CN108786403B - Denitration reactor and denitration and desulfurization method - Google Patents
Denitration reactor and denitration and desulfurization method Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 43
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 24
- 230000023556 desulfurization Effects 0.000 title claims abstract description 24
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 113
- 239000003546 flue gas Substances 0.000 claims abstract description 82
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 81
- 229910052751 metal Inorganic materials 0.000 claims abstract description 46
- 239000002184 metal Substances 0.000 claims abstract description 46
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 40
- 238000006243 chemical reaction Methods 0.000 claims abstract description 39
- 239000003054 catalyst Substances 0.000 claims abstract description 36
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- 238000005507 spraying Methods 0.000 claims abstract description 22
- 150000003863 ammonium salts Chemical class 0.000 claims abstract description 18
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 17
- 239000012266 salt solution Substances 0.000 claims abstract description 7
- 238000005406 washing Methods 0.000 claims description 15
- 239000000203 mixture Substances 0.000 claims description 6
- 238000007789 sealing Methods 0.000 claims description 5
- 230000005540 biological transmission Effects 0.000 claims 1
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- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 abstract description 6
- 230000008569 process Effects 0.000 abstract description 6
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 abstract 1
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- 238000004231 fluid catalytic cracking Methods 0.000 description 12
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Classifications
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- 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
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- 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
Abstract
The invention discloses a denitration reactor and a denitration and desulfurization method. The method comprises the following steps: flue gas enters from the top of the denitration reactor, mixed gas containing ammonia gas is filled into the flue gas through the primary ammonia-spraying grid, airflow passes through a catalyst bed layer filled with a denitration catalyst from top to bottom to carry out denitration reaction to remove NOx, escaped ammonia and the flue gas after reaction are subjected to heat exchange and are subjected to desulfurization reaction with the mixed gas containing ammonia gas filled through the secondary ammonia-spraying grid, ammonium salt generated by the reaction and dust in the flue gas are adhered to a plurality of layers of metal mesh chains in operation, are taken out of the reactor, and are washed by water to generate ammonium salt solution which is discharged. The reactor of the invention adopts two-stage ammonia injection grids and metal mesh chains, can effectively remove nitrogen oxides and sulfur oxides in the flue gas, does not block subsequent devices, reduces subsequent processes and reduces operation cost.
Description
Technical Field
The invention belongs to the technical field of flue gas denitration, and particularly relates to a flue gas denitration reactor and a denitration and desulfurization method.
Background
Nitrogen oxides, collectively referred to as NOx, are one of the main sources of atmospheric pollution. The most harmful are:NO、NO2. The major hazards of NOx are as follows: (1) has toxic effect on human body; (2) has toxic action on plants; (3) acid rain and acid mist can be formed; (4) forming photochemical smog with hydrocarbon; (5) and destroying the ozone layer.
The flue gas denitration refers to removing NOx in flue gas, and can be divided into wet denitration and dry denitration according to treatment processes. The method mainly comprises the following steps: acid absorption, alkali absorption, selective catalytic reduction, non-selective catalytic reduction, adsorption, plasma activation, and the like. Some researchers at home and abroad have also developed a method for treating NOx waste gas by using microorganisms. But is of industrial value and the most widely used is the Selective Catalytic Reduction (SCR) process.
At present, the denitration treatment of flue gas of a coal-fired power plant and FCC regenerated flue gas of an oil refinery mainly adopts an SCR method and is matched with wet washing, desulfurization and dust removal. Taking FCC flue gas as an example, the main flow is as follows: the method comprises the steps that FCC regenerated flue gas at 500-600 ℃ is subjected to heat recovery through a waste heat boiler, the temperature of the flue gas is reduced to 320-400 ℃, the flue gas enters an SCR fixed bed reactor for denitration reaction, NOx in the flue gas is removed, then the flue gas returns to the waste heat boiler to recover heat, the temperature of the flue gas is reduced to 150-200 ℃, then the flue gas enters a desulfurization and dedusting washing tower, SOx and dust in the flue gas are washed down by adopting alkaline absorption liquid, and the temperature of the flue gas is reduced to 55-60 ℃ and is discharged. And (3) carrying out liquid-solid separation on the desulfurization waste absorption liquid by the steps of settling, filtering, concentrating and the like, wherein the liquid after the liquid-solid separation is oxidized by adopting air aeration, COD (chemical oxygen demand) reaches the standard and is discharged, and the solid is buried.
The existing SCR denitration process adopts a fixed bed denitration reactor, a catalyst adopts a honeycomb type, a plate type or a corrugated type, and the catalyst is placed in the reactor in a module form. Firstly injecting reducing agent NH in front of the reaction bed layer3Let NH3Fully mixed with NOx in the flue gas, and the NOx is catalytically reduced into N through a denitration catalyst bed layer2. Because the flue gas generally contains SO2、SO3，O2With water vapor, SO when the reaction zone has excess ammonia (ammonia slip)3Reacting to form ammonium salt, and forming ammonium salt (NH)4HSO4) At a temperature of 180 &The liquid state at 240 ℃ has viscosity, and the liquid state is easy to adhere to a heat exchange tube of a coal economizer of a downstream device of the SCR denitration reactor, so that dust in flue gas is bonded to cause scaling blockage and corrosion of the heat exchange tube layer, and the operation period of the device is influenced. In order to avoid ammonia escape, the uniformity of ammonia injection at the inlet of the SCR fixed bed reactor generally requires that the plus-minus deviation is less than 5%.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a flue gas denitration reactor and a flue gas denitration and desulfurization method.
The denitration reactor comprises a reactor shell 12, a reactor inner cylinder 9, a primary ammonia spraying grid 7, a catalyst bed layer 8, a heat exchanger 10, a secondary ammonia spraying grid 11, a multi-layer metal mesh chain 13 and a rinsing bath 15; the middle upper part of the reactor inner cylinder 9 is arranged outside the reactor shell 12, the lower part of the reactor inner cylinder 9 is arranged in the reactor shell 12, and the closed space between the reactor shell 12 and the reactor inner cylinder 9 is a reactor sealing cavity;
the horizontal part of the multilayer metal mesh chain 13 is positioned in the reactor, traverses the inner cylinder 9 of the reactor and clings to a chain driving wheel 14-1 in a sealed cavity of the reactor, the tail end of the uppermost layer horizontal part of the multilayer metal mesh chain 13 extends out of the outer sealed cavity of the reactor, vertically downwards passes through the chain driving wheel 14-2 and then upwards passes through a chain driving wheel 14-3 in a rinsing tank 15 to be closed with the tail end of the lowermost layer of the horizontal part of the multilayer metal mesh chain 13 in the outer sealed cavity of the reactor;
and washing equipment is arranged on the right side of the vertically downward part of the multilayer metal mesh chain 13, and a water outlet of the washing equipment is positioned above the water tank.
The top of the reactor inner cylinder is provided with a gas inlet, and the bottom of the reactor inner cylinder is provided with a gas outlet; the outlets of the first-stage ammonia spraying grid are opposite to the catalyst bed layer, and the outlets of the second-stage ammonia spraying grid are opposite to the horizontal part of the metal mesh chain.
In the denitration reactor, the multi-layer metal net chain is a conventional metal chain, a layer of metal net, preferably a stainless steel net, is covered on the chain, and the size of the meshes ensures that ammonium salt adhered on the chain does not fall off from the meshes, generally 100-350 meshes, preferably 180-250 meshes. The horizontal part of multilayer metal mesh chain preferably sets up 2~10 layers, more preferably 3~6 layers, and multilayer metal mesh chain width sets up according to the reactor size to do not reach the reactor wall and influence the operation limit of metal mesh chain. The multilayer metal mesh chains are driven by external motors, and the rotation directions of the chain driving wheels are consistent.
The invention also provides a flue gas denitration and desulfurization method, which comprises the following steps: flue gas enters from the top of the denitration reactor, mixed gas containing ammonia gas is filled into the flue gas through the primary ammonia-spraying grid, airflow passes through a catalyst bed layer filled with a denitration catalyst from top to bottom to carry out denitration reaction to remove NOx, escaped ammonia and the flue gas after reaction are subjected to heat exchange and are subjected to desulfurization reaction with the mixed gas containing ammonia gas filled through the secondary ammonia-spraying grid, ammonium salt generated by the reaction and dust in the flue gas are adhered to a plurality of layers of metal mesh chains in operation, are taken out of the reactor, and are washed by water to generate ammonium salt solution which is discharged.
In the method, the flue gas generally comes from flue gas of a coal-fired power plant, FCC regenerated flue gas, flue gas of an oil refinery process furnace or flue gas of a chemical industry furnace (such as flue gas of an ethylene cracking furnace) and the like. The flue gas mainly contains NOx, SOx and impurities, wherein the impurities are dust, water and CO2And O2Etc., wherein the concentration of NOx is generally 700-4500 mg/Nm3The concentration of SOx is generally 700-4500 mg/Nm3(ii) a The temperature of the flue gas entering the reactor is 300-420 ℃, and preferably 340-400 ℃.
In the method, the mixed gas containing ammonia gas is a mixture of ammonia gas and air, wherein the volume concentration of the ammonia gas in the mixed gas is 0.5-10%, and preferably 3-7%.
In the method, the denitration catalyst is a fixed bed denitration catalyst commonly used in the field, and can be prepared by a commercially available product or an existing method. The catalyst is a vanadium tungsten titanium honeycomb catalyst generally, and comprises the following components which are commonly used in the field, and the contents of the components are calculated by oxides according to the weight of the catalyst: 0.01wt% -1 wt% of V, 88wt% -99 wt% of Ti, 0.1wt% -10 wt% of W and 0.01wt% -1 wt% of Mo. In the method, in the mixed gas containing ammonia gas filled by the primary ammonia-spraying grid, the molar ratio of the ammonia gas to NOx in the flue gas is 0.9: 1-1.15: 1.
in the method, the temperature of the flue gas after heat exchange by the heat exchanger is 150-260 ℃, and preferably 180-240 ℃.
In the method, in the mixed gas containing ammonia gas filled by the secondary ammonia-spraying grid, the mol ratio of the ammonia gas to SOx in the flue gas is 0.9: 1-1.15: 1.
in the method, the flow velocity of the flue gas is 2-15 m/s, preferably 4-10 m/s; the residence time of the denitration reaction is 0.5-20 s, and the residence time of the desulfurization reaction is 0.5-20 s;
in the method, the conveying speed of the multilayer metal mesh chain is 0.1-10 mm/s, preferably 0.5-2 mm/s.
In the method, the number of layers of the multilayer metal mesh chain can be selected according to actual needs and the size of the reactor, and preferably 2-10 layers.
In the method, the vertical distance between two adjacent layers of conveyor belts is 1200-2000 mm, preferably 1400-1600 mm.
In the method, the metal mesh chain is washed by the washing water sprayed from the water outlet of the washing equipment, and the washed ammonium salt solution directly enters the water tank.
Compared with the prior art, the method has the following advantages:
(1) the invention is provided with the primary and secondary ammonia injection grids, the denitration and desulfurization reactions are realized in the same reactor only under the condition of filling the denitration catalyst, the escaped ammonia of the denitration reaction continues the desulfurization reaction, SOx is directly converted into ammonium salt to be adhered to a continuously running metal net and is taken out of the reactor, the problem that the ammonium salt caused by the escaped ammonia in the prior art is adhered to a heat exchange tube of a subsequent economizer to cause scaling blockage and corrosion of the heat exchange tube layer is avoided, and the operation period of the device is influenced;
(2) the method has high flexibility and adaptability, and can adjust the amount of the attached ammonium salt by adjusting the movement speed and the number of layers of the chains, thereby being capable of treating the flue gas with large SOx concentration change range; the ammonium salt adhered to the metal net can form ammonium salt solution to be discharged through simple water washing, and the operation is simple; meanwhile, the dust in the flue gas is also adhered to the ammonium salt, so that the dust in the flue gas is further removed, and the denitration, the desulfurization and the dust removal are completed in the same reactor, so that the subsequent flow and the operation amount are reduced, and the investment and the operation cost are reduced.
Drawings
FIG. 1 is a schematic view of a denitration reactor of the present invention.
1-flue gas, 2-mixed gas containing ammonia gas, 3-mixed gas containing ammonia gas, 4-washing water, 5-ammonium salt solution, 6-purified gas, 7-primary ammonia spraying grid, 8-catalyst bed layer, 9-reactor inner cylinder, 10-heat exchanger, 11-secondary ammonia spraying grid, 12-reactor shell, 13-multilayer metal mesh chain, 14-1, 14-2 and 14-3-chain driving wheel and 15-water washing tank.
Detailed Description
The denitration reactor and the denitration and desulfurization method according to the present invention will be described in detail with reference to the following specific examples, but the present invention is not limited thereto.
The operation process of the denitration reactor is as follows: flue gas 1 enters from the top of the reactor, mixed gas 2 containing ammonia gas is injected into the flue gas 1 through a primary ammonia injection grid 7, the mixed gas and the mixed gas pass through a catalyst bed layer 8 from top to bottom for denitration reaction and NOx removal, the flue gas after denitration is heated and cooled through a heat exchanger 10, the flue gas and the mixed gas 3 containing ammonia gas injected through a secondary ammonia injection grid 11 are subjected to desulfurization reaction, SOx is removed, the obtained purified gas 6 is discharged from the top of the reactor, and NH generated after desulfurization reaction4HSO4Attached to the multi-layer metal mesh chain 13, the multi-layer metal mesh chain 13 is continuously sprayed with washing water 4 by a right washing device to be washed when moving downwards, and the chain driving wheel drives NH attached to the metal mesh chain 134HSO4Moves into a water washing tank 15 and forms ammonium salt solution 5 to be discharged.
Example 1
The flow rate of FCC regeneration flue gas is 15 ten thousand Nm3H, temperatureAt 650 ℃, a pressure of 10kPa, and a NOx concentration of 600mg/Nm3，SO2The concentration is 1000mg/Nm3，SO3The concentration is 20mg/Nm3Dust content of 200mg/Nm3. NOx emission standard is 200mg/Nm3。
In the embodiment, a fixed reactor is adopted, a commercially available vanadium-tungsten-titanium honeycomb catalyst is adopted as the catalyst, the components are well known in the field, the catalyst is filled in a modularized mode, the height of a single catalyst module is 1m, three layers of catalysts are filled, and the size of an inner sealing cavity of the reactor is 8m in length, 6m in width and 8m in height; the metal net is a 200-mesh stainless steel net, the multi-layer metal net chain is provided with 2 layers, the conveyor belt is 9m long by 5.8m wide, the diameter of the driving wheel is 300mm, the space between the upper and lower layers of conveyor belts is 1300mm high, and enough maintenance space is reserved; the flow rate of the ammonia-containing mixture supplied from the raw material supply section was 1120Nm3H, ammonia concentration 4 v%. Firstly, FCC regenerated flue gas is heated by a boiler, the temperature is reduced from 650 ℃ to 400 ℃ of SCR denitration reaction temperature, mixed gas containing ammonia is added into an upstream flue which is at a certain distance from the inlet of a reactor, after the mixed gas is mixed and diffused by a primary ammonia injection grid, the ammonia concentration deviation in the flue gas at the inlet of the reactor is ensured to be less than 5%, the mixed gas enters the reactor for reaction, the reaction time is 0.5s, after the denitration reaction, the flue gas temperature is reduced to 200 ℃ through heat exchange, the mixed gas containing ammonia injected by a secondary ammonia injection grid is subjected to desulfurization reaction, the reaction time is 0.5s, and the NOx content of purified flue gas can be ensured to be 100mg/Nm3，SO2The content is 25mg/Nm3Dust content of less than 10mg/Nm3Meets the environmental protection requirement of key control areas, and the smoke can be discharged through a chimney.
Example 2
The FCC regeneration flue gas flow, temperature and pressure are the same as those of example 1, and the NOx concentration is 2000mg/Nm3，SO2The concentration is 2000mg/Nm3，SO3The concentration is 200mg/Nm3Dust content of 400mg/Nm3. NOx emission standard is 100mg/Nm3。
The catalyst was the same as in example 1.
Firstly, FCC regenerated flue gas is heated and warmed by a boilerThe temperature is reduced from 650 ℃ to 300 ℃ for SCR denitration reaction; the flow rate of the ammonia-containing mixture supplied from the raw material supply section was 1000Nm3The ammonia concentration is 3v%, and the size of an inner sealing cavity of the reactor is 8m in length, 6m in width and 15m in height; the metal mesh selects 200 meshes of stainless steel mesh, the multilayer metal mesh chain is provided with 10 layers, the conveyor belt is 9m long multiplied by 5.8m wide, the diameter of the driving wheel is 300mm, the space between the upper layer of conveyor belt and the lower layer of conveyor belt is 1300mm high, and enough maintenance space is reserved. Adding mixed gas containing ammonia gas into an upstream flue at a certain distance from the inlet of the reactor, after mixed diffusion of the primary ammonia injection grid, ensuring that the concentration deviation of the ammonia gas in the flue gas at the inlet of the reactor is less than 5%, allowing the mixed gas to enter the reactor for reaction for 0.5s, reducing the temperature of the flue gas to 200 ℃ through heat exchange after denitration reaction, performing desulfurization reaction with the mixed gas containing ammonia gas injected into the secondary ammonia injection grid, wherein the reaction time is 2s, and ensuring that the NOx content of purified flue gas is 100mg/Nm3，SO2The content is 25mg/Nm3Dust content of less than 5mg/Nm3Meets the environmental protection requirement of key control areas, and the smoke can be discharged through a chimney.
Example 3
The FCC regeneration flue gas flow, temperature and pressure are the same as those of the example 1, and the concentration of NOx is 300mg/Nm3，SO2The concentration is 600mg/Nm3，SO3The concentration is 10mg/Nm3Dust content of 100mg/Nm3. NOx emission standard is 200mg/Nm3。
The catalyst was the same as in example 1.
Firstly, heating FCC (fluid catalytic cracking) regenerated flue gas by a boiler, and reducing the temperature from 650 ℃ to 300 ℃ for SCR denitration reaction; the flow rate of the ammonia-containing mixture supplied from the raw material supply section was 2000Nm3The concentration of ammonia gas is 2.8v%, and the size of an inner sealing cavity of the reactor is 8m in length, 6m in width and 6m in height; the metal mesh selects 200 meshes of stainless steel mesh, the multilayer metal mesh chain is provided with 2 layers, the conveyor belt is 9m long multiplied by 5.8m wide, the diameter of the driving wheel is 500mm, the space between the upper layer of conveyor belt and the lower layer of conveyor belt is 2000mm, and enough maintenance space is reserved. The mixed gas containing ammonia gas is added into an upstream flue at a certain distance from the inlet of the reactor and passes through a mixing expansion grid of a primary ammonia spraying gridAfter dispersion, ensuring that the concentration deviation of ammonia gas in the flue gas at the inlet of the reactor is less than 5 percent, entering the reactor for reaction, wherein the reaction time is 0.5s, after denitration reaction, reducing the temperature of the flue gas to 200 ℃ through heat exchange, and performing desulfurization reaction with mixed gas containing ammonia gas injected into the secondary ammonia injection grid, wherein the reaction time is 0.5s, and the NOx content of the purified flue gas can be ensured to be 100mg/Nm3，SO2The content is 25mg/Nm3Dust content of less than 5mg/Nm3Meets the environmental protection requirement of key control areas, and the smoke can be discharged through a chimney.
Comparative example 1
The same as example 1, except that the reactor is replaced by a traditional SCR denitration reactor, the catalyst adopts a commercial vanadium tungsten titanium honeycomb catalyst, the components of the catalyst are well known in the field, modular filling is adopted, the height of a single catalyst module is 1m, the size of the reactor is 8m multiplied by 6m, the catalyst is filled into three layers, firstly, FCC regenerated flue gas is heated by a boiler, and the temperature is reduced from 650 ℃ to the SCR denitration reaction temperature of 400 ℃; the flow rate of the ammonia-containing mixture supplied from the raw material supply section was 1120Nm3H, ammonia concentration 4 v%. The mixed gas containing ammonia gas is added into an upstream flue at a certain distance from the inlet of the reactor, the ammonia gas concentration deviation in the flue gas at the inlet of the reactor is ensured to be less than 5 percent after the mixed diffusion of an ammonia spraying grid, the mixed gas enters the SCR reactor for reaction, and the NOx content of the purified flue gas can be ensured to be 100mg/Nm after the denitration reaction3And the denitrated flue gas continuously enters a downstream device for heat exchange, desulfurization and dust removal, so that the environmental protection requirement of key control areas is met.
Comparative example 2
The same as the embodiment 2, except that the reactor is replaced by the traditional SCR denitration reactor (the same as the comparative example 1), the NOx content of the purified flue gas is ensured to reach the standard.
Comparative example 3
The same as example 3, except that the reactor is replaced by the traditional SCR denitration reactor (same as comparative example 1), and the NOx content of the purified flue gas is ensured to reach the standard.
The operation cycle and the amount of catalyst used in examples 1 to 3 and comparative examples 1 to 3 are shown in Table 1.
Table 1 comparison of run length and catalyst usage for the examples and comparative examples.
Claims (15)
1. A denitration reactor, comprising: the device comprises a reactor shell (12), a reactor inner cylinder (9), a primary ammonia spraying grid (7), a catalyst bed layer (8), a heat exchanger (10), a secondary ammonia spraying grid (11), a multi-layer metal mesh chain (13) and a rinsing bath (15); the middle upper part of the reactor inner cylinder (9) is arranged outside the reactor shell (12), the lower part of the reactor inner cylinder (9) is arranged in the reactor shell (12), and the closed space between the reactor shell (12) and the reactor inner cylinder (9) is a reactor sealing cavity; the horizontal part of the multilayer metal mesh chain (13) is positioned in the reactor, traverses through the inner cylinder (9) of the reactor and clings to a chain driving wheel in a sealed cavity of the reactor, the tail end of the topmost horizontal part of the multilayer metal mesh chain (13) extends out of the sealed cavity of the reactor, vertically downwards passes through the chain driving wheel, then upwards passes through the chain driving wheel in a washing tank (15) and is closed with the tail end of the bottommost layer of the horizontal part of the multilayer metal mesh chain (13) in the sealed cavity of the reactor; the top of the reactor inner cylinder is provided with a gas inlet, and the bottom of the reactor inner cylinder is provided with a gas outlet; the outlets of the first-stage ammonia spraying grid are opposite to the catalyst bed layer, and the outlets of the second-stage ammonia spraying grid are opposite to the horizontal part of the metal mesh chain.
2. The denitration reactor of claim 1, wherein: washing equipment is arranged on the right side of the vertically downward part of the multilayer metal mesh chain (13), and a water outlet of the washing equipment is positioned above the water tank.
3. The denitration reactor of claim 1, wherein: the multilayer metal net chain is formed by covering a metal net layer on a metal chain, and the mesh size is 100-350 meshes; the horizontal part of the multilayer metal mesh chain is provided with 2-10 layers.
4. The denitration reactor of claim 1, wherein: the multilayer metal mesh chains are driven by external motors, and the rotation directions of the chain driving wheels are consistent.
5. The flue gas denitration and desulfurization method of the denitration reactor of claim 1, characterized by comprising the following steps: flue gas enters from the top of the denitration reactor, mixed gas containing ammonia gas is filled into the flue gas through the primary ammonia-spraying grid, airflow passes through a catalyst bed layer filled with a denitration catalyst from top to bottom to carry out denitration reaction to remove NOx, escaped ammonia and the flue gas after reaction are subjected to heat exchange and are subjected to desulfurization reaction with the mixed gas containing ammonia gas filled through the secondary ammonia-spraying grid, ammonium salt generated by the reaction and dust in the flue gas are adhered to a plurality of layers of metal mesh chains in operation, are taken out of the reactor, and are washed by water to generate ammonium salt solution which is discharged.
6. The method of claim 5, wherein: the temperature of the flue gas entering the reactor is 300-420 ℃.
7. The method of claim 5, wherein: the mixed gas containing ammonia gas is a mixture of ammonia gas and air, wherein the volume concentration of the ammonia gas in the mixed gas is 0.5-10%.
8. The method of claim 5, wherein: the denitration catalyst comprises the following components in percentage by weight: 0.01wt% -1 wt% of V, 88wt% -99 wt% of Ti, 0.1wt% -10 wt% of W and 0.01wt% -1 wt% of Mo.
9. The method of claim 5, wherein: in the mixed gas containing ammonia gas filled by the primary ammonia-spraying grid, the mol ratio of the ammonia gas to NOx in the flue gas is 0.9: 1-1.15: 1.
10. the method of claim 5, wherein: the temperature of the flue gas after heat exchange of the heat exchanger is 150-260 ℃.
11. The method of claim 5, wherein: in the mixed gas containing ammonia gas filled by the secondary ammonia-spraying grid, the mol ratio of the ammonia gas to SOx in the flue gas is 0.9: 1-1.15: 1.
12. the method of claim 5, wherein: the flow velocity of the flue gas is 2-15 m/s; the residence time of the denitration reaction is 0.5-20 s.
13. The method of claim 5, wherein: the transmission speed of the multilayer metal mesh chain is 0.1 mm/s-10 mm/s.
14. The method of claim 5, wherein: the number of layers of the multilayer metal mesh chain is 2-10.
15. The method of claim 5, wherein: the vertical distance between two adjacent layers of metal mesh chains is 1200-2000 mm.
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| CN114917746B (en) * | 2022-06-16 | 2023-03-28 | 南通恒和环保科技有限公司 | Waste gas purification tower spray set and waste gas purification tower |
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