CN108786403A - A kind of Benitration reactor and denitration sulfur method - Google Patents
A kind of Benitration reactor and denitration sulfur method Download PDFInfo
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- CN108786403A CN108786403A CN201710299557.3A CN201710299557A CN108786403A CN 108786403 A CN108786403 A CN 108786403A CN 201710299557 A CN201710299557 A CN 201710299557A CN 108786403 A CN108786403 A CN 108786403A
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- 238000000034 method Methods 0.000 title claims abstract description 46
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 8
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 7
- 239000011593 sulfur Substances 0.000 title claims abstract description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 108
- 239000003546 flue gas Substances 0.000 claims abstract description 69
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 66
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 54
- 229910052751 metal Inorganic materials 0.000 claims abstract description 46
- 239000002184 metal Substances 0.000 claims abstract description 46
- 238000006243 chemical reaction Methods 0.000 claims abstract description 38
- 239000003054 catalyst Substances 0.000 claims abstract description 35
- 238000005507 spraying Methods 0.000 claims abstract description 32
- 239000008246 gaseous mixture Substances 0.000 claims abstract description 20
- 150000003863 ammonium salts Chemical class 0.000 claims abstract description 17
- 238000005406 washing Methods 0.000 claims abstract description 15
- 239000000428 dust Substances 0.000 claims abstract description 14
- 239000012266 salt solution Substances 0.000 claims abstract description 7
- 239000007789 gas Substances 0.000 claims description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 230000005540 biological transmission Effects 0.000 claims description 2
- 239000000203 mixture Substances 0.000 claims description 2
- 229910052750 molybdenum Inorganic materials 0.000 claims description 2
- 229910052719 titanium Inorganic materials 0.000 claims description 2
- 229910052721 tungsten Inorganic materials 0.000 claims description 2
- 229910052720 vanadium Inorganic materials 0.000 claims description 2
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 abstract description 9
- 230000008569 process Effects 0.000 abstract description 6
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 abstract 1
- 239000000779 smoke Substances 0.000 description 9
- 230000000052 comparative effect Effects 0.000 description 7
- 238000006477 desulfuration reaction Methods 0.000 description 5
- 230000023556 desulfurization Effects 0.000 description 5
- 229910000831 Steel Inorganic materials 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 4
- 230000007613 environmental effect Effects 0.000 description 4
- 230000035484 reaction time Effects 0.000 description 4
- 239000010959 steel Substances 0.000 description 4
- 238000011144 upstream manufacturing Methods 0.000 description 4
- 238000010531 catalytic reduction reaction Methods 0.000 description 3
- 238000009792 diffusion process Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 238000012423 maintenance Methods 0.000 description 3
- WKXHZKXPFJNBIY-UHFFFAOYSA-N titanium tungsten vanadium Chemical compound [Ti][W][V] WKXHZKXPFJNBIY-UHFFFAOYSA-N 0.000 description 3
- 235000019504 cigarettes Nutrition 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000007789 sealing Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 231100000331 toxic Toxicity 0.000 description 2
- 230000002588 toxic effect Effects 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 1
- 230000001680 brushing effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000001413 cellular effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 239000013065 commercial product Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 230000013011 mating Effects 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000010936 titanium 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
- B01D53/75—Multi-step processes
-
- 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
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur 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
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/76—Gas phase processes, e.g. by using aerosols
-
- 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
- B01D53/8631—Processes characterised by a specific device
-
- 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
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- 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)
- Dispersion Chemistry (AREA)
- Treating Waste Gases (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
The invention discloses a kind of Benitration reactor and denitration sulfur method, which includes shell of reactor, reactor inner cylinder, level-one ammonia-spraying grid, catalyst bed, heat exchanger, two level ammonia-spraying grid, multiple layer metal network chain item and rinsing bowl.Method following content：Flue gas enters at the top of Benitration reactor, gaseous mixture containing ammonia is filled into through level-one ammonia-spraying grid in flue gas, air-flow passes through the catalyst bed equipped with denitrating catalyst from top to bottom, it carries out denitration reaction and removes NOx, flue gas after escape ammonia and reaction is by heat exchange, desulphurization reaction is carried out with the gaseous mixture containing ammonia of two level ammonia-spraying grid filling, it reacts on the multiple layer metal network chain item of dust adhesion in operation in the ammonium salt and flue gas generated, it takes reactor out of, ammonium salt solution discharge is generated by washing.Reactor of the present invention uses two-stage ammonia-spraying grid and metal mesh chain, can effectively remove nitrogen oxides in effluent and oxysulfide, will not block follow up device, reduces follow-up process, reduces operating cost.
Description
Technical field
The invention belongs to gas denitrifying technology fields, more particularly to a kind of flue gas denitration reactor and denitration desulfurization side
Method.
Background technology
Nitrogen oxides is collectively referred to as NOx, is one of primary pollution source of atmosphere pollution.Endanger it is maximum mainly：NO,NO2。
The main harm of NOx is as follows：（1）To the toxic effect of human body；（2）To the toxic effect of plant；（3）Acid rain, acid mist can be formed；
（4）Photochemical fog is formed with hydrocarbon；（5）Destroy ozone layer.
Denitrating flue gas refers to the NOx removed in flue gas, can be divided into wet denitration and Dry denitration by Processing tecchnics.Mainly
Including：Sour absorption process, Alkali absorption method, selective catalytic reduction, non-selective catalytic reduction, absorption method, gas ions activation
Method etc..Some domestic and international scientific research personnel also developed the method for handling NOx exhaust gas with microorganism.But there is industrial value,
With being most widely selective catalytic reduction（SCR）.
The FCC regenerated flue gas denitrations of the flue gas, oil plant of coal-burning power plant at present, which are administered, mainly uses SCR methods, and mating wet
Method washing desulphurization dedusting.By taking FCC flue gases as an example, main flow is as follows：500~600 DEG C of FCC regenerated flue gas first passes through waste heat pot
Stove carries out recycling heat, and flue-gas temperature is reduced to 320~400 DEG C to enter SCR fixed bed reactors and carries out denitration reaction, removes cigarette
Then NOx in gas returns waste heat boiler and carries out recycling heat, flue-gas temperature is down to 150~200 DEG C, subsequently into desulfurization
SOx in flue gas is washed by dedusting washing tower with dust simultaneously using alkaline absorption solution, and flue-gas temperature is reduced to 55~60 DEG C
Discharge.Desulfurization give up absorbing liquid to be settled, be filtered, concentrate and etc. progress solid-liquor separation, ask liquid to use after solid-liquor separation
Air aeration aoxidizes, and COD qualified discharges, solid is filled.
Existing SCR denitration technique is all made of fixed bed Benitration reactor, and catalyst uses cellular, board-like or ripple
Formula, catalyst are placed in reactor in modular form.Reducing agent NH is initially injected before reaction bed3, allow NH3With cigarette
NOx in gas is sufficiently mixed, and by denitrating catalyst bed, NOx catalysis is reduced to N2.Due to typically containing SO in flue gas2、
SO3, O2With vapor, when reaction zone ammonia surplus（The escaping of ammonia）Shi Huiyu SO3Reaction generates ammonium salt, the ammonium salt of generation
（NH4HSO4）, it is in a liquid state for 180~240 DEG C in temperature, there is viscosity, the downstream unit for being liable to stick to SCR denitration reactor saves
On the heat exchanger tube of coal device, the dust being bonded in flue gas causes fouling and clogging and the corrosion of heat exchange tube layer, influences device operation week
Phase.In order to avoid the escaping of ammonia, SCR fixed bed reactors entrances spray ammonia uniformity generally requires positive and negative deviation to be less than 5%.
Invention content
In view of the deficiencies of the prior art, a kind of flue gas denitration reactor of present invention offer and denitrating flue gas sulfur method, this
Invention reactor uses two-stage ammonia-spraying grid and metal mesh chain, can effectively remove the nitrogen oxides in flue gas and sulphur oxidation
Object will not block follow up device, reduce follow-up process, reduce operating cost.
The Benitration reactor of the present invention, including shell of reactor 12, reactor inner cylinder 9, level-one ammonia-spraying grid 7, catalyst
Bed 8, heat exchanger 10, two level ammonia-spraying grid 11, multiple layer metal network chain item 13 and rinsing bowl 15；9 middle and upper part of reactor inner cylinder exists
Except shell of reactor 12,9 lower part of reactor inner cylinder is close between shell of reactor 12 and inner cylinder 9 in shell of reactor 12
It is reactor seal chamber to close space；
The horizontal component of multiple layer metal network chain item 13 is located in reactor, crosses reactor inner cylinder 9, is tightly attached to reactor seal chamber
On interior chain driving wheel 14-1, reactor external seal chamber is stretched out in top layer's horizontal component end of multiple layer metal network chain item 13
Outside, straight down through chain driving wheel 14-2, then upward through the chain driving wheel 14-3 in rinsing bowl 15, and it is close outside reactor
The horizontal component lowest level end for sealing the multiple layer metal network chain item 13 of intracavitary is closed；
Washing facility is set on the right side of the chain of the part straight down of multiple layer metal network chain item 13, and the water outlet of washing facility is located at
Above sink.
Gas access is set at the top of reactor inner cylinder, and gas vent is arranged in reactor inner cylinder bottom；Level-one ammonia-spraying grid is each
Face catalyst bed is exported, two level ammonia-spraying grid respectively exports face metal mesh chain horizontal component.
In the Benitration reactor of the present invention, multiple layer metal network chain item is the metal bracelet of routine, one layer of metal of chain overlying
Net, preferably stainless (steel) wire, mesh size ensure that the ammonium salt adhered to it is not fallen from mesh, generally 100 ~ 350 mesh, preferably
180 ~ 250 mesh.Multiple layer metal network chain horizontal component is preferably provided with 2 ~ 10 layers, more preferably 3 ~ 6 layers, and multiple layer metal network chain item is wide
Degree is configured according to reactor size, is limited with not brushing up against wall of reactor influence metal mesh chain operation.Multiple layer metal net
The external motor driving of chain strip adoption, the rotation direction of each chain driving wheel are consistent.
Present invention simultaneously provides a kind of denitrating flue gas sulfur methods, including following content：Flue gas is at the top of Benitration reactor
Into the gaseous mixture containing ammonia is filled into through level-one ammonia-spraying grid in flue gas, and air-flow passes through and denitrating catalyst is housed from top to bottom
Catalyst bed, carry out denitration reaction remove NOx, escape ammonia and reaction after flue gas by heat exchange, with two level ammonia-spraying grid
The gaseous mixture containing ammonia of filling carries out desulphurization reaction, reacts the ammonium salt of generation and dust adhesion in flue gas in operation
On multiple layer metal network chain item, reactor is taken out of, ammonium salt solution discharge is generated by washing.
In the method for the present invention, the flue gas is typically from coal-fired plant flue gas, FCC regenerated flue gas, refinery processes
Kiln gas or chemical industry kiln gas（Such as cracking of ethylene kiln gas）Deng.Flue gas mainly contains NOx, SOx and impurity, wherein described
Impurity be generally dust, water, CO2And O2Deng the wherein concentration of NOx is generally 700 ~ 4500mg/Nm3, the concentration of SOx is general
For 700 ~ 4500mg/Nm3；Flue-gas temperature into reactor is 300 ~ 420 DEG C, preferably 340~400 DEG C.
In the method for the present invention, the gaseous mixture containing ammonia is the mixture of ammonia and air, and wherein ammonia is mixed
It is 0.5% ~ 10%, preferably 3% ~ 7% to close the volumetric concentration in gas.
In the method for the present invention, the denitrating catalyst is fixed bed denitrating catalyst commonly used in the art, be may be used
Commercial product is prepared according to existing method.Generally vanadium tungsten titanium honeycombed catalyst, group become group commonly used in the art
Point, with catalyst weight, each component content is calculated as with oxide：0.01wt%~1wt%V, 88wt%~99wt%Ti, 0.1wt%
~10wt%W and 0.01wt%~1wt%Mo.In the method for the present invention, the gaseous mixture containing ammonia of the level-one ammonia-spraying grid filling
In, the molar ratio of ammonia and the NOx in flue gas are 0.9：1~1.15：1.
In the method for the present invention, the temperature of the flue gas after heat exchanger exchanges heat is 150 ~ 260 DEG C, preferably 180~
240℃。
In the method for the present invention, in the gaseous mixture containing ammonia of the two level ammonia-spraying grid filling, in ammonia and flue gas
The molar ratio of SOx is 0.9：1~1.15：1.
In the method for the present invention, the flue gas flow rate is 2~15m/s, preferably 4 ~ 10m/s；The denitration reaction residence time is
0.5~20s, desulphurization reaction residence time are 0.5~20s；
In the method for the present invention, the multiple layer metal network chain transmission speed is 0.1mm/s~10mm/s, preferably 0.5~2mm/s.
In the method for the present invention, the multiple layer metal network chain number of plies can according to actual needs and reactor size is selected
It selects, preferably 2~10 layers.
In the method for the present invention, vertical range between the adjacent two layers conveyer belt is 1200 ~ 2000mm, preferably 1400
~1600mm。
In the method for the present invention, the washings sprayed by washing facility water outlet are rinsed metal mesh chain, rinse
Ammonium salt solution afterwards is directly entered sink.
Compared with prior art, the method for the present invention has the following advantages：
（1）Firsts and seconds ammonia-spraying grid is arranged in the present invention, real in same reactor in the case of only loading denitrating catalyst
Denitration and desulphurization reaction are showed, the escape ammonia of denitration reaction continues desulphurization reaction, and SOx, which is converted into ammonium salt, to be adhered to
On the metal mesh of continuous operation, reactor is taken out of, ammonium salt caused by the escaping of ammonia in the prior art is avoided to be adhered to subsequent province's coal
On the heat exchanger tube of device, causes the fouling and clogging of heat exchange tube layer and the problem of corrosion, extending influences the device cycle of operation；
（2）The method of the present invention flexibility and adaptable can adjust attachment by adjusting movement velocity and the number of plies of chain
Ammonium salt amount, therefore the big flue gas of SOx concentration variation ranges can be handled；The ammonium salt being adhered on metal mesh can pass through letter
Single washing forms ammonium salt solution discharge, easy to operate；The dust in flue gas is also adhered to above ammonium salt simultaneously simultaneously, into one
Step is stripped of the dust in flue gas, and denitration, desulfurization and dedusting are completed in same reactor, reduce follow-up process and operation
Amount reduces investment and operating cost.
Description of the drawings
The schematic diagram of the Benitration reactor of Fig. 1 present invention.
1- flue gases, 2- contain the gaseous mixture of ammonia, and 3- contains the gaseous mixture of ammonia, 4- washings, 5- ammonium salt solutions, and 6- is net
Change gas, 7- level-one ammonia-spraying grids, 8- catalyst beds, 9- reactor inner cylinders, 10- heat exchangers, 11- two level ammonia-spraying grids, 12- are anti-
Answer device shell, 13- multiple layer metal network chain items, 14-1,14-2 and 14-3- chain driving wheel, 15- rinsing bowls.
Specific implementation mode
It elaborates to the Benitration reactor and denitration sulfur method of the present invention below by specific embodiment, but not
Therefore the present invention is limited.
The operating process of the Benitration reactor of the present invention is as follows：Flue gas 1 enters from reactor head, the gaseous mixture containing ammonia
2 are filled by level-one ammonia-spraying grid 7 in flue gas 1, and the two mixing passes through catalyst bed 8 from top to bottom, carries out denitration reaction,
NOx is removed, the flue gas after denitration takes heat drop temperature by heat exchanger 10, mixed containing ammonia with being filled by two level ammonia-spraying grid 11
It closes gas 3 and carries out desulphurization reaction, remove SOx, obtained purified gas 6 is discharged from reactor head, is generated after desulphurization reaction
NH4HSO4It is attached on multiple layer metal network chain item 13, multiple layer metal network chain item 13 is constantly sprayed when moving downward by right side washing facility
Go out washings 4 to wash it, chain driving wheel drives the NH adhered on metal mesh chain 134HSO4It is moved into rinsing bowl
15, it forms ammonium salt solution 5 and is discharged.
Embodiment 1
FCC regenerated flue gas flows are 150,000 Nm3/ h, temperature are 650 DEG C, pressure 10kPa, NOx concentration 600mg/Nm3, SO2
A concentration of 1000mg/Nm3, SO3A concentration of 20mg/Nm3, dust content 200mg/Nm3.NOx emission standard is 200 mg/Nm3。
The present embodiment uses fixed reactor, catalyst that commercially available vanadium tungsten titanium honeycombed catalyst, group is used to be divided into
Component known in the art, is loaded using modularization, and single catalyst module height is 1m, three layers of Catalyst packing, reactor
Interior sealing chamber size be long 8m × wide 6m × high 8m；Metal mesh selects 200 mesh stainless (steel) wires, multiple layer metal network chain item setting 2
Layer, conveyer belt size are long 9m × wide 5.8m, drive wheel diameter 300mm, outage 1300mm between upper layer and lower layer conveyer belt, there are
Enough space for maintenances；The mixed gas flow containing ammonia that raw material drainage area provides is 1120Nm3/ h, wherein ammonia concentration are
4v%.FCC regenerated flue gas takes heat, temperature to be reduced to 400 DEG C of SCR denitration reaction temperature by 650 DEG C, contain ammonia by boiler first
The gaseous mixture of gas is added in the upstream flue apart from reactor inlet certain distance, is spread by the mixing of level-one ammonia-spraying grid
Afterwards, ensure that the ammonia concentration deviation in reactor inlet flue gas is less than 5%, into reactor reaction, reaction time 0.5s, warp
After crossing denitration reaction, flue-gas temperature is reduced to 200 DEG C by heat exchange, the mixing containing ammonia with the injection of two level ammonia-spraying grid
Gas carries out desulphurization reaction, reaction time 0.5s, it is ensured that the NOx content of purifying smoke is 100mg/Nm3, SO2Content is
25mg/Nm3, dust content is less than 10mg/ Nm3, meet the environmental requirement of priority control area, flue gas can pass through smoke stack emission.
Embodiment 2
FCC regenerated flue gas flow, temperature, pressure are the same as embodiment 1, NOx concentration 2000mg/Nm3, SO2A concentration of 2000mg/
Nm3, SO3A concentration of 200mg/Nm3, dust content 400mg/Nm3.NOx emission standard is 100 mg/Nm3。
Catalyst is the same as embodiment 1.
FCC regenerated flue gas takes heat, temperature to be reduced to 300 DEG C of SCR denitration reaction temperature by 650 DEG C by boiler first；It is former
Expect that the mixed gas flow containing ammonia that drainage area provides is 1000Nm3/ h, wherein ammonia concentration be 3v%, reactor it is interior close
Envelope chamber size is long 8m × wide 6m × high 15m；Metal mesh selects 200 mesh stainless (steel) wires, multiple layer metal network chain item to be arranged 10 layers, passes
It is long 9m × wide 5.8m to send band size, drives wheel diameter 300mm, and outage 1300mm between upper layer and lower layer conveyer belt, there are enough
Space for maintenance.Gaseous mixture containing ammonia is added in the upstream flue apart from reactor inlet certain distance, is sprayed by level-one
After the mixing diffusion of ammonia grid, ensure that the ammonia concentration deviation in reactor inlet flue gas is less than 5%, into reactor reaction, instead
Flue-gas temperature is reduced to 200 DEG C by heat exchange after denitration reaction for 0.5s between seasonable, is injected with two level ammonia-spraying grid
Gaseous mixture containing ammonia carry out desulphurization reaction, reaction time 2s, it is ensured that the NOx content of purifying smoke is 100mg/
Nm3, SO2Content is 25mg/Nm3, dust content is less than 5mg/ Nm3, meet the environmental requirement of priority control area, flue gas can pass through
Smoke stack emission.
Embodiment 3
FCC regenerated flue gas flow, temperature, pressure are the same as embodiment 1, NOx concentration 300mg/Nm3, SO2A concentration of 600mg/Nm3,
SO3A concentration of 10mg/Nm3, dust content 100mg/Nm3.NOx emission standard is 200 mg/Nm3。
Catalyst is the same as embodiment 1.
FCC regenerated flue gas takes heat, temperature to be reduced to 300 DEG C of SCR denitration reaction temperature by 650 DEG C by boiler first；It is former
Expect that the mixed gas flow containing ammonia that drainage area provides is 2000Nm3/ h, wherein ammonia concentration be 2.8v%, reactor it is interior
Seal chamber size is long 8m × wide 6m × high 6m；Metal mesh selects 200 mesh stainless (steel) wires, multiple layer metal network chain item to be arranged 2 layers, passes
It is long 9m × wide 5.8m to send band size, drives wheel diameter 500mm, and outage 2000mm between upper layer and lower layer conveyer belt, there are enough
Space for maintenance.Gaseous mixture containing ammonia is added in the upstream flue apart from reactor inlet certain distance, is sprayed by level-one
After the mixing diffusion of ammonia grid, ensure that the ammonia concentration deviation in reactor inlet flue gas is less than 5%, into reactor reaction, instead
Flue-gas temperature is reduced to 200 DEG C by heat exchange after denitration reaction for 0.5s between seasonable, is injected with two level ammonia-spraying grid
Gaseous mixture containing ammonia carry out desulphurization reaction, reaction time 0.5s, it is ensured that the NOx content of purifying smoke is 100mg/
Nm3, SO2Content is 25mg/Nm3, dust content is less than 5mg/ Nm3, meet the environmental requirement of priority control area, flue gas can pass through
Smoke stack emission.
Comparative example 1
With embodiment 1, only reactor replaces with traditional SCR denitration reactor, and catalyst uses commercially available vanadium tungsten titanium honeycomb
Shape catalyst, group are divided into component known in the art, are loaded using modularization, and single catalyst module height is 1m, reaction
Device size is 8m × 6m, and three layers of Catalyst packing, first FCC regenerated flue gas take heat, temperature to be reduced to by 650 DEG C by boiler
400 DEG C of SCR denitration reaction temperature；The mixed gas flow containing ammonia that raw material drainage area provides is 1120Nm3/ h, wherein ammonia
A concentration of 4v%.Gaseous mixture containing ammonia is added in the upstream flue apart from reactor inlet certain distance, by ammonia-spraying grid
Mixing diffusion after, ensure reactor inlet flue gas in ammonia concentration deviation be less than 5%, enter back into SCR reactor reactions, pass through
After crossing denitration reaction, it is ensured that the NOx content of purifying smoke is 100mg/Nm3, the flue gas after denitration goes successively to downstream unit
It is exchanged heat, desulfurization and dedusting, meets the environmental requirement of priority control area.
Comparative example 2
With embodiment 2, only reactor replaces with traditional SCR denitration reactor（With comparative example 1）, ensure purifying smoke
NOx content is up to standard.
Comparative example 3
With embodiment 3, only reactor replaces with traditional SCR denitration reactor（With comparative example 1）, ensure purifying smoke
NOx content is up to standard.
The cycle of operation and catalyst amount of embodiment 1 ~ 3 and comparative example 1 ~ 3 are shown in Table 1.
The comparison of table 1 embodiment and the comparative example cycle of operation and catalyst amount.
Claims (16)
1. a kind of Benitration reactor, it is characterised in that including：Shell of reactor（12）, reactor inner cylinder（9）, level-one ammonia-spraying grid
（7）, catalyst bed（8）, heat exchanger（10）, two level ammonia-spraying grid（11）, multiple layer metal network chain item（13）And rinsing bowl（15）；
Reactor inner cylinder（9）Middle and upper part is in shell of reactor（12）Except, reactor inner cylinder（9）Lower part is in shell of reactor（12）It is interior,
Shell of reactor（12）And inner cylinder（9）Between confined space be reactor seal chamber；Multiple layer metal network chain item（13）Level
Part is located in reactor, crosses reactor inner cylinder（9）, the chain driving wheel be tightly attached in reactor seal chamber（14-1）On,
Multiple layer metal network chain item（13）Top layer's horizontal component end stretch out reactor external seal chamber outside, through chain driving wheel（14-2）
Straight down, then through rinsing bowl（15）Interior chain driving wheel（14-3）Upwards, golden with the multilayer of reactor external seal intracavitary
Belong to network chain item（13）Horizontal component lowest level end be closed.
2. Benitration reactor described in accordance with the claim 1, it is characterised in that：Multiple layer metal network chain item（13）Portion straight down
Washing facility is set on the right side of the chain divided, and the water outlet of washing facility is located above sink.
3. Benitration reactor described in accordance with the claim 1, it is characterised in that：Gas access is set at the top of reactor inner cylinder, instead
Answer device inner cylinder bottom that gas vent is set；Level-one ammonia-spraying grid respectively exports face catalyst bed, and two level ammonia-spraying grid respectively exports
Face metal mesh chain horizontal component.
4. Benitration reactor described in accordance with the claim 1, it is characterised in that：Multiple layer metal network chain item is metal bracelet overlying one
Layer metal mesh, mesh size are 100 ~ 350 mesh；Multiple layer metal network chain horizontal component is arranged 2 ~ 10 layers.
5. Benitration reactor described in accordance with the claim 1, it is characterised in that：The external motor of multiple layer metal network chain strip adoption drives
Dynamic, the rotation direction of each chain driving wheel is consistent.
6. a kind of denitrating flue gas sulfur method, it is characterised in that including following content：Flue gas enters at the top of Benitration reactor, contains
The gaseous mixture of ammonia is filled into through level-one ammonia-spraying grid in flue gas, and air-flow passes through the catalyst equipped with denitrating catalyst from top to bottom
Bed carries out denitration reaction and removes NOx, and the flue gas after escape ammonia and reaction is by heat exchange, with containing for two level ammonia-spraying grid filling
The gaseous mixture of ammonia carries out desulphurization reaction, reacts the ammonium salt of generation and the multiple layer metal of dust adhesion in operation in flue gas
On network chain item, reactor is taken out of, ammonium salt solution discharge is generated by washing.
7. according to the method for claim 6, it is characterised in that：The flue-gas temperature into reactor is 300 ~ 420 DEG C.
8. according to the method for claim 6, it is characterised in that：The gaseous mixture containing ammonia is ammonia and air
The volumetric concentration of mixture, wherein ammonia in gaseous mixture is 0.5% ~ 10%.
9. according to the method for claim 6, it is characterised in that：The denitrating catalyst, with catalyst weight, each group
Point content is calculated as with oxide：0.01wt%~1wt%V, 88wt%~99wt%Ti, 0.1wt%~10wt%W and 0.01wt%~
1wt%Mo。
10. according to the method for claim 6, it is characterised in that：The mixing containing ammonia of the level-one ammonia-spraying grid filling
It closes in gas, the molar ratio of ammonia and the NOx in flue gas are 0.9：1~1.15：1.
11. according to the method for claim 6, it is characterised in that：The temperature of the flue gas after heat exchanger exchanges heat
It is 150 ~ 260 DEG C.
12. according to the method for claim 6, it is characterised in that：The mixing containing ammonia of the two level ammonia-spraying grid filling
It closes in gas, the molar ratio of ammonia and the SOx in flue gas are 0.9：1~1.15：1.
13. according to the method for claim 6, it is characterised in that：The flue gas flow rate is 2~15m/s；Denitration reaction stops
It is 0.5~20s to stay the time.
14. according to the method for claim 6, it is characterised in that：The multiple layer metal network chain transmission speed is 0.1mm/s
~10mm/s.
15. according to the method for claim 6, it is characterised in that：The multiple layer metal network chain number of plies is 2~10 layers.
16. according to the method for claim 6, it is characterised in that：Vertical range between the adjacent two layers conveyer belt
For 1200 ~ 2000mm.
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Effective date of registration: 20231009 Address after: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee after: CHINA PETROLEUM & CHEMICAL Corp. Patentee after: Sinopec (Dalian) Petrochemical Research Institute Co.,Ltd. Address before: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee before: CHINA PETROLEUM & CHEMICAL Corp. Patentee before: DALIAN RESEARCH INSTITUTE OF PETROLEUM AND PETROCHEMICALS, SINOPEC Corp. |