CN115400590A - SCR denitration process method in tail gas of solid caustic furnace - Google Patents
SCR denitration process method in tail gas of solid caustic furnace Download PDFInfo
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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
- B01D53/86—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
- 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
- B01D53/346—Controlling the process
-
- 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
- B01D53/90—Injecting reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
Abstract
The invention discloses an SCR denitration process method in tail gas of a solid alkali furnace, ammonia water with the mass concentration of 20% is used as a denitration reducing agent, 1 layer of catalyst is arranged in each SCR reactor, 1 set of SCR reactor is arranged at the outlet of a combustion air heat exchanger of the solid alkali molten salt furnace, a plurality of layers of SCR reactors are used in cascade, 1 acoustic wave soot blower and a flue gas purification device are respectively arranged above each layer of catalyst, if the parameters of a single SCR reactor reach design and outlet calibration indexes, the automatic operation can be determined to the next production procedure or the multiple return is carried out to the bottom SCR reactor through sampling detection, the differential pressure of the bottom catalyst is 0-400 Pa, the differential pressure of the middle catalyst is 0-350 Pa, the differential pressure of the top catalyst is 0-380 Pa, the total resistance is ensured to be lower than 600Pa, the flue gas enters the SCR reactor from bottom to top for denitration, the temperature and the mass concentration of the ammonia liquid in an ammonia liquid siphon device are ensured to be more uniform, and a plurality of problems provided in the background can be solved, the operation is convenient, and the process is suitable for industrial application compared with the traditional process.
Description
Technical Field
The invention relates to the field of SCR denitration technology in tail gas, in particular to a process method for SCR denitration in tail gas of a solid alkali furnace.
Background
The production process mainly comprises the steps that molten salt (liquid state) in a molten salt storage tank is pumped into a solid alkali heating furnace (two layers of coil pipes are arranged in the furnace) for burning calcium carbide furnace gas (or natural gas) and air through a molten salt pump, the molten salt in the coil pipes is heated to about 430 ℃ through heat transfer and then carries out reverse heat exchange with 61% alkali liquor in a final concentrator, the alkali liquor is concentrated into high-concentration alkali with the concentration of more than 98.2%, the molten salt after heat exchange flows back into the molten salt storage tank by means of self gravity, the process is carried out repeatedly, the calcium carbide furnace gas (or natural gas) and the air need to be matched through a low-nitrogen combustion control system, flue gas tail gas generated after burning and cold air provided by a combustion air fan exchange heat in a flue gas preheater, the comprehensive heat efficiency is further improved, and the tail gas after heat exchange is discharged into the atmosphere. The existing problem is that the nitrogen oxide in the tail gas exceeds the standard value, and the furnace end is also considered to be replaced in the tail gas treatment, and the low-nitrogen combustion mode is adopted. However, the low-nitrogen combustion needs a long stopping period of the alkali fixation furnace, so that the annual yield plan is influenced, whether an operating system of the furnace end after low-nitrogen combustion is matched with the matching technology and hardware of the existing furnace body cannot be determined, and the replacement cost and the new technical improvement cost are high; in the industry, an SCR denitration process is also adopted for treating solid caustic soda tail gas, but the resistance of a catalytic layer is increased, and combustion-supporting air at a combustor has higher back pressure, so that the heat provided by the combustor can be influenced; the concentration device can not obtain enough heat to cause low-load operation, sometimes causes vibration of a furnace and a combustor, and has great influence on the safe use of equipment. Such as refractory falling, such as sealing problems, and even coil sinking; can lead to insufficient combustion and generate a large amount of CO, which is a potential safety hazard; meanwhile, in the production process, the temperature is low, the SCR reactor does not reach the optimal catalytic temperature, and the risk of ammonia escape is increased; when the temperature is high, the temperature of the SCR inlet smoke is too high and exceeds the highest temperature which can be borne by the catalyst, permanent damage can be caused to the catalyst, and the SCR inlet smoke is not suitable for being put into a denitration system; when the content of the nitrogen oxides is low, the ammonia injection amount is too large, and the risk of ammonia escape exists; when the NOx content is high, the ammonia injection amount is too small, and the risk of environmental protection not reaching the standard exists. The pressure is low, the ammonia water atomization device is not suitable for the state of the minimum pressure required by ammonia water atomization, and the soot blowing of the soot blower is incomplete; pressure is high, causes the damage to instrument, spray gun and soot blower to lead to the compressed air consumption to increase the too high waste water pit overflow that leads to easily of liquid level, lead to ammonia in the cofferdam to distribute, the severe person leads to the poisoning of people's poisoning etc. ammonia to leak and leads to nearby personnel poisoning, may lead to dangers such as explosion under the too high condition of concentration.
Chinese patent ZL 202011637455.6 discloses an SCR denitration method and device, and flue gas is mainly subjected to denitration by a ceramic heat accumulator, a first catalyst, a second catalyst, the first catalyst and the ceramic heat accumulator in sequence in a one-way manner; the denitrated flue gas passes through the ceramic heat accumulator, the first catalyst, the second catalyst, the first catalyst and the ceramic heat accumulator in sequence in one way for denitration; the technical problem solved is how to effectively denitrate the flue gas with the temperature fluctuating in a wider range, SO that the problems of nitrogen oxide emission exceeding standard, ammonia escape increasing and the like can not occur, the problem of sulfur poisoning caused by the increase of SO2/SO3 conversion rate due to the reduction of the activity temperature of a catalyst can not be caused, the effective denitration during full-load operation of a system can be also met, the flue gas denitration device can adapt to the flue gas temperature change caused by frequent fluctuation of the load of a boiler (kiln), the stable ultralow emission of the nitrogen oxide and the ammonia is realized, and the denitration device is more practical. However, this technique is not based on the existing production scale and is not matched with the existing process model, and only can be processed to the terminal outlet in a one-step mode, and during the process, if the process does not meet the discharge condition, the process cannot be recycled, and if the process meets the discharge condition in advance, the process cannot be processed directly to the terminal.
Disclosure of Invention
The invention relates to the field of SCR denitration technology in tail gas, in particular to a process method for SCR denitration in tail gas of a solid alkali furnace.
The invention provides a process method for SCR denitration in tail gas of a solid caustic soda furnace, which comprises the following steps:
1) And ammonia water with the mass concentration of 20% is used as a denitration reducing agent.
2) The catalyst material is generally V 2 O 5 -WO 3 (MoO 3)/TiO 2, the temperature range of the medium-low temperature catalyst used in the invention is between 230 and 350 ℃.
3) Each SCR reactor is provided with 1 layer of catalyst, and 1 set of SCR reactor is arranged at the outlet of a combustion-supporting air heat exchanger of the solid alkali molten salt furnace.
4) The SCR reactor adopts a plurality of layers of cascade use, 1 acoustic wave soot blower and a flue gas purification device are respectively arranged above each layer of catalyst, and if parameters of a single SCR reactor reach design and outlet calibration indexes, the parameters can be automatically determined to be in the next production procedure or be returned to the bottom SCR reactor for a plurality of times through sampling detection.
5) The differential pressure of the bottom catalyst is 0-400 Pa, the differential pressure of the middle catalyst is 0-350 Pa, and the differential pressure of the top catalyst is 0-380 Pa, so that the total resistance is lower than 600Pa.
6) The pressure of the atomization compressed air pipe is 0.18-0.50 MPa
7) The liquid level of the ammonia water storage tank is kept between 0.50 and 0.65m to replenish ammonia water in time.
8) The flue gas passes through a combustion-supporting air heat exchanger and a catalyst bed layer in sequence in a one-way mode, and the temperature of the flue gas isThe temperature of the flue gas must be 240-520 ℃; SO 2 The concentration is 0-20 mg/Nm 3 The gas flow rate is 8000-14000 Nm/h, and the water content in the flue gas is 6% VOL.
9) And (4) enabling the flue gas to enter the SCR reactor from bottom to top for denitration.
11 Each step of flue gas analysis after denitration of the SCR reactor can be selected to enter any section at any time for return treatment or directly enter a terminal pipeline.
12 Ammonia water regulating valve will regulate the ammonia injection amount according to the concentration of NOx at SCR outlet to ensure that the concentration of NOx at chimney outlet is not higher than 50mg/Nm 3 。
13 The concentration of nitrogen oxides NOx at the outlet of the SCR reactor and the flow rate of ammonia water are gradually increased, the opening of an ammonia spraying manual valve is gradually increased, and when the concentration of an ammonia spraying analyzer is more than 3ppm or the content of the NOx at the outlet is not obviously changed, ammonia spraying is stopped.
14 When the ammonia leakage instrument alarms abnormally, the temperature transmitter of the ammonia tank is less than or equal to 40 ℃, and the spraying device is started.
15 Further, in the step 8, when the inlet flue gas temperature of the SCR reactor is lower than 240 ℃, strictly opening and strictly starting the denitration device is prohibited. When the temperature of the inlet flue gas is higher than 230 ℃ but not higher than 350 ℃, the pressure of the atomized compressed air pipe is adjusted to be 0.18-0.25 MPa; when the inlet flue gas temperature is higher than 250 ℃ but not higher than 350 ℃, the pressure of the atomized compressed air main pipe is 0.40-0.50 MPa, and the load range of the flue gas flow rate of more than 50% is determined.
16 Further, in the step 8, when the inlet flue gas temperature of the SCR reactor exceeds 520 ℃, the inlet flue gas temperature is too high and exceeds the highest temperature which can be borne by the catalyst in the system, and the denitration system and the shutdown furnace system can be shut down in a chain manner.
17 Preferably, after the denitration efficiency is stabilized at 40% in the above steps, calibrating the instrument by using standard gas, and after the denitration efficiency reaches 60% of a design value normally, checking the control logic of the ammonia gas flow regulating valve, putting the regulating valve into a control target of automatically increasing and reducing the concentration of nitrogen oxide NOx at the reaction outlet, and optimizing the automatic control of the ammonia gas flow regulating valve.
18 Preferably, in the above steps, the control parameters include uniform distribution of NOx and NH3, concentration of nitrogen oxide NOx at the reaction outlet of the SCR reactor, and ammonia slip rate as auxiliary control parameters, and when the load of the alkali-fixation furnace is rapidly changed after the load is reduced from 100% to 30% after ammonia flow control is put into operation, the denitration system should respond rapidly.
The device of the denitration process realized by the SCR denitration process method in the tail gas of the solid alkali furnace mainly comprises a solid alkali molten salt furnace, an igniter, a combustion-supporting fan, a combustion-supporting air heat exchanger, an ammonia liquid siphon device control valve, an ammonia liquid siphon device, an air storage tank, a rotary SCR reaction device, an exhaust main pipe, an acoustic wave soot blower, a flue gas purification device, an emptying device and a detection sampling port, wherein the outlet of the solid alkali molten salt furnace is provided with the igniter, the combustion-supporting air heat exchanger and the combustion-supporting fan, the outlet of the combustion-supporting air heat exchanger is provided with the ammonia liquid siphon device and the rotary SCR reaction device, the outlet pipe of the ammonia liquid siphon device is connected with the control valve of the ammonia liquid siphon device, the inlet end of the rotary SCR reaction device is provided with the ammonia liquid device, the outlet end of the rotary SCR reaction device is provided with the exhaust main pipe, the acoustic wave soot blower, the flue gas purification device, the exhaust device and the detection sampling port, the rotary SCR reaction device is sequentially connected in an ascending cyclone type by a bottom SCR reaction device, a middle-layer SCR reaction device, a top layer and an SCR reaction device, and an automatic control regulating valve is arranged at a terminal outlet.
The ammonia liquid siphon device is composed of an ammonia liquid siphon tank, a rotary sprayer, an ammonia liquid siphon tank top, a liquid seal tank, an ammonia mass concentration online analyzer, an ammonia liquid outlet pump, an ammonia liquid inlet pump and an ammonia liquid storage tank.
The inside rotary sprayer that has of ammoniacal liquor siphon jar is provided with the motor drive inside by ammoniacal liquor siphon jar lower part and rotates, and ammoniacal liquor siphon jar outer wall is provided with ammonia mass concentration on-line analyzer, ammoniacal liquor goes out liquid pump, ammoniacal liquor feed pump to link to each other with the ammoniacal liquor basin through two pumps, there is liquid seal tank 64 on ammoniacal liquor siphon tank deck upper portion.
The internal rotation type sprayer comprises an internal rotation type spraying shaft, an upper bearing set, an upper bearing seat and a sealing device, a water inlet jacket, a water inlet pipe, internal rotation type spraying blades, spraying holes, a lower bearing seat and a sealing device, an upper bearing set and a water outlet pipe, wherein the water inlet jacket is arranged on the outer ring of the outer diameter of the internal rotation type spraying shaft.
The internal rotation type spraying blades are arranged on the outer wall of the water inlet jacket on the outer wall of the internal rotation type spraying shaft, and the interval between every two internal rotation type spraying blades is 150mm.
The inner diameter of the spraying hole is uniformly distributed along the whole internal rotation type spraying blade, 8 spraying holes are formed in the tangential direction of an angle of 45 degrees along the circumference, the diameter of the spraying hole is 15mm, and a passage is formed between the spraying hole and the water inlet jacket.
The bottom SCR reaction device comprises a bottom SCR reactor, a catalyst bed and a catalyst in the SCR reactor, a flue gas purification device, a tower layer sieve plate, an acoustic soot blower, a detection sampling port, a bottom layer automatic backflow regulating valve and a top layer terminal automatic regulating valve from bottom to top, wherein the inside of the flue gas purification device is provided with the tower layer sieve plate.
The middle-layer SCR reaction device comprises a middle-layer SCR reactor, a catalyst bed and a catalyst in the SCR reactor, a flue gas purification device, a tower layer sieve plate, an acoustic soot blower, a detection sampling port, a bottom layer automatic backflow regulating valve and a top layer terminal automatic regulating valve from bottom to top, wherein the tower layer sieve plate is arranged in the flue gas purification device.
The top layer SCR reaction device comprises a top layer SCR reactor, a catalyst bed and a catalyst in the SCR reactor, a flue gas purification device, a tower layer sieve plate, an acoustic wave soot blower, a detection sampling port, a bottom layer automatic backflow regulating valve and a top layer terminal automatic regulating valve from bottom to top, wherein the inside of the flue gas purification device is provided with the tower layer sieve plate.
The tower layer sieve plate in the flue gas purification device is provided with purification and adsorption catalyst particles.
The invention has the beneficial effects that: the rotary SCR reaction device is formed by sequentially and progressively connecting a bottom SCR reaction device, a middle SCR reaction device and a top SCR reaction device in a cyclone manner, the SCR reaction devices at each layer are provided with backflow and automatic control regulating valves to a terminal outlet, the outlet end of the rotary SCR reaction device is provided with a venting main pipe, an acoustic wave soot blower, a flue gas purification device, a venting device and a detection sampling port, nitrogen oxides in tail gas of a solid alkali furnace can be effectively removed, and in addition, the rotary SCR reaction device is additionally provided with a nitrogen oxide removal deviceThe water flows back to a control valve of the terminal, can return to any circulation loop after detecting and sampling the system, and is directly discharged after reaching the standard after reaching the initial bottom layer or the top layer of the terminal; the inlet end of the rotary SCR reaction device is provided with an ammonia liquid siphon device, ammonia water with 20% mass concentration can be used as a denitration reducing agent, an ammonia water regulating valve can regulate the ammonia spraying amount according to the concentration of NOx in an SCR outlet, and the concentration of NOx in an outlet of a chimney is ensured not to be higher than 50mg/Nm 3 . The concentration of nitrogen oxide NOx and the flow of ammonia water at the outlet of an SCR reactor are gradually increased, the opening of an ammonia spraying manual valve is gradually increased, ammonia spraying is stopped when the concentration of an ammonia spraying analyzer is more than 3ppm or the content of the NOx at the outlet is not obviously changed, when an ammonia leakage analyzer alarms abnormally, an ammonia tank temperature transmitter is less than or equal to 40 ℃, a peripheral whole ammonia system spraying device is started, the system is safe and reliable, and the design of a rotary sprayer can effectively spray and rotatably cool so as to ensure that the temperature and the mass concentration of ammonia liquid in an ammonia liquid siphon device are uniform, and a plurality of problems provided in the background can be solved.
Drawings
FIG. 1 is a schematic diagram of an apparatus and a process for SCR denitration process in tail gas of a soda-fixing furnace according to an embodiment of the present invention;
FIG. 2 is a schematic view of the ammonia siphon apparatus of FIG. 1.
Fig. 3 is a schematic view of the internal rotation sprayer of fig. 1.
Fig. 4 is a schematic view of the internal rotation type spray blade and the spray hole device in fig. 1.
Fig. 5 is a schematic view of the rotary SCR reactor shown in fig. 1.
In fig. 1 and 2: 1 is a solid alkali molten salt furnace; 2 is an igniter; 3 is a combustion fan; 4 is a combustion air heat exchanger; 5 is ammonia liquid siphon device control valve; 6 is ammonia liquid siphon device; 7 is an air storage tank; 8 is a rotary SCR reaction device; 11 is a emptying header pipe; 10 is a sound wave soot blower; 11 is a flue gas purification device; 12 is an emptying device; and 13 is a detection sampling port.
In fig. 2, 3, 4: 61 is an ammonia siphon tank; 62 is an internal rotation type sprayer; 63 is the ammonia liquid siphon tank top; 64 is a liquid seal tank; 65 is an ammonia mass concentration on-line analyzer; 66 is an ammonia liquid outlet pump; 67 is an ammonia liquor inlet pump; 68 is an ammonia liquid storage tank.
62 is an internal rotation type sprayer; 621 is an internal rotation type spraying shaft; 622, an upper bearing set; 623 an upper bearing seat and a sealing device; 624 is a water inlet jacket; 625, a water inlet pipe; 626 is an internal rotation type spray blade; 627 is a spray hole; 628 is a lower bearing seat and a sealing device; 629 is an upper bearing set; 630 is a water outlet pipe.
In FIG. 5: 81 is a bottom SCR reaction device; 82 is a middle-layer SCR reaction device; 83 is a top layer SCR reaction device;
811 is a bottom layer SCR reactor; 812 is a catalyst bed and a catalyst in the SCR reactor; 813 is a flue gas purification device; 814 is a tower layer sieve plate; 815 is a sound wave soot blower; 816 is a detection sampling port; 817 is a bottom automatic backflow regulating valve; 818 is the top terminal self-regulating valve.
821 is a middle layer SCR reactor; 822 is the catalyst bed and catalyst in SCR reactor; 823 is a flue gas purification device; 824 is a tower layer sieve plate; 825 is a sound wave soot blower; 826 is a detection sampling port; 827 is bottom automatic reflux adjusting valve; 828 is a top terminal self-regulating valve.
831 is a top layer SCR reactor; 832 catalyst bed and catalyst in the SCR reactor; 833 is a flue gas cleaning device; 834 is a tower layer sieve plate; 835 is a sound wave soot blower; 836 is a detection sampling port; 837 is a bottom automatic reflux adjusting valve; 828 is a top terminal self-regulating valve.
Detailed Description
In order to explain the technical content, the objects and the effects of the present invention in detail, the following description will be given with reference to the embodiments.
Referring to the attached drawings 1-5, in order to achieve the above purpose, the embodiment 1 of the invention provides a comprehensive utilization method of phosphorus-containing wastewater, which is implemented by taking acetylene gas cleaning wastewater in a calcium carbide method PVC production process as an example, and aims to overcome the defects of the prior art and realize a process method for treating and subsequently producing and recycling the phosphorus-containing wastewater, and the method comprises the following steps:
the invention relates to the field of SCR denitration technology in tail gas, in particular to a process method for SCR denitration in tail gas of a solid alkali furnace.
The invention provides a process method for SCR denitration in tail gas of a solid caustic soda furnace, which comprises the following steps:
1) And ammonia water with the mass concentration of 20% is used as a denitration reducing agent.
2) The catalyst material is generally V2O5-WO3 (MoO 3)/TiO 2, and the suitable temperature range of the medium-low temperature catalyst used in the invention is 230-350 ℃.
3) Each SCR reactor is filled with 1 layer of catalyst, and 1 set of SCR reactor is arranged at the outlet of a combustion-supporting air heat exchanger of the solid alkali molten salt furnace.
4) The SCR reactor adopts a plurality of layers of cascade use, 1 acoustic wave soot blower and a flue gas purification device are respectively arranged above each layer of catalyst, and if parameters of a single SCR reactor reach design and outlet calibration indexes, the parameters can be automatically determined to be in the next production procedure or be returned to the bottom SCR reactor for a plurality of times through sampling detection.
5) The differential pressure of the bottom catalyst is 0-400 Pa, the differential pressure of the middle catalyst is 0-350 Pa, and the differential pressure of the top catalyst is 0-380 Pa, so that the total resistance is lower than 600Pa.
6) The pressure of the atomization compressed air pipe is 0.18-0.50 MPa
7) The liquid level of the ammonia water storage tank is kept between 0.50 and 0.65m, and then ammonia water is required to be supplemented in time.
8) The flue gas passes through a combustion air heat exchanger and a catalyst bed layer in sequence in a unidirectional mode, and the temperature of the flue gas is that the temperature of the flue gas must be 240-520 ℃; SO (SO) 2 The concentration is 0-20 mg/Nm 3 The necessary flue gas flow is 8000-14000 Nm/h 8000, and the water content in the flue gas is 6 percent VOL.
9) And enabling the flue gas to enter the SCR reactor from bottom to top for denitration.
11 The flue gas is analyzed in each step after denitration is carried out on the SCR reactor, and the flue gas can be selectively sent to any section to be returned for treatment at any time or directly sent to a terminal pipeline.
12 Ammonia water regulating valve will adjust the ammonia injection amount according to the concentration of nitrogen oxide NOx at the outlet of SCR, and ensure that the concentration of NOx at the outlet of chimney is not higher than 50mg/Nm3.
14 The concentration of nitrogen oxide NOx at the outlet of the SCR reactor and the flow rate of ammonia water are gradually increased, and ammonia injection is stopped when the concentration of an ammonia injection analyzer is more than 3ppm or the content of the outlet NOx is not obviously changed.
15 When the ammonia leakage instrument gives an alarm, the temperature transmitter of the ammonia tank is less than or equal to 40 ℃, and the spraying device is started.
16 Further, in the step 8, when the inlet flue gas temperature of the SCR reactor is lower than 240 ℃, strictly opening the denitration device. When the temperature of the inlet flue gas is higher than 230 ℃ but not higher than 350 ℃, the pressure of the atomized compressed air pipe is adjusted to be 0.18-0.25 MPa; when the inlet flue gas temperature is higher than 250 ℃ but not higher than 350 ℃, the pressure of the atomizing compressed air main pipe is 0.40-0.50 MPa, and the load range of flue gas flow rate is determined to be more than 50%.
17 Further, in the step 8, when the inlet flue gas temperature of the SCR reactor exceeds 520 ℃, the inlet flue gas temperature is too high and exceeds the highest temperature which can be borne by the catalyst in the system, and the denitration system and the shutdown furnace system can be shut down in a chain manner.
18 Preferably, after the denitration efficiency is stabilized at 40% in the above steps, calibrating the instrument by using standard gas, and after the denitration efficiency reaches 60% of a design value normally, checking the control logic of the ammonia gas flow regulating valve, putting the regulating valve into a control target of automatically increasing and reducing the concentration of nitrogen oxide NOx at the reaction outlet, and optimizing the automatic control of the ammonia gas flow regulating valve.
19 Preferably, in the above steps, the control parameters include uniform distribution of NOx and NH3, concentration of nitrogen oxide NOx at the reaction outlet of the SCR reactor, and ammonia slip rate as auxiliary control parameters, and when the load of the alkali-fixation furnace is rapidly changed after the load is reduced from 100% to 30% after ammonia flow control is put into operation, the denitration system should respond rapidly.
The device for realizing the denitration process by the SCR denitration process method in the tail gas of the solid alkali furnace mainly comprises a solid alkali molten salt furnace 1, an igniter 2, a combustion fan 3, a combustion air heat exchanger 4, an ammonia liquid siphon device control valve 5, an ammonia liquid siphon device 6, an air storage tank 7, a rotary SCR reaction device 8, an emptying header pipe 9, an acoustic wave soot blower 10, a flue gas purification device 11, an emptying device 12 and a detection sampling port 13, wherein the igniter 2, the combustion air heat exchanger 4 and the combustion fan 3 are arranged at the outlet of the solid alkali molten salt furnace 1, the ammonia liquid siphon device 6 and the rotary SCR reaction device 8 are arranged at the outlet of the combustion air heat exchanger 4, the outlet pipe of the ammonia liquid siphon device 6 is connected with the ammonia liquid siphon device control valve 5, the ammonia liquid siphon device 6 is arranged at the inlet end of the rotary SCR reaction device 8, the emptying header pipe 9, the acoustic wave soot blower 10, the flue gas purification device 11, the emptying device 12 and the detection sampling port 13 are arranged at the outlet of the rotary SCR reaction device 8, and the rotary SCR reaction device 81, the top layer SCR reaction device 82 and the SCR sequential SCR reaction device inlet regulating valve are connected with the bottom layer.
The ammonia liquid siphon device 6 comprises an ammonia liquid siphon tank 61, a rotary sprayer 62, an ammonia liquid siphon tank top 63, a liquid seal tank 64, an ammonia mass concentration online analyzer 65, an ammonia liquid outlet pump 66, an ammonia liquid inlet pump 67 and an ammonia liquid storage tank 68.
A rotary sprayer 62 is arranged in the ammonia liquid siphon tank 61, the lower portion of the ammonia liquid siphon tank 61 is provided with a motor for driving the rotary sprayer 62 in the ammonia liquid siphon tank to rotate, the outer wall of the ammonia liquid siphon tank 61 is provided with an ammonia mass concentration online analyzer 65, an ammonia liquid outlet pump 66 and an ammonia liquid inlet pump 67, the ammonia liquid outlet pump is connected with an ammonia liquid storage tank 68 through the two pumps, and a liquid seal tank 64 is arranged on the upper portion of the top 63 of the ammonia liquid siphon tank.
The internal rotation type sprayer 62 as described above is composed of an internal rotation type spraying shaft 621, an upper bearing set 622, an upper bearing seat and sealing device 623, a water inlet jacket 624, a water inlet pipe 625, an internal rotation type spraying blade 626, a spraying hole 627, a lower bearing seat and sealing device 628, an upper bearing set 629 and a water outlet pipe 630, wherein the water inlet jacket 624 is arranged on the outer ring of the outer diameter of the internal rotation type spraying shaft 621.
The inward rotating type shower blades 626 are provided on the outer wall of the water inlet jacket 624 on the outer wall of the inward rotating type shower shaft 621, and the intervals between the inward rotating type shower blades 626 are 150mm.
The inner diameter of the spraying holes 627 is uniformly distributed along the inner rotary type spraying blade 626 in a whole piece manner, 8 spraying holes are arranged along the tangential direction of an angle of 45 degrees of the circumference, the diameter of each spraying hole 627 is 15mm, and a passage is formed between each spraying hole 627 and the water inlet jacket 624.
The bottom layer SCR reaction device 81 comprises a bottom layer SCR reactor 811, a catalytic bed and catalyst 812 in the SCR reactor, a flue gas purification device 813, a tower layer sieve plate 814, an acoustic wave soot blower 815, a detection sampling port 816, a bottom layer automatic backflow regulating valve 817 and a top layer terminal automatic regulating valve 818 from bottom to top, wherein the tower layer sieve plate 814 is arranged in the flue gas purification device 813.
The middle-layer SCR reaction device 82 comprises a middle-layer SCR reactor 821, a catalytic bed and catalyst 822 in the SCR reactor, a flue gas purification device 823, a tower-layer sieve plate 824, a sonic soot blower 825, a detection sampling port 826, a bottom-layer automatic backflow regulating valve 827, and a top-layer terminal automatic regulating valve 828 from bottom to top, wherein the inside of the flue gas purification device 823 is provided with the tower-layer sieve plate 824.
The top-layer SCR reactor 83 is composed of a top-layer SCR reactor 831, a catalytic bed and catalyst 832 in the SCR reactor, a flue gas purification device 833, a tower-layer sieve plate 834, an acoustic soot blower 835, a detection sampling port 836, a bottom-layer automatic backflow regulating valve 837, a top-layer terminal automatic regulating valve 838 from bottom to top, and the inside of the flue gas purification device 833 is provided with the tower-layer sieve plate 834.
The tower layer sieve plate in the flue gas purification device is provided with purification and adsorption catalyst particles.
The invention has the beneficial effects that: furnace gas generated by a solid alkali molten salt furnace 1 and an igniter 2 passes through a combustion fan 3, a combustion air heat exchanger 4 to an ammonia liquid siphon device control valve 5, an ammonia liquid siphon device 6, an air storage tank 7, a rotary SCR reaction device 8 to a vent header pipe 9, a sound wave soot blower 10, a flue gas purification device 11, a vent device 12 and a detection sampling port 13, wherein the outlet of the solid alkali molten salt furnace 1 is provided with the igniter 2 and the combustion air heat exchanger 4, and the combustion fan 3 rotary SCR reaction device 8 is connected in a cyclone manner by a bottom layer SCR reaction device 81, a middle layer SCR reaction device 82 and a top layer SCR reaction device 83 in a sequential progressive manner, each layer SCR reaction device is provided with a backflow and terminal outlet automatic control regulating valve, the outlet end of the rotary SCR reaction device 8 is provided with the vent header pipe 9, the sound wave soot blower 10, the flue gas purification device 11, the vent device 12 and the detection sampling port 13, nitrogen oxides in tail gas of the solid alkali furnace can be effectively removed, and a control valve which flows back to a terminal is added, and can be detected and sampled by the system to any loop, and is discharged to the top layer of the system and directly reach the standard after the initial bottom layer or the top layer; the entrance point of the rotary SCR reaction device 8 is provided with an ammonia liquid siphon device 6, ammonia water with 20% mass concentration can be used as a denitration reducing agent, an ammonia water regulating valve can regulate the ammonia spraying amount according to the concentration of NOx at the outlet of the SCR, and the concentration of NOx at the outlet of a chimney is not higher than 50mg/Nm3. The concentration of nitrogen oxide NOx and the ammonia water flow at the outlet of the SCR reactor are gradually increased, the opening of an ammonia spraying manual valve is gradually increased, ammonia spraying is stopped when the concentration of an ammonia spraying analyzer is more than 3ppm or the content of the NOx at the outlet is not obviously changed, when an ammonia leakage analyzer alarms abnormally, a temperature transmitter of an ammonia tank is less than or equal to 40 ℃, a peripheral whole ammonia system spraying device is started, the system is safe and reliable, and the design of a rotary sprayer can effectively spray and rotatably cool to ensure that the temperature and the mass concentration of ammonia liquid in an ammonia liquid siphon device are uniform, the operation is convenient, and the method is suitable for industrial application compared with the traditional process.
While the foregoing is directed to the preferred embodiment of the present invention, it will be understood that it is not intended to be exhaustive or to limit the invention to the precise form disclosed, and that various modifications and adaptations may be resorted to without departing from the principles of the invention and are intended to those skilled in the art by virtue of the fact that the invention is described in detail and with the understanding that various embodiments of the invention are suited to the particular use contemplated.
Claims (15)
1. A process method for SCR denitration in solid caustic soda furnace tail gas is characterized by comprising the following steps: the tail gas of the solid caustic soda furnace is subjected to an SCR denitration process, and comprises the following steps:
1) Ammonia water with the mass concentration of 20% is used as a denitration reducing agent;
2) The catalyst material is generally V 2 O 5 -WO 3 (MoO 3 )/TiO 2 The suitable temperature range of the medium-low temperature catalyst used in the invention is 230-350 ℃;
3) 1 layer of catalyst is filled in each SCR reactor, and 1 set of SCR reactor is arranged at the outlet of a combustion-supporting air heat exchanger of the solid alkali molten salt furnace;
4) The SCR reactor adopts a plurality of layers of cascade use, 1 acoustic wave soot blower and a flue gas purification device are respectively arranged above each layer of catalyst, and if the parameters of a single SCR reactor reach design and outlet calibration indexes, the parameters can be automatically determined to be in the next production procedure or returned to the bottom SCR reactor for a plurality of times through sampling detection;
5) The differential pressure of the bottom catalyst is 0-400 Pa, the differential pressure of the middle catalyst is 0-350 Pa, and the differential pressure of the top catalyst is 0-380 Pa, so that the total resistance is lower than 600Pa;
6) The pressure of the atomization compressed air pipe is 0.18-0.50 MPa;
7) The liquid level of the ammonia water storage tank is kept between 0.50 and 0.65m to supplement ammonia water in time;
8) The flue gas passes through a combustion air heat exchanger and a catalyst bed layer in one way, and the temperature of the flue gas is that the temperature of the flue gas must be 240-520 ℃; SO 2 The concentration is 0-20 mg/Nm 3 The flow rate of the flue gas is 8000-14000 Nm/h, and the water content in the flue gas is 6% VOL;
9) Flue gas enters the SCR reactor from bottom to top for denitration;
11 Each step of flue gas analysis after denitration of the SCR reactor can be selected to enter any section at any time for return treatment or directly enter a terminal pipeline;
12 Ammonia water regulating valve will regulate the ammonia injection amount according to the concentration of NOx at SCR outlet to ensure that the concentration of NOx at chimney outlet is not higher than 50mg/Nm 3 ；
13 ) the concentration of nitrogen oxides NOx at the outlet of the SCR reactor and the flow rate of ammonia water are gradually increased, the opening of an ammonia spraying manual valve is gradually increased, and when the concentration of an ammonia spraying analyzer is more than 3ppm or the content of the NOx at the outlet is not obviously changed, ammonia spraying is stopped;
14 When the ammonia leakage instrument gives an alarm, the temperature transmitter of the ammonia tank is less than or equal to 40 ℃, and the spraying device is started.
2. The SCR denitration process method in the tail gas of the solid caustic soda furnace according to claim 1, which is characterized in that: in the step 8, when the temperature of the flue gas at the inlet of the SCR reactor is lower than 240 ℃, opening a denitration device strictly forbidden is forbidden; when the temperature of the inlet flue gas is higher than 230 ℃ but not higher than 350 ℃, the pressure of the atomized compressed air pipe is adjusted to be 0.18-0.25 MPa; when the inlet flue gas temperature is higher than 250 ℃ but not higher than 350 ℃, the pressure of the atomizing compressed air main pipe is 0.40-0.50 MPa, and the load range of flue gas flow rate is determined to be more than 50%.
3. The SCR denitration process method in the tail gas of the solid caustic soda furnace according to claim 1, which is characterized in that: in the step 8, when the inlet flue gas temperature of the SCR reactor exceeds 520 ℃, the inlet flue gas temperature is too high and exceeds the highest temperature which can be borne by a catalyst in the system, and the denitration system and the off-stream furnace system can be shut down in a linkage manner.
4. The SCR denitration process method in the tail gas of the solid caustic soda furnace according to claim 1, which is characterized in that: and (3) after the denitration efficiency is stabilized at 40% in any step of the steps 1 to 14, calibrating the instrument by using standard gas, checking the control logic of the ammonia gas flow regulating valve when the denitration efficiency reaches 60% of a design value after normal operation, putting the regulating valve into automation, increasing and reducing the control target of the concentration of nitrogen oxide NOx at a reaction outlet, and optimizing the automatic control of the ammonia gas flow regulating valve.
5. The SCR denitration process method in the tail gas of the solid caustic soda furnace according to claim 1, which is characterized in that: the parameters of the above steps are controlled by NOx and NH 3 The distribution is even, the concentration of nitrogen oxides NOx and the ammonia escape rate at the reaction outlet of the SCR reactor are used as auxiliary control parameters, and after the ammonia flow is controlled and put into operation, the load is reduced from 100% to 30%, and when the load of the alkali fixing furnace is changed rapidly, the denitration system can respond rapidly.
6. The production device for realizing the SCR denitration process method in the tail gas of the soda-fixing furnace according to claim 1, which is characterized in that: the denitration process device mainly comprises a solid alkali molten salt furnace, an igniter, a combustion-supporting fan, a combustion-supporting air heat exchanger, an ammonia liquid siphon device control valve, an ammonia liquid siphon device, an air storage tank, a rotary SCR (selective catalytic reduction) reaction device, an air discharge header pipe, an acoustic wave soot blower, a flue gas purification device, a venting device and a detection sampling port, wherein the igniter, the combustion-supporting air heat exchanger and the combustion-supporting fan are arranged at an outlet of the solid alkali molten salt furnace, the ammonia liquid siphon device and the rotary SCR reaction device are arranged at an outlet of the combustion-supporting air heat exchanger, an outlet pipe of the ammonia liquid siphon device is connected with the ammonia liquid siphon device control valve, the ammonia liquid siphon device is arranged at an inlet end of the rotary SCR reaction device, the venting header pipe, the acoustic wave soot blower, the flue gas purification device, the venting device and the detection sampling port are arranged at an outlet end of the rotary SCR reaction device, the top layer SCR reaction device is sequentially connected in a stepped manner through the bottom layer SCR reaction device, the middle layer SCR reaction device and the SCR reaction device, and the SCR reaction device at each layer is provided with a backflow and an automatic control regulating valve to a terminal outlet.
7. The production device for realizing the SCR denitration process method in the tail gas of the soda-fixing furnace according to claim 6, which is characterized in that: the ammonia liquid siphon device is composed of an ammonia liquid siphon tank, a rotary sprayer, an ammonia liquid siphon tank top, a liquid seal tank, an ammonia mass concentration online analyzer, an ammonia liquid outlet pump, an ammonia liquid inlet pump and an ammonia liquid storage tank.
8. The production device for realizing the SCR denitration process method in the tail gas of the soda-fixing furnace according to claim 6, which is characterized in that: the ammonia siphon tank is internally provided with a rotary sprayer, the lower part of the ammonia siphon tank is provided with a motor for driving the inner rotary sprayer to rotate, the outer wall of the ammonia siphon tank is provided with an ammonia mass concentration online analyzer, an ammonia liquid outlet pump and an ammonia liquid inlet pump, the ammonia liquid outlet pump and the ammonia liquid inlet pump are connected with an ammonia liquid storage tank through two pumps, and the upper part of the top of the ammonia siphon tank is provided with a liquid seal tank.
9. The production device for realizing the SCR denitration process method in the tail gas of the soda-fixing furnace according to claim 7, which is characterized in that: the internal rotation type sprayer comprises an internal rotation type spraying shaft, an upper bearing sleeve, an upper bearing seat and sealing device, a water inlet jacket, a water inlet pipe, internal rotation type spraying blades, spraying holes, a lower bearing seat and sealing device, an upper bearing sleeve and a water outlet pipe, wherein the water inlet jacket is arranged on the outer ring of the outer diameter of the internal rotation type spraying shaft.
10. The production device for realizing the SCR denitration process method in the tail gas of the soda-fixing furnace according to claim 9, which is characterized in that: the internal rotation type spraying blades are arranged on the outer wall of the water inlet jacket on the outer wall of the internal rotation type spraying shaft, and the interval between every two internal rotation type spraying blades is 150mm.
11. The production device for realizing the SCR denitration process method in the tail gas of the soda-fixing furnace according to claim 10, which is characterized in that: the spraying hole inner diameter along the whole piece equipartition of internal rotation formula spraying blade 8 and along 45 degree angle tangential direction of circumference, the spraying hole diameter is 15mm, presss from both sides the cover with the water inlet and forms the route.
12. The production device for realizing the SCR denitration process method in the tail gas of the soda-fixing furnace according to the claim 5, is characterized in that: the bottom SCR reaction device consists of a bottom SCR reactor, a catalyst bed and a catalyst in the SCR reactor, a flue gas purification device, a tower layer sieve plate, an acoustic wave soot blower, a detection sampling port, a bottom layer automatic backflow regulating valve and a top layer terminal automatic regulating valve from bottom to top, wherein the inside of the flue gas purification device is provided with the tower layer sieve plate.
13. The production device for realizing the SCR denitration process method in the tail gas of the soda-fixing furnace according to the claim 5, is characterized in that: the middle-layer SCR reaction device consists of a middle-layer SCR reactor, a catalyst bed and a catalyst in the SCR reactor, a flue gas purification device, a tower layer sieve plate, an acoustic wave soot blower, a detection sampling port, a bottom layer automatic backflow regulating valve and a top layer terminal automatic regulating valve from bottom to top, wherein the inside of the flue gas purification device is provided with the tower layer sieve plate.
14. The production device for realizing the SCR denitration process method in the tail gas of the soda-fixing furnace according to claim 5, which is characterized in that: the top layer SCR reaction device comprises a bottom layer SCR reactor, a catalyst bed and a catalyst in the SCR reactor, a flue gas purification device, a tower layer sieve plate, an acoustic wave soot blower, a detection sampling port, a bottom layer automatic backflow regulating valve and a top layer terminal automatic regulating valve from bottom to top, wherein the inside of the flue gas purification device is provided with the tower layer sieve plate.
15. The production device for realizing the SCR denitration process method in the tail gas of the soda-fixing furnace according to claim 5, which is characterized in that: the tower layer sieve plate in the flue gas purification device is provided with purification and adsorption catalyst particles.
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