CN102847433B - The processing method of tail gas in the production of a kind of sodium nitrate, natrium nitrosum - Google Patents
The processing method of tail gas in the production of a kind of sodium nitrate, natrium nitrosum Download PDFInfo
- Publication number
- CN102847433B CN102847433B CN201210359090.4A CN201210359090A CN102847433B CN 102847433 B CN102847433 B CN 102847433B CN 201210359090 A CN201210359090 A CN 201210359090A CN 102847433 B CN102847433 B CN 102847433B
- Authority
- CN
- China
- Prior art keywords
- tail gas
- natrium nitrosum
- sodium nitrate
- sodium
- catalyst
- 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.)
- Active
Links
- VWDWKYIASSYTQR-UHFFFAOYSA-N sodium nitrate Chemical compound [Na+].[O-][N+]([O-])=O VWDWKYIASSYTQR-UHFFFAOYSA-N 0.000 title claims abstract description 56
- 235000010344 sodium nitrate Nutrition 0.000 title claims abstract description 28
- 239000004317 sodium nitrate Substances 0.000 title claims abstract description 28
- KEAYESYHFKHZAL-UHFFFAOYSA-N Sodium Chemical compound [Na] KEAYESYHFKHZAL-UHFFFAOYSA-N 0.000 title claims abstract description 26
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 14
- 238000003672 processing method Methods 0.000 title claims abstract description 8
- 239000007789 gas Substances 0.000 claims abstract description 58
- 239000003054 catalyst Substances 0.000 claims abstract description 31
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 21
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims abstract description 17
- 159000000000 sodium salts Chemical class 0.000 claims abstract description 17
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 16
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 15
- 239000003595 mist Substances 0.000 claims abstract description 11
- 230000005494 condensation Effects 0.000 claims abstract description 10
- 238000009833 condensation Methods 0.000 claims abstract description 10
- 229910000029 sodium carbonate Inorganic materials 0.000 claims abstract description 9
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 8
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 7
- 238000010531 catalytic reduction reaction Methods 0.000 claims description 22
- 238000010521 absorption reaction Methods 0.000 claims description 20
- 230000003197 catalytic effect Effects 0.000 claims description 20
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims description 12
- 229910010413 TiO 2 Inorganic materials 0.000 claims description 12
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims description 12
- 239000003513 alkali Substances 0.000 claims description 7
- 229910052763 palladium Inorganic materials 0.000 claims description 6
- 229910052697 platinum Inorganic materials 0.000 claims description 6
- 229910001220 stainless steel Inorganic materials 0.000 claims description 6
- 239000010935 stainless steel Substances 0.000 claims description 6
- 230000001413 cellular effect Effects 0.000 claims description 4
- 239000002075 main ingredient Substances 0.000 claims description 3
- 239000008187 granular material Substances 0.000 claims description 2
- 230000005484 gravity Effects 0.000 claims description 2
- 238000000034 method Methods 0.000 abstract description 43
- 239000002912 waste gas Substances 0.000 abstract description 7
- 238000005516 engineering process Methods 0.000 abstract description 6
- 239000000203 mixture Substances 0.000 abstract description 4
- 238000006555 catalytic reaction Methods 0.000 abstract description 2
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 48
- 230000006378 damage Effects 0.000 description 3
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- 239000008280 blood Substances 0.000 description 2
- 210000004369 blood Anatomy 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000009776 industrial production Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 150000003863 ammonium salts Chemical class 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 210000000481 breast Anatomy 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000010668 complexation reaction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000010894 electron beam technology Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 230000003394 haemopoietic effect Effects 0.000 description 1
- 210000002216 heart Anatomy 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 210000003734 kidney Anatomy 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 210000004185 liver Anatomy 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000033116 oxidation-reduction process Effects 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
Abstract
A processing method for tail gas in the production of sodium nitrate, natrium nitrosum, the NO in the waste gas that mist absorption-SCR technology removes sodium nitrate, natrium nitrosum production is discharged is caught in the present invention's employing
x.By condensation wire-mesh mist extractor removing sodium salt (sodium nitrate, natrium nitrosum, sodium carbonate mixture); The waste gas of removing sodium salt, under catalyst action, forms nitrogen and water with ammonia generation catalytic reaction, realizes qualified discharge in crossing current reactor.The present invention is applicable to sodium nitrate, natrium nitrosum manufacturing enterprise tail gas NO
xprocess, this technique has that technique is simple, operating cost is low, non-secondary pollution and NOx process feature thoroughly.
Description
Technical field
The present invention relates to a kind of sodium nitrate, natrium nitrosum tail gas NO
xprocessing method.
Background technology
NOx can be combined by hemochrome in animal blood, makes blood anoxic, causes nervous centralis to benumb, and causes damage, damage the ozone layer to heart, liver, kidney and hematopoietic tissue, and with SO in air
2to coexist formation acid rain with dust, great harm is caused to people and environment.
At present, the method kind of industrial NO_x removal is more, the method of purified treatment NOx can be divided into wet denitration and Dry denitration by Processing tecchnics, and wet denitration comprises absorption process (absorption process can be divided into water absorption method, sour absorption process, alkali absorb method, oxidative absorption method, liquid-phase reduction absorption process), microbial cleaning method etc.; Dry denitration comprises catalytic reduction method (catalytic reduction method can be divided into absorption process can be divided into selective catalytic reduction, non-selective catalytic reduction), absorption method, plasma method (ion method can be divided into electron beam irradiation method and impulse electric corona method), but application is at present more, the technology of development relative maturity is SCR (SCR), liquid absorption method, absorption method, and other method is not industrially used widely.
Oneself SCR (SCR) method be used widely abroad, and this method can obtain higher NOx removal efficiency at a lower temperature, and clearance reaches 85%.This technique can be used for power plant, gas fired-boiler, explosive motor, chemical plant etc., and ammonia injects the flue gas containing NOx as reducing agent, and NOx is reduced to N under the effect of catalyst
2and H
2o.Therefore SCR takes off NOx is a very effective method, but the method catalyst easily poisons, and disposal cost is high, generates the surface that ammonium salt can be deposited on heat exchanger and miscellaneous equipment, reduces the thermal efficiency.
NOx in absorption process purifying exhaust air, by the kind of absorbent being divided into water absorption method, sour absorption process, alkali absorb method, oxidationreduction and Absorption via Chemical Complexation etc.Because absorbent kind is more, source is also wide, so strong adaptability, but this method removal NOx efficiency is lower, and energy consumption is high, easily causes secondary pollution.
Existing industrial production sodium nitrate, natrium nitrosum, main employing selects ammoxidation rear oxidation nitrogen directly to absorb (dense gas method) technique, the advantage of this technique is can according to the demand of market to sodium nitrate and sodium nitrate in producing, the ratio of any adjustment natrium nitrosum and sodium nitrate, even if but shortcoming is nitrogen oxide gas enter five series connection Alkali absorption towers absorb after, the NO in tail gas
xcontent is also at more than 2000ppm, and in tail gas, be also entrained with a large amount of sodium salts (mixture of sodium nitrate, natrium nitrosum, sodium carbonate), if be directly discharged in air, both resource was wasted, cause environmental pollution again, therefore the content of NOx how is reduced in 240ppm(discharging standards) below, reclaim the sodium salt carried secretly in tail gas own through becoming the key issue of sodium nitrate, natrium nitrosum industrial production, operation.
Based on above analysis, from current prior art both at home and abroad, be difficult to reach removing sodium nitrate, natrium nitrosum production tail gas NO
xobject, therefore develop high efficiency waste gas and take off NO
xtechnology be after exhuast gas desulfurization and the key subjects another urgently to be resolved hurrily of facing.
Summary of the invention
For the catalysts selective catalytic reduction method of prior art, the deficiency of absorption process, the mist absorption-SCR technology of catching that a kind of technique is advanced, operating cost is low is the object of the present invention is to provide to remove tail gas NO in sodium nitrate, natrium nitrosum production
xthe method of process.
The object of the present invention is achieved like this: the processing method of tail gas in the production of a kind of sodium nitrate, natrium nitrosum, from Alkali absorption tower waste gas out through a condensation wire-mesh mist extractor removing sodium salt, the NOx gas sloughing sodium salt enters tail gas pre-heater, heater exhaust gas enters catalytic reactor and namely to flow over reactor after being heated to 170 ~ 190 DEG C, the steam of heater exhaust gas is from webmaster, steam condensate back boiler room, the gas ammonia of crossing current reactor is from synthetic ammonia installation.Under catalyst action, pressure is 0.1 ~ 0.11Mpa, and temperature is that the condition of 170 ~ 190 DEG C and reducibility gas carry out catalytic reduction reaction, by NO
xbe reduced to nitrogen and water.
Described tail gas Main Ingredients and Appearance is drop and the NO of sodium nitrate, natrium nitrosum and sodium carbonate
x.
Described reducibility gas is ammonia.
Described catalyst is cellular platinum, palladium, V
2o
5-WO
3/ TiO
2, MnO
x/ TiO
2or Fe-ZSM-5.
Honeycombed catalyst is placed in stainless steel module, and stainless steel module is placed in catalytic reactor and forms beds, and beds is three layers.
By NO
xthe tail gas be reduced to after nitrogen and water enters after tail gas pre-heater reclaims heat and discharges.
The processing method of tail gas in the production of sodium nitrate provided by the invention, natrium nitrosum, beneficial effect is as follows:
1, chimney breast NOx content < 160 ppm, the discharge of NOx reaches discharging standards.
2, decrease poisoning catalyst, the present invention eliminates the drop of sodium nitrate, natrium nitrosum and sodium carbonate, if do not remove, is adsorbed on catalyst surface, causes catalyst activity to reduce.
3, produce the manufacturing enterprise of 80,000 tons of sodium nitrate, natrium nitrosum per year, adopt this technology every year can voluminous sodium nitrate, natrium nitrosum 360 tons, reduce with ammonia 100 tons.
Accompanying drawing explanation
Below in conjunction with drawings and Examples, the invention will be further described.
Fig. 1 is schematic flow sheet of the present invention.
Detailed description of the invention
Catalyst is placed: honeycombed catalyst is placed in stainless steel module, and stainless steel module is placed in catalytic reactor and forms beds, and beds is three layers.
Operation principle of the present invention is as follows: Alkali absorption tower waste gas is out through a condensation wire-mesh mist extractor, by manufacturing a large amount of millimetre-sized water droplets in condensation wire-mesh mist extractor, millimetre-sized water droplet is allowed to go to catch micron-sized water droplet, thus the drop isolated containing sodium salt in tail gas, remaining gas contains the drop containing sodium salt of a small amount of submillimeter level, again through the removing of condensation silk screen, with atomized water low speed by silk screen generation cohesion, granule water droplet becomes bulky grain water droplet, then by Action of Gravity Field removing sodium salt (sodium nitrate, natrium nitrosum, sodium carbonate mixture), the waste gas of removing sodium salt (sodium nitrate, natrium nitrosum, sodium carbonate mixture), with cellular platinum, palladium, V
2o
5-WO
3/ TiO
2, MnO
x/ TiO
2, Fe-ZSM-5 is catalyst, be 0.1 ~ 0.11MPa at pressure, temperature is 170 ~ 190 DEG C, and the NOx gas sloughing sodium salt forms nitrogen (N with ammonia generation catalytic reaction in crossing current reactor
2) and water (H
2o), realize row's dye up to standard to put.
embodiment 1
From the Alkali absorption tower sodium nitrate, natrium nitrosum production process out waste gas (Main Ingredients and Appearance is NO
x, salt made from earth containing a comparatively high percentage of sodium chloride and carbonate drop) through condensation wire-mesh mist extractor removing sodium salt (sodium nitrate, natrium nitrosum, sodium carbonate drop), slough NOx gas and the reducibility gas NH of sodium salt
3, with cellular flat platinum for catalyst, be 0.10 ~ 0.11Mpa at pressure, temperature is carry out catalytic reduction reaction in the catalytic reactor of 180 DEG C, by NO
xbe reduced to nitrogen (N
2) and water (H
2o).And discharge a large amount of heat, enter after tail gas pre-heater reclaims heat from gas and enter chimney.After testing, the nitrogen oxide in tail gas content of chimney is 156ppm.
embodiment 2
With honeycomb platinum for catalyst, be 0.10 ~ 0.11Mpa at pressure, temperature is carry out catalytic reduction reaction in the catalytic reactor of 170 DEG C, and all the other are with embodiment 1, and the nitrogen oxide in tail gas content of chimney is 160ppm.
embodiment 3
With honeycomb platinum for catalyst, be 0.1MPa at pressure, temperature is carry out catalytic reduction reaction in the catalytic reactor of 190 DEG C, and all the other are with embodiment 1, and the nitrogen oxide in tail gas content of chimney is 145ppm.
embodiment 4
With honeycomb palladium for catalyst, be 0.10 ~ 0.11Mpa at pressure, temperature is carry out catalytic reduction reaction in the catalytic reactor of 170 DEG C, and all the other are with embodiment 1, and the nitrogen oxide in tail gas content of chimney is 170ppm.
embodiment 5
With honeycomb palladium for catalyst, be 0.1MPa at pressure, temperature is carry out catalytic reduction reaction in the catalytic reactor of 180 DEG C, and all the other are with embodiment 1, and the nitrogen oxide in tail gas content of chimney is 158ppm.
embodiment 5
With honeycomb palladium for catalyst, be 0.10 ~ 0.11Mpa at pressure, temperature is carry out catalytic reduction reaction in the catalytic reactor of 190 DEG C, and all the other are with embodiment 1, and the nitrogen oxide in tail gas content of chimney is 160ppm.
embodiment 6
With V
2o
5-WO
3/ TiO
2for catalyst, be 0.10 ~ 0.11Mpa at pressure, temperature is carry out catalytic reduction reaction in the catalytic reactor of 170 DEG C, and all the other are with embodiment 1, and the nitrogen oxide in tail gas content of chimney is 220ppm.
embodiment 7
With V
2o
5-WO
3/ TiO
2for catalyst, be 0.1MPa at pressure, temperature is carry out catalytic reduction reaction in the catalytic reactor of 180 DEG C, and all the other are with embodiment 1, and the nitrogen oxide in tail gas content of chimney is 192ppm.
embodiment 8
With V
2o
5-WO
3/ TiO
2for catalyst, be 0.10 ~ 0.11Mpa at pressure, temperature is carry out catalytic reduction reaction in the catalytic reactor of 190 DEG C, and all the other are with embodiment 1, and the nitrogen oxide in tail gas content of chimney is 185ppm.
embodiment 9
With MnO
x/ TiO
2for catalyst, be 0.10 ~ 0.11Mpa at pressure, temperature is carry out catalytic reduction reaction in the catalytic reactor of 170 DEG C, and all the other are with embodiment 1, and the nitrogen oxide in tail gas content of chimney is 230ppm.
embodiment 10
With MnO
x/ TiO
2for catalyst, be 0.10 ~ 0.11Mpa at pressure, temperature is carry out catalytic reduction reaction in the catalytic reactor of 180 DEG C, and all the other are with embodiment 1, and the nitrogen oxide in tail gas content of chimney is 227ppm.
embodiment 11
With MnO
x/ TiO
2for catalyst, be 0.10 ~ 0.11Mpa at pressure, temperature is carry out catalytic reduction reaction in the catalytic reactor of 190 DEG C, and all the other are with embodiment 1, and the nitrogen oxide in tail gas content of chimney is 200ppm.
embodiment 12
Taking Fe-ZSM-5 as catalyst, is 0.10 ~ 0.11Mpa at pressure, and temperature is carry out catalytic reduction reaction, the other the same as in Example 1 in the catalytic reactor of 170 DEG C, and the nitrogen oxide in tail gas content of chimney is 252ppm.
embodiment 13
Taking Fe-ZSM-5 as catalyst, is 0.10 ~ 0.11Mpa at pressure, and temperature is carry out catalytic reduction reaction, the other the same as in Example 1 in the catalytic reactor of 180 DEG C, and the nitrogen oxide in tail gas content of chimney is 241ppm.
embodiment 14
Taking Fe-ZSM-5 as catalyst, is 0.10 ~ 0.11Mpa at pressure, and temperature is carry out catalytic reduction reaction, the other the same as in Example 1 in the catalytic reactor of 190 DEG C, and the nitrogen oxide in tail gas content of chimney is 225ppm.
Claims (2)
1. a sodium nitrate, the processing method of tail gas in natrium nitrosum production, it is characterized in that: from Alkali absorption tower tail gas out through a condensation wire-mesh mist extractor, by manufacturing a large amount of millimetre-sized water droplets in condensation wire-mesh mist extractor, millimetre-sized water droplet is allowed to go to catch micron-sized water droplet, thus the drop isolated containing sodium salt in tail gas, remaining gas contains the drop containing sodium salt of a small amount of submillimeter level, again through the removing of condensation wire-mesh mist extractor, with atomized water low speed by condensation wire-mesh mist extractor generation cohesion, granule water droplet becomes bulky grain water droplet, then by Action of Gravity Field removing sodium salt, slough the NO of sodium salt
xgas enters tail gas pre-heater, heater exhaust gas enters catalytic reactor after being heated to 170 ~ 190 DEG C, and under catalyst action, pressure is 0.1 ~ 0.11MPa, and temperature is that the condition of 170 ~ 190 DEG C and ammonia carry out catalytic reduction reaction, by NO
xbe reduced to nitrogen and water,
Described tail gas Main Ingredients and Appearance is drop and the NO of sodium nitrate, natrium nitrosum and sodium carbonate
x,
Described catalyst is cellular platinum, palladium, V
2o
5-WO
3/ TiO
2, MnO
x/ TiO
2or Fe-ZSM-5, wherein honeycombed catalyst is placed in stainless steel module, and stainless steel module is placed in catalytic reactor and forms beds, and beds is three layers.
2. sodium nitrate according to claim 1, natrium nitrosum produce in the processing method of tail gas, it is characterized in that: described NO
xthe tail gas be reduced to after nitrogen and water enters after tail gas pre-heater reclaims heat and discharges.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210359090.4A CN102847433B (en) | 2012-09-25 | 2012-09-25 | The processing method of tail gas in the production of a kind of sodium nitrate, natrium nitrosum |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210359090.4A CN102847433B (en) | 2012-09-25 | 2012-09-25 | The processing method of tail gas in the production of a kind of sodium nitrate, natrium nitrosum |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102847433A CN102847433A (en) | 2013-01-02 |
| CN102847433B true CN102847433B (en) | 2015-08-26 |
Family
ID=47394652
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210359090.4A Active CN102847433B (en) | 2012-09-25 | 2012-09-25 | The processing method of tail gas in the production of a kind of sodium nitrate, natrium nitrosum |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102847433B (en) |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7390471B2 (en) * | 2005-11-17 | 2008-06-24 | Siemens Power Generation, Inc. | Apparatus and method for catalytic treatment of exhaust gases |
| CN202044875U (en) * | 2011-06-20 | 2011-11-23 | 西安同大实业有限公司 | High-efficiency separator for tail gas of device with sodium nitrate and sodium nitrite |
-
2012
- 2012-09-25 CN CN201210359090.4A patent/CN102847433B/en active Active
Non-Patent Citations (4)
| Title |
|---|
| "高效低温氨选择还原NOx催化剂的研制和工业应用;刘淑文等;《第六届全国硝酸硝酸盐技术交流会论文集》;20111101;第53-54页 * |
| 四川电力建设二公司组编.烟气脱硝的现场施工.《火力发电厂脱硫脱硝施工安装与运行技术》.2010,第190-191页. * |
| 梁仁杰等.天然气的分离与净化.《化工工艺学》.1998,第229-230页. * |
| 直接法生产亚硝酸钠、硝酸钠尾气分离器的改造;张正滨等;《无机盐工业》;20061031;第38卷(第10期);参见第46-47页 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102847433A (en) | 2013-01-02 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101439260B (en) | System for removing nitrous oxides in low-temperature flue gas and technique thereof | |
| CN102266723B (en) | Regenerating method and regenerating device for selective catalytic reduction de-nitration catalyst | |
| CN103878034B (en) | The renovation process of a kind of arsenic and phosphorism denitrifying catalyst with selective catalytic reduction | |
| CN104495837B (en) | Sargassum-based activated carbon and preparation method and application thereof | |
| CN103878035B (en) | The regenerated liquid of a kind of vanadium, titanium based selective catalytic-reduction denitrified catalyst | |
| CN101874964B (en) | Low temperature storage and reduction method for purifying oxynitrides | |
| CN101279185A (en) | Gas phase oxidation-liquid phase reduction method for absorbing and removing nitrous oxides in exhaust air | |
| CN104888806A (en) | Regeneration method for inactivated TiV-based honeycomb denitration catalyst having combined denitration and demercuration modification function | |
| CN103212245B (en) | Dedusting filter material containing MnO2 catalyst, and preparation method and application thereof | |
| CN107282141B (en) | Photocatalyst for desulfurization and denitrification of ship flue gas and preparation method thereof | |
| CN106311245A (en) | Preparation method for lignite semi-coke-based denitration agent used for low-temperature catalytic oxidation | |
| CN102949930A (en) | Method for NO oxidation and nitrogen oxide removal at room temperature through synergism of plasma and catalyst | |
| CN203123795U (en) | Flue gas denitration device using ozone oxidation method | |
| CN110433788A (en) | Using biomass-based active carbon as denitrating catalyst of carrier and preparation method thereof | |
| CN202136916U (en) | Flue gas purification system | |
| CN106475108A (en) | A kind of multiple-effect denitrating catalyst and preparation method thereof | |
| CN111054209B (en) | Low-temperature SCR denitration process based on ethylene reducing agent | |
| CN107952494A (en) | A kind of renovation process of SCR catalyst | |
| CN102847433B (en) | The processing method of tail gas in the production of a kind of sodium nitrate, natrium nitrosum | |
| CN102513094B (en) | Preparation method of sulphur-resisting low temperature selectivity catalytic reduction nitric oxide catalysts | |
| CN105396626A (en) | Regeneration liquid of SCR denitration catalyst and regeneration method of SCR denitration catalyst | |
| CN201776085U (en) | Heating type denitration device | |
| CN105013303A (en) | Combined desulfurization, denitration and decarburization device for flue gas | |
| CN110841447A (en) | Wet-method-SCR combined purification method and system for waste incineration flue gas | |
| CN203916428U (en) | A kind of flue gas combined desulfurization nitre carbon device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20210714 Address after: 444100 No.1 Jinping Avenue, Dangyang city, Yichang City, Hubei Province Patentee after: HUAQIANG CHEMICAL GROUP Co.,Ltd. Address before: 443002 No. 8, University Road, Yichang, Hubei Patentee before: CHINA THREE GORGES University Patentee before: HUAQIANG CHEMICAL GROUP Co.,Ltd. |
|
| TR01 | Transfer of patent right | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of invention: A method for treating tail gas in the production of sodium nitrate and sodium nitrite Granted publication date: 20150826 Pledgee: Hubei Dangyang Rural Commercial Bank Co.,Ltd. Pledgor: HUAQIANG CHEMICAL GROUP Co.,Ltd. Registration number: Y2024980006527 |
|
| PE01 | Entry into force of the registration of the contract for pledge of patent right |