CN105617857A - Method for performing selective low-temperature catalytic reduction on NO by use of PH3 - Google Patents
Method for performing selective low-temperature catalytic reduction on NO by use of PH3 Download PDFInfo
- Publication number
- CN105617857A CN105617857A CN201610001895.XA CN201610001895A CN105617857A CN 105617857 A CN105617857 A CN 105617857A CN 201610001895 A CN201610001895 A CN 201610001895A CN 105617857 A CN105617857 A CN 105617857A
- Authority
- CN
- China
- Prior art keywords
- nitrate
- reduction
- concentration
- based catalyst
- gas
- 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.)
- Granted
Links
- 238000000034 method Methods 0.000 title claims abstract description 38
- 238000010531 catalytic reduction reaction Methods 0.000 title abstract description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 24
- 239000003054 catalyst Substances 0.000 claims abstract description 24
- 239000003638 chemical reducing agent Substances 0.000 claims abstract description 12
- 238000006243 chemical reaction Methods 0.000 claims abstract description 10
- 230000009467 reduction Effects 0.000 claims description 30
- 239000002250 absorbent Substances 0.000 claims description 22
- 230000002745 absorbent Effects 0.000 claims description 22
- 239000003610 charcoal Substances 0.000 claims description 22
- 229910002651 NO3 Inorganic materials 0.000 claims description 13
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims description 13
- VCJMYUPGQJHHFU-UHFFFAOYSA-N iron(3+);trinitrate Chemical compound [Fe+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O VCJMYUPGQJHHFU-UHFFFAOYSA-N 0.000 claims description 12
- KBJMLQFLOWQJNF-UHFFFAOYSA-N nickel(ii) nitrate Chemical compound [Ni+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O KBJMLQFLOWQJNF-UHFFFAOYSA-N 0.000 claims description 7
- OERNJTNJEZOPIA-UHFFFAOYSA-N zirconium nitrate Chemical compound [Zr+4].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O OERNJTNJEZOPIA-UHFFFAOYSA-N 0.000 claims description 6
- UFMZWBIQTDUYBN-UHFFFAOYSA-N cobalt dinitrate Chemical group [Co+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O UFMZWBIQTDUYBN-UHFFFAOYSA-N 0.000 claims description 5
- 229910001981 cobalt nitrate Inorganic materials 0.000 claims description 5
- XTVVROIMIGLXTD-UHFFFAOYSA-N copper(II) nitrate Chemical compound [Cu+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O XTVVROIMIGLXTD-UHFFFAOYSA-N 0.000 claims description 5
- FYDKNKUEBJQCCN-UHFFFAOYSA-N lanthanum(3+);trinitrate Chemical compound [La+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O FYDKNKUEBJQCCN-UHFFFAOYSA-N 0.000 claims description 4
- MIVBAHRSNUNMPP-UHFFFAOYSA-N manganese(2+);dinitrate Chemical compound [Mn+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O MIVBAHRSNUNMPP-UHFFFAOYSA-N 0.000 claims description 4
- 238000006555 catalytic reaction Methods 0.000 claims description 3
- HSJPMRKMPBAUAU-UHFFFAOYSA-N cerium(3+);trinitrate Chemical compound [Ce+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O HSJPMRKMPBAUAU-UHFFFAOYSA-N 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 2
- 239000007789 gas Substances 0.000 abstract description 24
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 abstract description 16
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 abstract description 9
- 229910000069 nitrogen hydride Inorganic materials 0.000 abstract description 8
- XYFCBTPGUUZFHI-UHFFFAOYSA-N Phosphine Chemical compound P XYFCBTPGUUZFHI-UHFFFAOYSA-N 0.000 abstract description 6
- 239000004202 carbamide Substances 0.000 abstract description 5
- 239000002699 waste material Substances 0.000 abstract description 3
- 239000003344 environmental pollutant Substances 0.000 abstract description 2
- 231100000719 pollutant Toxicity 0.000 abstract description 2
- 238000004064 recycling Methods 0.000 abstract description 2
- 239000000126 substance Substances 0.000 abstract description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 abstract 1
- 229910052698 phosphorus Inorganic materials 0.000 abstract 1
- 239000011574 phosphorus Substances 0.000 abstract 1
- 229910000073 phosphorus hydride Inorganic materials 0.000 description 37
- 238000006722 reduction reaction Methods 0.000 description 23
- 239000003546 flue gas Substances 0.000 description 17
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 16
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 9
- 239000001301 oxygen Substances 0.000 description 9
- 229910052760 oxygen Inorganic materials 0.000 description 9
- 238000004088 simulation Methods 0.000 description 9
- 238000010586 diagram Methods 0.000 description 8
- NBIIXXVUZAFLBC-UHFFFAOYSA-N phosphoric acid Substances OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 8
- 229910021529 ammonia Inorganic materials 0.000 description 5
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 4
- 235000013877 carbamide Nutrition 0.000 description 4
- 238000000746 purification Methods 0.000 description 4
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 239000003905 agrochemical Substances 0.000 description 2
- 150000003863 ammonium salts Chemical class 0.000 description 2
- 230000006378 damage Effects 0.000 description 2
- BHEPBYXIRTUNPN-UHFFFAOYSA-N hydridophosphorus(.) (triplet) Chemical compound [PH] BHEPBYXIRTUNPN-UHFFFAOYSA-N 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 230000004044 response Effects 0.000 description 2
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- -1 nitrous acid ammonium salt Chemical class 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/54—Nitrogen compounds
- B01D53/56—Nitrogen oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
- B01D2257/404—Nitrogen oxides other than dinitrogen oxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Catalysts (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a method for performing selective low-temperature catalytic reduction on NO by use of PH3. According to the method, PH3 serving as a reducing agent is used for performing catalytic reduction on NO in the presence of activated carbon-based catalyst; the removal rate of NO in reacted tail gas is more than 60%. The method disclosed by the invention is simple and low in cost, conforms to working conditions of actual application, and solves the problem that NH3 in NH3-SCR is difficult to convey. The method can be directly used for denitration of phosphorus chemical enterprise industrial parks and other enterprises, so that a pollutant hydrogen phosphide gas can be utilized, waste materials are changed into things of value, and recycling is achieved; the reaction temperature is lower than that of a conventional treatment method, so that energy sources are saved; a conflict with the agriculture caused by excessive liquid ammonia or urea consumption is avoided.
Description
Technical field
The present invention relates to atmospheric pollution purification techniques field, specifically a kind of PH3The method of selectivity low-temperature catalyzed reduction NO.
Background technology
Nitrogen oxides (wherein NO accounts for more than 90%) is one of main atmosphere pollution. It may result in the destruction of photochemical fog and ozone layer or an important precursor source of formation PM2.5, the health of the serious harm mankind. Therefore, NO is removedxHave become as important topic in field of Environment Protection.
The NO removed at presentxEffective technology is NH3Selective Catalytic Reduction of NO (NH3-SCR) technology. But, this technology will consume substantial amounts of NH3. And liquefied ammonia or carbamide are the important component of agrochemical, too much consumption carbamide or ammonia will cause agrochemical yield to reduce, and cause that agricultural output declines. Liquefied ammonia or urea production and NO is synthesized according to China's yearxGrowing amount calculates, and NO is removed in the whole nationxCan consume 10% year production ammonium salt, so will be formed and strive the situation of grain with agricultural. At NH3In the system of-SCR, generally add equivalent or excessive NH3, cause NH3Directly escape in air, bring secondary pollution. And this reaction can generate ammonium salt/nitrous acid ammonium salt, not only result in catalysqt deactivation, it is also possible to blast, cause potential safety hazard. Additionally, ammonia transport inconvenience, easily cause potential safety hazard. Therefore, new removal NO is developedxTechnical method be imperative.
Hydrogen phosphide (PH3) can be prepared with high alkali liquid by elemental phosphorous, utilize PH3Replace NH3, Selective Catalytic Reduction of NO is a kind of practicable method. Having not yet to see bibliographical information, the method is simple, has the prospect of commercial Application.
Summary of the invention
It is an object of the invention to provide a kind of PH3The method of selectivity low-temperature catalyzed reduction NO, utilizes PH3The reproducibility of gas, with PH3For reducing agent, Reduction of NO under absorbent charcoal based catalyst existence condition, the method is invested, operating cost is low, it is easy to industrial applications.
Reaction temperature 50-120 DEG C of the inventive method catalysis reduction, the flue gas containing NO after desulfurizing tower desulfurization can directly utilize PH3Gas and catalyst reduction NO, or utilize plant gas waste heat to carry out catalysis reduction again after need to processing flue gas.
The concentration range of described NO is 100-600ppm, PH3With NO concentration than for 0.6-1.2.
The reaction equation of the method is.
Described absorbent charcoal based catalyst is to be placed in by activated carbon in the nitrate solution that concentration is 0.01-5mol/L, at 60-70 DEG C after ultrasonic 2-8h, is placed at 105 DEG C and dries 8-24h, and finally at 300-450 DEG C, roasting 3-5h prepares; Wherein nitrate is cobalt nitrate, manganese nitrate, one or more mixture in ferric nitrate, cerous nitrate, copper nitrate, zirconium nitrate, nickel nitrate, Lanthanum (III) nitrate.
The present invention is directed to Problems existing in above-mentioned treatment technology, adopt PH3Selectivity low-temperature catalyzed reduction NO method removes NO, and NO clearance is up to more than 60%, provides a simple approach for industrial waste gas purifying NO.
The PH of remaining after reaction3Phosphoric acid can be prepared by prior art purification, accomplish to turn waste into wealth, not produce secondary pollution, as adopted method in patent CN101318124A, CN1345619A and CN1398658A.
The P produced in reaction2O5Phosphoric acid can be prepared, as with reference to method in patent CN101732962A and CN101690866A by related art method.
Compared to the prior art, the present invention has the following advantages:
1, method is simple, cost is low, meets the operating mode of practical application;
2, NH is solved3NH in-SCR3The problem not easily transported;
3, the method can be directly used for other enterprise's denitration of phosphorous chemical industry enterprise industrial zone so that pollutant phosphine gas can be utilized, and turns waste into wealth, and reaches recycling;
4, reaction temperature is lower than conventional treatment method, saves the energy, at NH3In-SCR system, reaction temperature is generally 300-400 DEG C, need to consume the substantial amounts of energy to maintain pyroreaction, cause that operating cost strengthens; The method does not need additionally to consume the energy, and to reacted product (PH3And P2O5) can also be reclaimed, prepare phosphoric acid;
5, avoid too much causing and striving the situation of grain with agricultural because consuming liquefied ammonia or carbamide.
Accompanying drawing explanation
Fig. 1 is one-level denitrification apparatus NO removal efficiency result schematic diagram of the present invention;
Fig. 2 is one-level denitrification apparatus NO removal efficiency result schematic diagram of the present invention;
Fig. 3 is one-level denitrification apparatus NO removal efficiency result schematic diagram of the present invention;
Fig. 4 is two grades of denitrification apparatus NO removal efficiency result schematic diagrams of the present invention;
Fig. 5 is one-level denitrification apparatus NO removal efficiency result schematic diagram of the present invention;
Fig. 6 is one-level denitrification apparatus NO removal efficiency result schematic diagram of the present invention;
Fig. 7 is the embodiment of the present invention 6 method flow schematic diagram;
Fig. 8 is the embodiment of the present invention 7 method flow schematic diagram.
Specific embodiments
Below by drawings and Examples, the present invention is described in further detail, but scope is not limited to described content.
Embodiment 1: this PH3The method of selectivity low-temperature catalyzed reduction NO, particular content is as follows:
Considering to be actually needed, before entering denitrification apparatus, the EGT containing NO is generally 60-80 DEG C, and the laboratory simulation flue gas containing 100ppmNO presses NO and PH simultaneously3Concentration ratio is 1 addition PH3Gas, the oxygen of 5%, N2As Balance Air, with PH3For reducing agent, Reduction of NO on absorbent charcoal based catalyst, wherein absorbent charcoal based catalyst is to be placed in by activated carbon in the nitrate solution (cobalt nitrate and nickel nitrate 1:1 in mass ratio mixing) that concentration is 0.1mol/L, at 60 DEG C after ultrasonic 5h, being placed at 105 DEG C and dry 15h, finally at 300 DEG C, roasting 5h prepares; The clearance of NO such as table 1:
Table 1
��
Embodiment 2: this PH3The method of selectivity low-temperature catalyzed reduction NO, particular content is as follows:
Considering to be actually needed, before entering denitrification apparatus, the EGT containing NO is generally 60-80 DEG C, and the laboratory simulation flue gas containing 600ppmNO presses NO and PH simultaneously3Concentration ratio is 0.6 addition PH3Gas, the oxygen of 2%, N2As Balance Air, with PH3For reducing agent, Reduction of NO on absorbent charcoal based catalyst, wherein absorbent charcoal based catalyst is to be placed in by activated carbon in nitrate (ferric nitrate and the copper nitrate 3:1 in mass ratio mixing) solution that concentration is 0.4mol/L, at 60 DEG C after ultrasonic 8h, being placed at 105 DEG C and dry 20h, finally at 350 DEG C, roasting 4h prepares; The clearance of NO such as table 2:
Table 2
��
Embodiment 3: this PH3The method of selectivity low-temperature catalyzed reduction NO, particular content is as follows:
Considering to be actually needed, before entering denitrification apparatus, the EGT containing NO is generally 60-80 DEG C, and the laboratory simulation flue gas containing 400ppmNO presses NO and PH simultaneously3Concentration ratio is 1.2 addition PH3Gas, the oxygen of 10%, N2As Balance Air, with PH3For reducing agent, Reduction of NO on absorbent charcoal based catalyst, wherein absorbent charcoal based catalyst is to be placed in by activated carbon in nitrate (zirconium nitrate and the copper nitrate 2:1 in mass ratio mixing) solution that concentration is 1mol/L, at 65 DEG C after ultrasonic 3h, it is placed at 105 DEG C and dries 24h, finally at 400 DEG C, roasting 4h prepares, and the clearance of NO is shown in Fig. 1.
Embodiment 4: this PH3The method of selectivity low-temperature catalyzed reduction NO, particular content is as follows:
Considering to be actually needed, before entering denitrification apparatus, the EGT containing NO is generally 60-80 DEG C, and the laboratory simulation flue gas containing 400ppmNO presses NO and PH simultaneously3Concentration ratio is 1.2 addition PH3Gas, the oxygen of 5%, N2As Balance Air, with PH3For reducing agent, Reduction of NO on absorbent charcoal based catalyst, wherein absorbent charcoal based catalyst is to be placed in by activated carbon in the nitrate solution (the ratio mixing of manganese nitrate and ferric nitrate 1:2 in mass ratio) that concentration is 3mol/L, at 70 DEG C after ultrasonic 2h, being placed at 105 DEG C and dry 8h, finally at 450 DEG C, roasting 3h prepares; When flue-gas temperature is 80 DEG C, the clearance of NO is shown in Fig. 2 up to 53%().
Embodiment 5: this PH3The method of selectivity low-temperature catalyzed reduction NO, particular content is as follows:
Considering to be actually needed, before entering denitrification apparatus, the EGT containing NO is generally 60-80 DEG C, and the laboratory simulation flue gas containing 500ppmNO presses NO and PH simultaneously3Concentration ratio is 0.8 addition PH3Gas, the oxygen of 1%, N2As Balance Air, with PH3For reducing agent, Reduction of NO on absorbent charcoal based catalyst, wherein absorbent charcoal based catalyst is to be placed in by activated carbon in the nitrate solution (the ratio mixing of nickel nitrate and Lanthanum (III) nitrate 2:1 in mass ratio) that concentration is 4mol/L, at 60 DEG C after ultrasonic 8h, being placed at 105 DEG C and dry 15h, finally at 400 DEG C, roasting 5h prepares; When flue-gas temperature is 80 DEG C, the clearance of NO is shown in Fig. 3 up to 51%().
Embodiment 6: this PH3The method of selectivity low-temperature catalyzed reduction NO, particular content is as follows:
The laboratory simulation flue gas containing 300ppmNO, presses NO and PH simultaneously3Concentration ratio is 0.7 addition PH3Gas, the oxygen of 10%, N2As Balance Air, with PH3For reducing agent, Reduction of NO on absorbent charcoal based catalyst, wherein absorbent charcoal based catalyst is to be placed in by activated carbon in the nitrate solution (the ratio mixing of nickel nitrate, Lanthanum (III) nitrate, copper nitrate 1:1:1 in mass ratio) that concentration is 1mol/L, at 60 DEG C after ultrasonic 8h, being placed at 105 DEG C and dry 10h, finally at 350 DEG C, roasting 5h prepares. After denitrification apparatus, flue gas still contains a small amount of PH3With NO gas, then to PH3Tail gas purifies, and the tail gas containing NO after process is re-added in denitrification apparatus, and so, gas completes the removal to NO in an airtight waste gas purification process, does not produce secondary pollution, and flow chart is shown in clearance such as table 3 of Fig. 7, NO:
Table 3
��
Embodiment 7
The laboratory simulation flue gas containing 400ppmNO, presses NO and PH simultaneously3Concentration ratio is 0.9 addition PH3Gas, the oxygen of 5%, N2As Balance Air, with PH3For reducing agent, Reduction of NO on absorbent charcoal based catalyst, wherein absorbent charcoal based catalyst is to be placed in by activated carbon in the nitrate solution (the ratio mixing of manganese nitrate, ferric nitrate, cerous nitrate 1:1:1 in mass ratio) that concentration is 2mol/L, at 60 DEG C after ultrasonic 8h, being placed at 105 DEG C and dry 10h, finally at 350 DEG C, roasting 5h prepares; Reaction temperature is 70 DEG C, after one-level denitrification apparatus, still contains part PH in flue gas3With NO gas, then these gas by two grades of denitrification apparatus, NO clearance is up to 75%, but still contains part PH in gas3(such as Fig. 4, shown in 8). Again to PH3Purified treatment prepares phosphoric acid, and the tail gas after process just can enter a purification process.
Embodiment 8
The laboratory simulation flue gas containing 400ppmNO, presses NO and PH simultaneously3Concentration specific concentration ratio is 1 addition PH3Gas, the oxygen of 5%, N2As Balance Air, with PH3For reducing agent Reduction of NO on absorbent charcoal based catalyst, wherein absorbent charcoal based catalyst is to be placed in by activated carbon in the nitrate solution (the ratio mixing of nickel nitrate and cobalt nitrate 2:1 in mass ratio) that concentration is 2mol/L, at 60 DEG C after ultrasonic 8h, being placed at 105 DEG C and dry 15h, finally at 400 DEG C, roasting 5h prepares; When flue-gas temperature is 50 DEG C, the clearance that the response time is 180min, NO is shown in Fig. 5.
Embodiment 9
The laboratory simulation flue gas containing 400ppmNO, presses NO and PH simultaneously3Concentration specific concentration is than for adding PH3Gas, the oxygen of 5%, N2As Balance Air, with PH3For reducing agent Reduction of NO on absorbent charcoal based catalyst, wherein absorbent charcoal based catalyst is to be placed in by activated carbon in the nitrate solution (the ratio mixing of nickel nitrate, cobalt nitrate and ferric nitrate 1:1:1 in mass ratio) that concentration is 1mol/L, at 60 DEG C after ultrasonic 8h, being placed at 105 DEG C and dry 15h, finally at 400 DEG C, roasting 5h prepares; When flue-gas temperature is 120 DEG C, the clearance that the response time is 180min, NO is shown in Fig. 6.
Claims (5)
1. a PH3The method of selectivity low-temperature catalyzed reduction NO, it is characterised in that: with PH3For reducing agent, Reduction of NO under absorbent charcoal based catalyst existence condition.
2. PH according to claim 13The method of selectivity low-temperature catalyzed reduction NO, it is characterised in that: the concentration of NO is 100-600ppm, NO and PH3Concentration is than for 0.6-1.2.
3. PH according to claim 1 and 23The method of selectivity low-temperature catalyzed reduction NO, it is characterised in that: reaction temperature 50-120 DEG C of catalysis reduction.
4. PH according to claim 33The method of selectivity low-temperature catalyzed reduction NO, it is characterized in that: absorbent charcoal based catalyst is to be placed in by activated carbon in the nitrate solution that concentration is 0.01-5mol/L, at 60-70 DEG C after ultrasonic 2-8h, being placed at 105 DEG C and dry 8-24h, finally at 300-450 DEG C, roasting 3-5h prepares.
5. PH according to claim 43The method of selectivity low-temperature catalyzed reduction NO, it is characterised in that: nitrate is cobalt nitrate, manganese nitrate, one or more mixture in ferric nitrate, cerous nitrate, copper nitrate, zirconium nitrate, nickel nitrate, Lanthanum (III) nitrate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610001895.XA CN105617857B (en) | 2016-01-06 | 2016-01-06 | A kind of PH3The low-temperature catalyzed reduction NO of selectivity method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610001895.XA CN105617857B (en) | 2016-01-06 | 2016-01-06 | A kind of PH3The low-temperature catalyzed reduction NO of selectivity method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105617857A true CN105617857A (en) | 2016-06-01 |
| CN105617857B CN105617857B (en) | 2017-12-01 |
Family
ID=56033434
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610001895.XA Active CN105617857B (en) | 2016-01-06 | 2016-01-06 | A kind of PH3The low-temperature catalyzed reduction NO of selectivity method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105617857B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111228980A (en) * | 2020-03-10 | 2020-06-05 | 昆明理工大学 | Method for combined removal of phosphorus, sulfur, cyanogen and nitrogen oxide in waste gas |
| CN111495377A (en) * | 2020-05-27 | 2020-08-07 | 河南城建学院 | PH based on agricultural waste biochar catalyst3Method for selective low-temperature catalytic reduction of N0 |
| CN112371126A (en) * | 2020-11-27 | 2021-02-19 | 昆明理工大学 | Low-temperature CO-SCR denitration Cu-Fe/AC catalyst and preparation method and application thereof |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1208361A (en) * | 1995-12-13 | 1999-02-17 | Basf公司 | Process for reducing NOx from exhaust fumes |
| JP2010149097A (en) * | 2008-12-26 | 2010-07-08 | Tanaka Kikinzoku Kogyo Kk | Catalyst and method for cleaning exhaust gas |
| CN103055694A (en) * | 2011-10-21 | 2013-04-24 | 中国石油化工股份有限公司 | Method for flue gas denitrification by organic waste gas |
| US8617497B2 (en) * | 2010-04-20 | 2013-12-31 | Umicore Ag & Co. Kg | Mixed oxide materials for the selective catalytic reduction of nitrogen oxides in exhaust gases |
-
2016
- 2016-01-06 CN CN201610001895.XA patent/CN105617857B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1208361A (en) * | 1995-12-13 | 1999-02-17 | Basf公司 | Process for reducing NOx from exhaust fumes |
| JP2010149097A (en) * | 2008-12-26 | 2010-07-08 | Tanaka Kikinzoku Kogyo Kk | Catalyst and method for cleaning exhaust gas |
| US8617497B2 (en) * | 2010-04-20 | 2013-12-31 | Umicore Ag & Co. Kg | Mixed oxide materials for the selective catalytic reduction of nitrogen oxides in exhaust gases |
| CN103055694A (en) * | 2011-10-21 | 2013-04-24 | 中国石油化工股份有限公司 | Method for flue gas denitrification by organic waste gas |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111228980A (en) * | 2020-03-10 | 2020-06-05 | 昆明理工大学 | Method for combined removal of phosphorus, sulfur, cyanogen and nitrogen oxide in waste gas |
| CN111495377A (en) * | 2020-05-27 | 2020-08-07 | 河南城建学院 | PH based on agricultural waste biochar catalyst3Method for selective low-temperature catalytic reduction of N0 |
| CN112371126A (en) * | 2020-11-27 | 2021-02-19 | 昆明理工大学 | Low-temperature CO-SCR denitration Cu-Fe/AC catalyst and preparation method and application thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105617857B (en) | 2017-12-01 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103463978B (en) | Based on the device and method of catalytic oxidation of hydrogen peroxide flue gas and desulfurizing and denitrifying | |
| CN101810996B (en) | Method for producing ammonium sulfate and ammonium nitrate by simultaneously desulfurizing and denitrating ammonia water and cobaltic ethylenediamine (II) | |
| CN103212281A (en) | Smoke desulfurization and denitrification integration method and special device thereof | |
| CN102078752A (en) | Method for preparing sodium nitrite from nitric oxide waste gas through multistage oxidation absorption | |
| CN105536886B (en) | A kind of regeneration method of arsenic poisoning denitrating catalyst | |
| ES2573717B1 (en) | Procedure for the production of organic urea as well as organic urea and AUS32 obtained by this procedure | |
| CN102580525A (en) | Method for using activated carbon load copper oxide composite catalyst to absorb nitrogenous oxide | |
| CN106955589B (en) | Boiler flue gas simultaneous desulfurization and denitrification device | |
| CN106237851A (en) | A kind of utilize ozone to carry out SCR denitration to carry the System and method for of effect | |
| Zhang et al. | Effects of slurry properties on simultaneous removal of SO2 and NO by ammonia-Fe (II) EDTA absorption in sintering plants | |
| CN105617857A (en) | Method for performing selective low-temperature catalytic reduction on NO by use of PH3 | |
| CN102836636A (en) | Desulfurization denitration composition, preparation method and application thereof | |
| CN102794098A (en) | Flue gas wet-type oxidation denitration and resource utilization method | |
| CN104190226B (en) | Complexing absorption and aerobic denitrification combined smoke denitration process | |
| CN102188889A (en) | Device and method for combined removal of sulphur dioxide (SO2), nitrogen oxide (NOX) and mercury from fume | |
| CN105771652A (en) | Flue gas denitration method by taking manganese oxide as cyclic absorption medium | |
| CN101732960A (en) | Device for filtering and removing nitric oxides in ozone-oxidizing and combining organisms and method thereof | |
| CN101920166B (en) | Denitration method for desulfurization postposition | |
| CN103230743A (en) | Nitrogen oxide tail gas emission reduction method | |
| CN202590630U (en) | Coal-fired boiler low-temperature selective catalytic reduction (SCR) fixed bed smoke denitration device | |
| CN113546514B (en) | Low-temperature liquid desulfurizing agent in cement kiln | |
| CN204093282U (en) | A kind for the treatment of apparatus utilizing ozonization to remove nitrogen oxide | |
| CN102836634A (en) | Desulfurization denitration method | |
| CN105214463A (en) | A kind of processing method of aliphatic hydroxyl sulphonate water reducer process gas | |
| CN215276565U (en) | Plasma system for ammonia-containing waste gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |