CN106076112A - One removes N simultaneously2o and NOxmethod - Google Patents

One removes N simultaneously2o and NOxmethod Download PDF

Info

Publication number
CN106076112A
CN106076112A CN201610393208.3A CN201610393208A CN106076112A CN 106076112 A CN106076112 A CN 106076112A CN 201610393208 A CN201610393208 A CN 201610393208A CN 106076112 A CN106076112 A CN 106076112A
Authority
CN
China
Prior art keywords
remove
reactor
flow
vital energy
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.)
Granted
Application number
CN201610393208.3A
Other languages
Chinese (zh)
Other versions
CN106076112B (en
Inventor
李伟
雷军
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
HAISO TECHNOLOGY CO LTD
Yangquan Coal Industry Group Chemical Co ltd
Original Assignee
HAISO TECHNOLOGY CO LTD
Yangquan Coal Industry Group Chemical Co ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by HAISO TECHNOLOGY CO LTD, Yangquan Coal Industry Group Chemical Co ltd filed Critical HAISO TECHNOLOGY CO LTD
Priority to CN201610393208.3A priority Critical patent/CN106076112B/en
Publication of CN106076112A publication Critical patent/CN106076112A/en
Application granted granted Critical
Publication of CN106076112B publication Critical patent/CN106076112B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

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
    • B01D53/8628—Processes characterised by a specific catalyst
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/002—Mixed oxides other than spinels, e.g. perovskite
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
    • B01J23/8926—Copper and noble metals
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
    • B01J23/8933—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/8953—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with zinc, cadmium or mercury
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
    • B01J23/8933—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/898—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with vanadium, tantalum, niobium or polonium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2523/00—Constitutive chemical elements of heterogeneous catalysts
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/10—Capture or disposal of greenhouse gases of nitrous oxide (N2O)

Abstract

The present invention relates to one and remove N simultaneously2O and NOxMethod.The method is: to containing N2O and NOxPlace regulate the flow of vital energy in fill into NH3And air；Enter one under the conditions of 200～600 DEG C and can integrally remove N2O and NOxExtraordinary beds, carry out the N in regulating the flow of vital energy in place2O and NOxWhile remove, wherein: place regulate the flow of vital energy in N2O is N by catalytic decomposition2And O2, NOxWith the NH added under catalyst action3Reaction generates N2；Described one removing N2O and NOxCatalyst by mass percentage, in finished catalyst, noble metal accounts for 0.1%～5%, transition metal oxide accounts for 3%～15%, and alkali metal hydroxide accounts for 0.5%～1%, and surplus is alumina support.Before comparing, commonly used combining removes N2O and NOxMethod in be respectively adopted different catalysts removing N2O and NOx, this patent uses and removes N simultaneously2O and NOxMethod, technique is simple, and equipment investment is saved, and operation simplifies, can be by N under the lower temperature of 200～600 DEG C2O and NOxRemove, removal efficiency ＞ 95% simultaneously.

Description

One removes N simultaneously2O and NOxMethod
Technical field
The present invention relates to remove N2O and NOxTechnical field, particularly relate to one and remove N simultaneously2O and NOxMethod.
Background technology
The production processes such as nitric acid, fatty acid, caprolactam, acrylonitrile, oxalic acid Arrcostab generally produce nitrogen oxides give up Gas, mainly comprises N2O、NO、NO2、N2O3、N2O4, wherein N2O is a kind of colourless pleasantly sweet gas, has anesthetic action, is also called Laughing gas, has greenhouse effect concurrently and to depletion of the ozone layer effect, N2O causes the potentiality of global warming to compare CO2Exceed 310 times, at present N in air2The concentration of O is about 310nmol/mol, and with annual 0.2～about 0.3% speed increase, its development trend pair Human residential environment constitutes the biggest threat, is also one of gas of clear stipulaties limit row in Kyodo Protocol book.
NOxDirectly it is detrimental to health, causes lung damage, central nervous system is impacted, in atmosphere can simultaneously Generating photochemical fog, this toxic smog greatly endangers healthy, destroys ecological environment.NOxRemoving mainly have choosing Selecting property non-catalytic reduction (SNCR) and SCR (SCR), SNCR reaction temperature is higher, and denitration precision is the highest, therefore one As use SCR, reducing agent is typically chosen NH3、H2, methane etc..
It is generally directed to N2O and NOxRemoving, it is contemplated that according to N2O and NOxHeterogeneity be respectively adopted different catalysts Remove respectively, such as N2O uses catalytic decomposition catalyst, NOxUse denitrating catalyst by adding reducing agent selective catalysis also Former, but technique is more complicated, and equipment and material investment are big, remove N in currently available technology the most simultaneously2O and NOxMethod report.
Summary of the invention:
The technical problem to be solved is for the deficiencies in the prior art, it is provided that one removes N simultaneously2O and NOx Method.
For solving above-mentioned technical problem, the present invention adopts the following technical scheme that
One removes N simultaneously2O and NOxMethod, it is characterised in that: to containing N2O and NOxPlace regulate the flow of vital energy in fill into NH3With Air；Enter one under the conditions of 200～600 DEG C and can integrally remove N2O and NOxExtraordinary beds, carry out during place regulates the flow of vital energy N2O and NOxWhile remove, wherein: place regulate the flow of vital energy in N2O is N by catalytic decomposition2And O2, NOxUnder catalyst action and add NH3Reaction generates N2；Described one removing N2O and NOxCatalyst by mass percentage, noble metal in finished catalyst Account for 0.1%～5%, transition metal oxide accounts for 3%～15%, and alkali metal hydroxide accounts for 0.5%～1%, and surplus is oxidation Alumina supporter.
By such scheme, noble metal is one or more in palladium, platinum, rhodium, ruthenium, and transition metal oxide is five oxidations two In vanadium, copper oxide, cobalt black, zinc oxide any two kinds or more than.
By such scheme, described alkali metal hydroxide is one or both the group in sodium hydroxide, potassium hydroxide Close.
By such scheme, described containing N2O and NOxPlace regulate the flow of vital energy middle NOxVolumn concentration be 0.1～20%, N2O Volumn concentration be 0.1～50%.
By such scheme, in said method, will be containing N2O and NOxPlace regulate the flow of vital energy and add air and NH3After, after heating up Entrance is filled with the reactor of beds and reacts, by reactor inlet cold air and previous reaction exit gas heat exchange Rear entrance is filled with the reactor of beds and carries out reacting and remove NO simultaneouslyxAnd N2O, after then reacting, gas is discharged.
By such scheme, the tolerance being entered the reactor outlet gas in heat exchanger and entrance cold air by regulation is adjusted Reaction temperature in joint reactor.
By such scheme, according to outlet N in course of reaction2O and NOxReaction temperature in content regulation and control reactor.
By such scheme, N after reaction2O and NOxThe equal ＞ of removal efficiency 95%.
By such scheme, containing N2O and NOxPlace regulate the flow of vital energy entrance reactor before need to fill into air and a certain amount of NH3, And ensure mix homogeneously, the NH filled into3Regulate the flow of vital energy middle NO with placexVolume ratio be 1.0～1.2:1.
By such scheme, in reactor, the air speed of catalytic reaction is 3000～20000h-1；Reactor is carried out react time control Pressure 0.01MPa～2MPa of reaction system processed.
Above-mentioned one removing N2O and NOxThe preparation method of catalyst, it is characterised in that: preparation process is as follows:
(1) dipping: by salt corresponding for transition metal oxide wiring solution-forming in proportion, on equivalent impregnation to alumina support (equivalent implication is: the amount of solution of preparation and the adsorbable amount of solution of alumina support are equal)；
(2) dry: the alumina support after dipping dries in the shade post-drying；
(3) roasting: the semi-finished product after drying, through roasting, make transition metal salt be decomposed into the metal-oxide of correspondence；
(4) double-steeping: after the semi-finished product natural cooling after roasting, by precious metal salt wiring solution-forming, equivalent impregnation arrives On the carrier of step (3)；
(5) noble metal: the carrier after dipping noble metal processes your gold making to be impregnated on carrier through liquid-phase reduction Belong to salt and be reduced to the noble metal of zero-valent state；
(6) secondary drying: the semi-finished product of liquid-phase reduction are dried；
(7) three dippings: by alkali metal hydroxide wiring solution-forming, on the carrier of equivalent impregnation to step (6)；
Dry for (8) three times: the semi-finished product of step (7) are dried, and obtain and remove N simultaneously2O and NOxCatalyst.
By such scheme, time in step (1) by salt corresponding for transition metal oxide wiring solution-forming in proportion, according to salt Physico-chemical property adds ammonia or acetic acid as cosolvent.
By such scheme, time in step (4) by precious metal salt wiring solution-forming, add salt according to the physico-chemical property of precious metal salt Acid cosolvent.
It is hot air dries by the drying in such scheme, step (2) or step (6) or step (8), dries temperature 110 ～130 DEG C.
By such scheme, the sintering temperature of step (3) is 350～550 DEG C.
By such scheme, reducing agent used by the liquid-phase reduction in described step (5) is formaldehyde, ascorbic acid, ortho phosphorous acid One in sodium, potassium borohydride.
Remove N simultaneously2O and NOxMethod subtractive process in occur main chemical reactions equation be:
2N2O==2N2+O2 (1)
4NO+4NH3+O2==4N2+6H2O (2)
2NO2+4NH3+O2==3N2+6H2O (3)
6NO2+8NH3==7N2+12H2O (4)
The main efficacy results of this patent is:
Before comparing, commonly used combining removes N2O and NOxMethod in be respectively adopted different catalysts removing N2O and NOx, this patent uses and removes N simultaneously2O and NOxMethod, technique is simple, and equipment investment is saved, and operation simplifies, can 200～ By N under the lower temperature of 600 DEG C2O and NOxRemove, removal efficiency ＞ 95% simultaneously.Can be used for nitric acid, fatty acid, caprolactam, third In the chemical process such as alkene nitrile, oxalic acid Arrcostab produce containing N2O and NOx(NOxRefer to without N2The nitrogen oxides of O) tail gas Process.
Accompanying drawing explanation
Fig. 1 is the reaction process schematic diagram of the present invention.
Detailed description of the invention
The summary of the invention of the present invention is further illustrated below with example.
The preparation of catalyst sample:
Embodiment 1:
Catalyst is produced by following preparation technology
(1) dipping: 10 grams of ammonium metavanadates and 5 grams of cobalt oxalates are joined 60 milliliters of volume ratios is in 1:10 ammonia spirit, Dissolving completely, solution even is impregnated on 100 grams of alumina supports.
(2) dry: the alumina support after dipping dry in the shade after through 120 DEG C of hot air dries.
(3) roasting: the semi-finished product after drying, through 550 DEG C of roastings, make salt fully decompose.
(4) 1.6 grams of Palladous chloride .s are dissolved into 60 milliliters of volumes by double-steeping: after the semi-finished product natural cooling after roasting Than in 1:10 hydrochloric acid solution, dissolving completely, solution even is impregnated on the carrier of step (3).
(5) noble metal: the carrier after dipping noble metal makees reducing agent with potassium borohydride to be made through liquid-phase reduction process The precious metal salt being impregnated on carrier is reduced to the palladium of zero-valent state.
(6) semi-finished product in step (5) are through 120 DEG C of hot air dries.
(7) three dippings: 0.9 gram of sodium hydroxide is dissolved into wiring solution-forming in 60 milliliters of water, equivalent impregnation to step (6) Carrier on.
Dry for (8) three times: the semi-finished product of step (7) are through 120 DEG C of hot air dries.
Make one through above 8 steps and remove N simultaneously2O and NOxCatalyst 1.
Embodiment 2:
Catalyst is produced by following preparation technology
(1) dipping: 14 gram of one water acetic acid copper and 8 grams of zinc acetate dihydrates are joined 60 milliliters of volume ratios is that 1:10 acetic acid is molten In liquid, dissolving completely, solution even is impregnated on 100 grams of alumina supports.
(2) dry: the alumina support after dipping dry in the shade after through 120 DEG C of hot air dries.
(3) roasting: the semi-finished product after drying, through 450 DEG C of roastings, make salt fully decompose.
(4) 5.2 grams of chloroplatinic acids are dissolved into 60 milliliters of volumes by double-steeping: after the semi-finished product natural cooling after roasting Than in 1:10 hydrochloric acid solution, dissolving completely, solution even is impregnated on the carrier of step (3).
(5) noble metal: the carrier after dipping noble metal is made reducing agent with sodium hypophosphite and processed through liquid-phase reduction The precious metal salt being impregnated on carrier is made to be reduced to the palladium of zero-valent state.
(6) semi-finished product in step (5) are through 120 DEG C of hot air dries.
(7) three dippings: 0.7 gram of sodium hydroxide is dissolved into wiring solution-forming in 60 milliliters of water, equivalent impregnation to step (6) Carrier on.
Dry for (8) three times: the semi-finished product of step (7) are through 120 DEG C of hot air dries.
Make one through above 8 steps and remove N simultaneously2O and NOxCatalyst 2.
Embodiment 3:
Catalyst is produced by following preparation technology
(1) dipping: 6 grams of ammonium metavanadates and 3.5 grams of Schweinfurt greens are joined 60 milliliters of volume ratios is in 1:10 ammonia spirit, Dissolving completely, solution even is impregnated on 100 grams of alumina supports.
(2) dry: the alumina support after dipping dry in the shade after through 120 DEG C of hot air dries.
(3) roasting: the semi-finished product after drying, through 550 DEG C of roastings, make salt fully decompose.
(4) 13.7 grams of rhodium nitrates are dissolved into 60 milliliters of water by double-steeping: after the semi-finished product natural cooling after roasting In, dissolving completely, solution even is impregnated on the carrier of step (3).
(5) noble metal: the carrier after dipping noble metal makees reducing agent with ascorbic acid to be made through liquid-phase reduction process The precious metal salt being impregnated on carrier is reduced to the palladium of zero-valent state.
(6) semi-finished product in step (5) are through 120 DEG C of hot air dries.
(7) three dippings: 1 gram of potassium hydroxide is dissolved into wiring solution-forming in 60 milliliters of water, equivalent impregnation to step (6) On carrier.
Dry for (8) three times: the semi-finished product of step (7) are through 120 DEG C of hot air dries.
Make one through above 8 steps and remove N simultaneously2O and NOxCatalyst 3.
Embodiment 4:
Catalyst is produced by following preparation technology
(1) dipping: 11 grams of Schweinfurt greens and 6 grams of cobalt oxalates are joined 60 milliliters of volume ratios is in 1:10 ammonia spirit, molten Solving completely, solution even is impregnated on 100 grams of alumina supports.
(2) dry: the alumina support after dipping dry in the shade after through 120 DEG C of hot air dries.
(3) roasting: the semi-finished product after drying, through 450 DEG C of roastings, make salt fully decompose.
(4) 1.5 grams of ruthenium hydrochloride ammoniums are dissolved into 60 milliliters of water by double-steeping: after the semi-finished product natural cooling after roasting In, dissolving completely, solution even is impregnated on the carrier of step (3).
(5) noble metal: the carrier after dipping noble metal makees reducing agent with formaldehyde makes dipping through liquid-phase reduction process Precious metal salt on carrier is reduced to the palladium of zero-valent state.
(6) semi-finished product in step (5) are through 120 DEG C of hot air dries.
(7) three dippings: 0.8 gram of potassium hydroxide is dissolved into wiring solution-forming in 60 milliliters of water, equivalent impregnation to step (6) Carrier on.
(8) secondary drying: the semi-finished product of step (7) are through 120 DEG C of hot air dries.
Make one through above 8 steps and remove N simultaneously2O and NOxCatalyst 4.
Above-mentioned catalyst is used for containing typical containing N2O and NOxThe process of synthesis tail gas, in following embodiment 5-7 The pressure 0.1～0.5MPa of reactor, the selection of pressure mainly to consider to overcome catalyst bed layer resistance, simultaneously maximum pressure Not above catalyst tolerance, the otherwise easy efflorescence of catalyst.Comparatively speaking, pressure is the biggest favourable to reaction, but overall shadow Ring less.
Embodiment 5:
Consist of N2O 0.2%, NO 0.14%, NO20.04%, O21.5%, N297%, H2O 1.27% typical case's nitre Acid tail gas 30000Nm3/ h, filling into flow is 59.4Nm3The NH of/h3With a small amount of air, mix homogeneously, by the heater liter that goes into operation Temperature, to 250 DEG C, enters and is filled with 3m3The reactor bed of extraordinary catalyst that this patent describes, by reactor outlet gas and Entrance cold air heat exchange, progressively closes the heater that goes into operation, and regulating heat exchanger tolerance to regulate temperature of reactor is 350 DEG C, instead Discharge to aiutage after answering device exit gas and entrance cold air heat exchange, as it is shown in figure 1, the removal effect of 4 catalyst samples It is shown in Table 1:
Table 1
。
Embodiment 6:
Consist of N2O 37.9%, NO 0.3%, N247.8%, O24.4%, CO29.5% typical case's adipic acid tail gas 50000Nm3/ h, filling into flow is 165Nm3The NH of/h3With a small amount of air, mix homogeneously, by going into operation, heater is warming up to 450 DEG C, enter and be filled with 10m3The reactor bed of the extraordinary catalyst that this patent describes, by cold to reactor outlet gas and entrance Gas converting heat, progressively closes the heater that goes into operation, and regulating heat exchanger tolerance to regulate temperature of reactor is 550 DEG C, and reactor goes out Discharging to aiutage after gas and entrance cold air heat exchange, the removal effect of 4 catalyst samples is shown in Table 2:
Table 2
Embodiment 7:
Consist of N2O 4%, NO 17.1%, N244.3%, O22.4%, CO 21.1%, CO20.8%, CH4 5.2%, the typical dimethyl oxalate. synthesis tail gas 4500Nm of 5.1% methanol3/ h, filling into flow is 846Nm3The NH of/h3On a small quantity Air, mix homogeneously, it is warming up to 350 DEG C by the heater that goes into operation, enters and be filled with 0.3m3The extraordinary catalyst that this patent describes Reactor bed, by reactor outlet gas and entrance cold air heat exchange, progressively close and go into operation heater, regulated heat exchanger It is 450 DEG C that tolerance regulates temperature of reactor, discharges to aiutage, 4 after reactor outlet gas and entrance cold air heat exchange The removal effect of catalyst sample is shown in Table 3:
Table 3
。

Claims (10)

1. one kind removes N simultaneously2O and NOxMethod, it is characterised in that: to containing N2O and NOxPlace regulate the flow of vital energy in fill into NH3And sky Gas；Enter one under the conditions of 200～600 DEG C and can integrally remove N2O and NOxExtraordinary beds, carry out during place regulates the flow of vital energy N2O and NOxWhile remove, wherein: place regulate the flow of vital energy in N2O is N by catalytic decomposition2And O2, NOxUnder catalyst action and add NH3Reaction generates N2；Described one removing N2O and NOxCatalyst by mass percentage, noble metal in finished catalyst Account for 0.1%～5%, transition metal oxide accounts for 3%～15%, and alkali metal hydroxide accounts for 0.5%～1%, and surplus is oxidation Alumina supporter.
The most according to claim 1 remove N simultaneously2O and NOxMethod, it is characterised in that: noble metal is palladium, platinum, rhodium, ruthenium In one or more, transition metal oxide is any two kinds in vanadic anhydride, copper oxide, cobalt black, zinc oxide More than or.
The most according to claim 1 remove N simultaneously2O and NOxMethod, it is characterised in that: described alkali metal hydroxide Thing is one or both the combination in sodium hydroxide, potassium hydroxide.
The most according to claim 1 remove N simultaneously2O and NOxMethod, it is characterised in that: described containing N2O and NOxPlace Regulate the flow of vital energy middle NOxVolumn concentration be 0.1～20%, N2The volumn concentration of O is 0.1～50%.
The most according to claim 1 remove N simultaneously2O and NOxMethod, it is characterised in that: will be containing N2O and NOxProcess Gas adds air and NH3After, enter after heating up and be filled with the reactor of beds and react, by reactor inlet Enter after cold air and previous reaction exit gas heat exchange and be filled with the reactor of beds and carry out reacting and remove NO simultaneouslyx And N2O, after then reacting, gas is discharged.
The most according to claim 1 remove N simultaneously2O and NOxMethod, it is characterised in that: by regulation enter heat exchanger In reactor outlet gas and the tolerance of entrance cold air regulate the reaction temperature in reactor.
The most according to claim 1 remove N simultaneously2O and NOxMethod, it is characterised in that: according to outlet in course of reaction N2O and NOxReaction temperature in content regulation and control reactor.
The most according to claim 1 remove N simultaneously2O and NOxMethod, it is characterised in that: N after reaction2O and NOxRemoval efficiency All ＞ 95%.
The most according to claim 1 remove N simultaneously2O and NOxMethod, it is characterised in that: containing N2O and NOxProcess Gas needs to fill into a certain amount of NH before entering reactor3And air, and ensure mix homogeneously, the NH filled into3Regulate the flow of vital energy middle NO with placex's Volume ratio is 1.0～1.2:1.
The most according to claim 1 remove N simultaneously2O and NOxMethod, it is characterised in that: catalytic reaction in reactor Air speed is 3000～20000h-1；Pressure 0.01MPa～2MPa of reaction system is controlled when reactor reacts.
CN201610393208.3A 2016-06-03 2016-06-03 It is a kind of to remove N simultaneously2O and NOxMethod Active CN106076112B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201610393208.3A CN106076112B (en) 2016-06-03 2016-06-03 It is a kind of to remove N simultaneously2O and NOxMethod

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201610393208.3A CN106076112B (en) 2016-06-03 2016-06-03 It is a kind of to remove N simultaneously2O and NOxMethod

Publications (2)

Publication Number Publication Date
CN106076112A true CN106076112A (en) 2016-11-09
CN106076112B CN106076112B (en) 2018-12-11

Family

ID=57448319

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201610393208.3A Active CN106076112B (en) 2016-06-03 2016-06-03 It is a kind of to remove N simultaneously2O and NOxMethod

Country Status (1)

Country Link
CN (1) CN106076112B (en)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108187656A (en) * 2017-12-30 2018-06-22 宁波高新区州致科技有限公司 It is a kind of for catalyst of flue gas and desulfurizing and denitrifying and preparation method thereof
CN108970395A (en) * 2018-07-30 2018-12-11 江苏科瑞工程设计有限公司 A kind of method of sulfuric acid apparatus removing NOx
CN111097285A (en) * 2018-10-29 2020-05-05 中国石油化工股份有限公司 Method for removing NOx by sulfuric acid device

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101480615A (en) * 2009-03-10 2009-07-15 北京化工大学 Catalyst for decomposing laughing gas and preparation method thereof
CN101530799A (en) * 2009-04-16 2009-09-16 上海纳米技术及应用国家工程研究中心有限公司 Nitrogen oxide catalyst-sorbent and preparation method
CN102574108A (en) * 2009-09-30 2012-07-11 祥明大学校产学协力团 Mixed metal oxide catalyst for decomposition of nitrogen oxides
CN102553573A (en) * 2011-12-29 2012-07-11 中国科学院过程工程研究所 Nitrogen oxide oxidizing catalyst and preparation method of nitrogen oxide oxidizing catalyst
CN102631933A (en) * 2011-02-14 2012-08-15 中国石油化工股份有限公司 Catalyst for removing NO in smoke and preparation method thereof
CN102658169A (en) * 2012-05-16 2012-09-12 北京化工大学 Composite catalyst for catalytic reduction of nitrogen oxide and preparation method and application of catalyst
CN103657632A (en) * 2013-11-27 2014-03-26 上海纳米技术及应用国家工程研究中心有限公司 Alkali liquor treated integral chrome oxide catalyst, preparation method and application
CN104841273A (en) * 2014-02-13 2015-08-19 韩国能源技术研究院 Method for simultaneously removing nitrous oxide and nitric oxide in exhaust gas of chemical plant by utilizing catalyst
CN105363451A (en) * 2015-12-04 2016-03-02 中国天辰工程有限公司 Efficient catalyst for decomposition of N2O and preparation method and application thereof

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101480615A (en) * 2009-03-10 2009-07-15 北京化工大学 Catalyst for decomposing laughing gas and preparation method thereof
CN101530799A (en) * 2009-04-16 2009-09-16 上海纳米技术及应用国家工程研究中心有限公司 Nitrogen oxide catalyst-sorbent and preparation method
CN102574108A (en) * 2009-09-30 2012-07-11 祥明大学校产学协力团 Mixed metal oxide catalyst for decomposition of nitrogen oxides
CN102631933A (en) * 2011-02-14 2012-08-15 中国石油化工股份有限公司 Catalyst for removing NO in smoke and preparation method thereof
CN102553573A (en) * 2011-12-29 2012-07-11 中国科学院过程工程研究所 Nitrogen oxide oxidizing catalyst and preparation method of nitrogen oxide oxidizing catalyst
CN102658169A (en) * 2012-05-16 2012-09-12 北京化工大学 Composite catalyst for catalytic reduction of nitrogen oxide and preparation method and application of catalyst
CN103657632A (en) * 2013-11-27 2014-03-26 上海纳米技术及应用国家工程研究中心有限公司 Alkali liquor treated integral chrome oxide catalyst, preparation method and application
CN104841273A (en) * 2014-02-13 2015-08-19 韩国能源技术研究院 Method for simultaneously removing nitrous oxide and nitric oxide in exhaust gas of chemical plant by utilizing catalyst
CN105363451A (en) * 2015-12-04 2016-03-02 中国天辰工程有限公司 Efficient catalyst for decomposition of N2O and preparation method and application thereof

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108187656A (en) * 2017-12-30 2018-06-22 宁波高新区州致科技有限公司 It is a kind of for catalyst of flue gas and desulfurizing and denitrifying and preparation method thereof
CN108970395A (en) * 2018-07-30 2018-12-11 江苏科瑞工程设计有限公司 A kind of method of sulfuric acid apparatus removing NOx
CN111097285A (en) * 2018-10-29 2020-05-05 中国石油化工股份有限公司 Method for removing NOx by sulfuric acid device

Also Published As

Publication number Publication date
CN106076112B (en) 2018-12-11

Similar Documents

Publication Publication Date Title
CN114669190B (en) Catalytic article for treating exhaust gas
US11331657B2 (en) Method of preparing catalyst for low-temperature synergistic catalytic purification of NOx and HCN in flue gas, and use thereof
CN101810996B (en) Method for producing ammonium sulfate and ammonium nitrate by simultaneously desulfurizing and denitrating ammonia water and cobaltic ethylenediamine (II)
CN106944130A (en) A kind of SCR AOC combination catalysts of purification of diesel tail gas and preparation method thereof
CN106902864A (en) A kind of ammoxidation catalyst for diesel engine vent gas cleaning system and preparation method thereof
JP2014020310A (en) Exhaust gas purifying apparatus
CN102580525A (en) Method for using activated carbon load copper oxide composite catalyst to absorb nitrogenous oxide
CN106076112B (en) It is a kind of to remove N simultaneously2O and NOxMethod
CN106000420B (en) One removing N2O and NOxCatalyst and preparation method thereof
US11179674B2 (en) Process for the removal of dinitrogen oxide in process off-gas
CN100363099C (en) CO low temperature oxidation catalyst and its preparation process
CN105396460B (en) High-efficiency combined removal of N2O and NOxMethod (2)
CN103041821A (en) Preparation method of low-temperature selective-reduction oxynitride catalyst
CN102631838A (en) Method for removing NO (nitric oxide) in flue gas
CN103894184B (en) A kind of high-specific surface area vanadium zinc system's modification denitrating catalyst and preparation method
CN111330437A (en) Method and system for cooperatively purifying multiple pollutants in adipic acid production
CN209476008U (en) A kind of low-temperature denitration of flue gas catalytic reaction system
CN104645983A (en) Catalyst for cycling gas purification in process for producing glyoxal by air oxidation of ethylene glycol as well as preparation method and application thereof
CN107198963A (en) The method and its device of a kind of efficient wet denitration
CN107233892B (en) For low-temperature catalyzed decomposition N2The composite oxide catalysts of O and its preparation
EP3917651A1 (en) Process for removing nitrogen oxides from a gas
CN100563830C (en) The environmental friendliness manufacture method of catalyst
CN110314648A (en) Preparation method, adsorbent and its regeneration method of nitrous oxide adsorbent
JPH09150039A (en) Apparatus and method for purifying exhaust gas
CN107185553A (en) A kind of catalysis oxidation at room temperature removes catalyst of formaldehyde and preparation method thereof

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