warm air inlet tubes, and top is provided with a mixed gas inlet tube, and four bicarbonate of ammonia gas inlet tubes are set around the tank body.
Compared with prior art, the direct pyrolysis bicarbonate of ammonia of native system particle, reduced the dissolution system of carbamide reducing agent, save occupation area of equipment and reduce system complexity, avoid the potential safety hazard of reductive agents such as liquefied ammonia and ammoniacal liquor aspect the transportation storage, simplified system design, further improved economy, whole denitrating system is succinct, and is efficient.
Four, description of drawings:
Fig. 1 is a structural representation of the present utility model;
Fig. 2 is the utility model pyrolysis chamber synoptic diagram;
Fig. 3 is the A-A sectional view of Fig. 2;
Fig. 4 is the B-B sectional view of Fig. 2.
Description of reference numerals: 1-powder storehouse, 2-machine supplying powder, 3-venturi mixing tank, 4-powder feeding blower fan, 5-warm air blower fan, 7.1-warm air inlet tube, 7.2-bicarbonate of ammonia gas inlet tube, 7.3-mixed gas inlet tube, 6-well heater, 7-pyrolysis chamber, 8-surge tank, 9-variable valve, 10-dilution blower fan, 11-ammonia air mixer, 12-ammonia-spraying grid, 13-flue gas, 14-SCR reactor.
Five, embodiment:
Referring to Fig. 1: a kind of ammonium bicarbonate pyrolysis ammonia production system, comprise powder storehouse 1, described powder storehouse 1 is serially connected with machine supplying powder 2, venturi mixing tank 3, pyrolysis chamber 7, surge tank 8, ammonia air mixer 11, ammonia-spraying grid 12 and SCR reactor 14 successively, also be connected with powder feeding blower fan 4 on the described venturi mixing tank 3, also be connected in series in the described pyrolysis chamber 7 and be provided with well heater 6 and warm air blower fan 5, also be provided with variable valve 9 between described surge tank 8 and the ammonia air mixer 11, also be provided with dilution blower fan 10 on the ammonia air mixer 11.
Bicarbonate of ammonia in the powder storehouse 1 enters the powder-feeding amount of venturi mixer 3 by machine supplying powder 2 controls, enter pyrolysis chamber 7 by bicarbonate of ammonia gas inlet tube 7.2 and become ammonia with the warm air mixed decomposition that is heated to 300 ℃ by well heater 6, carbonic acid gas and water, enter surge tank 8 from mixed gas inlet tube 7.3 then, surge tank and associated conduit are incubated, to prevent that water condenses in the gas, surge tank 8 outlet mixed gass are regulated the ammonia amount that enters ammonia mixing tank 11 by variable valve 9, by 10 dilutions of dilution blower fan is that concentration is about 5% gas, send into ammonia-spraying grid 12, flue gas 13 with the upstream mixes and enters 14 reaction of SCR system catalyst layer, NO
XBe reduced into N
2
Described pyrolysis chamber, surge tank and associated pipe are taked the insulation measure, avoid that water condenses in the gas.
Referring to Fig. 2, Fig. 3, Fig. 4: pyrolysis chamber 7 is vertical rectangular parallelepiped jar, described tank body bottom is provided with two warm air inlet tubes 7.1, top is provided with a mixed gas inlet tube 7.3, around the tank body four bicarbonate of ammonia gas inlet tubes 7.2 are set, the height of pyrolysis chamber must guarantee that the bicarbonate of ammonia powder stopped 0.3～0.5 second so that the complete pyrolysis of bicarbonate of ammonia in stove.
Four bicarbonate of ammonia inlet tubes adopt the blended mode that liquidates, two warm air inlet tubes lay respectively under two pairs of bicarbonate of ammonia inlet tubes, guarantee that warm air has the support effect to the bicarbonate of ammonia powder, to guarantee that the bicarbonate of ammonia powder has enough residence time in pyrolysis oven, reach 100% and decompose.
The mixed gas outlet pipe is positioned at pyrolysis chamber's cross-section center, according to the related experiment data as can be known, in the time of 300 ℃, bicarbonate of ammonia can decompose fully in the 0.1s left and right sides, the inlet that bicarbonate of ammonia is sent into the pyrolysis chamber is two groups of nozzles that liquidate, utilize two groups of relative nozzles to cause intensive to mix, and warm air enters the pyrolysis chamber and the bicarbonate of ammonia powder is had good support effect by inlet, bicarbonate of ammonia is stopped in the pyrolysis chamber decomposed to reach fully in 0.1～0.5 second.
The bicarbonate of ammonia nitrogen content is 17%, and urea is 46%, and the bicarbonate of ammonia price is about 600 yuan/T at present, and the urea price is 1900 yuan/T, and the ammonia of every generation 1kg then spends 2.79 yuan bicarbonate of ammonia, perhaps 3.35 yuan urea.Contrast uses bicarbonate of ammonia system ammonia more economical as can be known.Because the theoretical pyrolysis temperature of bicarbonate of ammonia is 86 ℃, agrochemical bicarbonate of ammonia is owing to wherein contain impurity, therefore decomposition temperature is about 60 ℃, and this technology utilization bicarbonate of ammonia can be in the direct pyrolytic characteristics of graininess, avoided being provided with dissolution system, make that denitrating system is more succinct, occupation area of equipment is littler, improved economy and security.
The technical process of ammonium bicarbonate pyrolysis ammonia production system of the present invention is:
1) the bicarbonate of ammonia powder stores by canning cart or packed sending in the powder storehouse 1 by bag-crusher;
2) machine supplying powder 2 under the powder storehouse 1 is regulated rotating speed according to the amount in the flue gas, the control powder-feeding amount;
3) the bicarbonate of ammonia powder falls into the air that venturi mixer 3 blown by powder feeding blower fan 4 and is transported to pyrolysis chamber 7;
4) in pyrolysis chamber 7, the bicarbonate of ammonia powder is blown into the wind heater via through overfire air blower fan 5 and heats be decomposed out ammonia, carbonic acid gas and water;
5) mixed gas after the pyrolysis flows into surge tank 8, enters ammonia air mixer 11 by variable valve 9 subsequently and dilutes;
6) enter SCR reactor 14 behind flue gas 13 uniform mixing of the mixed gas after the dilution by ammonia-spraying grid 12 and upstream, under the effect of catalyst V 2O5-WO3/TiO2, NOX is reduced into, reach the denitrating flue gas purpose.
NOx measures into certain funtcional relationship in the powder-feeding amount of machine supplying powder 2 and the flue gas:
The powder-feeding amount of bicarbonate of ammonia is:
The Q-flue gas flow, Nm
3/ h
C
NONO concentration in the-flue gas, mg/Nm
3
The K-ammonia nitrogen is than coefficient, and promptly the mol ratio coefficient of ammonia and oxynitride generally gets 1.05.
Claims (5)
1. ammonium bicarbonate pyrolysis ammonia production system, comprise powder storehouse (1), it is characterized in that: described powder storehouse (1) is serially connected with machine supplying powder (2), venturi mixing tank (3), pyrolysis chamber (7), surge tank (8), ammonia air mixer (11), ammonia-spraying grid (12) and SCR reactor (14) successively.
2. a kind of ammonium bicarbonate pyrolysis ammonia production system according to claim 1 is characterized in that: also be connected with powder feeding blower fan (4) on the described venturi mixing tank (3).
3. a kind of ammonium bicarbonate pyrolysis ammonia production system according to claim 1 is characterized in that: also be connected in series on described pyrolysis chamber (7) and be provided with well heater (6) and warm air blower fan (5).
4. a kind of ammonium bicarbonate pyrolysis ammonia production system according to claim 1, it is characterized in that: also be provided with variable valve (9) between described surge tank (8) and the ammonia air mixer (11), also be provided with dilution blower fan (10) on the ammonia air mixer (11).
5. a kind of ammonium bicarbonate pyrolysis ammonia production system according to claim 1, it is characterized in that: described pyrolysis chamber (7) are vertical rectangular parallelepiped jar, described vertical rectangular parallelepiped tank bottom is provided with two warm air inlet tubes (7.1), top is provided with a mixed gas inlet tube (7.3), and four bicarbonate of ammonia gas inlet tubes (7.2) are set around the tank body.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010205227790U CN201793380U (en) | 2010-09-09 | 2010-09-09 | Ammonium hydrogen carbonate pyrolysis ammonia production system |
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|---|---|---|---|
| CN2010205227790U CN201793380U (en) | 2010-09-09 | 2010-09-09 | Ammonium hydrogen carbonate pyrolysis ammonia production system |
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| CN201793380U true CN201793380U (en) | 2011-04-13 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101913624A (en) * | 2010-09-09 | 2010-12-15 | 西安热工研究院有限公司 | Ammonium bicarbonate pyrolysis ammonia production system and process flow thereof |
| CN103301722A (en) * | 2013-06-06 | 2013-09-18 | 四川亚连科技有限责任公司 | Nitrogen-reduction denitration ammonia water device and method for preparing ammonium carbonate or ammonium bicarbonate as well as use thereof |
| CN103964469A (en) * | 2013-02-06 | 2014-08-06 | 中国大唐集团环境技术有限公司 | Device for preparing ammonia through pyrolysis of urea |
-
2010
- 2010-09-09 CN CN2010205227790U patent/CN201793380U/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101913624A (en) * | 2010-09-09 | 2010-12-15 | 西安热工研究院有限公司 | Ammonium bicarbonate pyrolysis ammonia production system and process flow thereof |
| CN103964469A (en) * | 2013-02-06 | 2014-08-06 | 中国大唐集团环境技术有限公司 | Device for preparing ammonia through pyrolysis of urea |
| CN103301722A (en) * | 2013-06-06 | 2013-09-18 | 四川亚连科技有限责任公司 | Nitrogen-reduction denitration ammonia water device and method for preparing ammonium carbonate or ammonium bicarbonate as well as use thereof |
| CN103301722B (en) * | 2013-06-06 | 2015-09-30 | 四川亚连科技有限责任公司 | Nitrogen denitration ammoniacal liquor method falls in ammonium carbonate or carbonic hydroammonium system |
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|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20110413 Termination date: 20140909 |
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| EXPY | Termination of patent right or utility model |