CN110314499B - Pilot scale system of denitration technology of catalytic reduction regeneration is absorbed in coordination to complex - Google Patents

Pilot scale system of denitration technology of catalytic reduction regeneration is absorbed in coordination to complex Download PDF

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CN110314499B
CN110314499B CN201910447663.0A CN201910447663A CN110314499B CN 110314499 B CN110314499 B CN 110314499B CN 201910447663 A CN201910447663 A CN 201910447663A CN 110314499 B CN110314499 B CN 110314499B
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catalytic reduction
complexing
liquid
denitration
reduction reaction
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CN110314499A (en
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邓军
张国孟
石瑞
夏亮
王逸
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Shanghai Hengyuan Marine Equipment Co ltd
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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
    • B01D53/14—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 by absorption
    • 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
    • B01D53/14—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 by absorption
    • B01D53/1425—Regeneration of liquid absorbents
    • 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
    • B01D53/14—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 by absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/005—Separating solid material from the gas/liquid stream
    • B01J8/006—Separating solid material from the gas/liquid stream by filtration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/90—Chelants
    • B01D2251/902—EDTA
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/502—Carbon monoxide

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  • Engineering & Computer Science (AREA)
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  • General Chemical & Material Sciences (AREA)
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  • Organic Chemistry (AREA)
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Abstract

The invention provides a pilot-scale test system for a denitration process by complexing absorption and catalytic reduction regeneration, which comprises a denitration packed tower, a complexing liquid tank, catalytic reduction reaction equipment, an air compressor and a heat exchanger, wherein the denitration packed tower is connected with the catalytic reduction reaction equipment; pumping the complexing liquid out of the complexing liquid tank through a spray pump, and then spraying the complexing liquid out of a spray layer in the denitration packed tower after heat exchange of a heat exchanger; falls to the packing layer below; NOx in the flue gas in the filler layer is fully contacted and absorbed with the complexing liquid, the complexing liquid after absorbing the NOx is conveyed into a catalytic reduction reaction device through a pipeline to be reduced and regenerated, the catalytic reduction reaction device reduces and regenerates the complexing liquid by utilizing a palladium-carbon catalyst, formic acid and sodium formate system, and a filter layer is arranged in the catalytic reduction reaction device and is used for filtering the reduced liquid to obtain reusable complexing liquid; the air compressor introduces the manufactured compressed gas into the catalytic reduction reaction equipment through a gas distributor arranged in the catalytic reduction reaction equipment, and the palladium-carbon catalyst and the complexing liquid are filtered by using pressure.

Description

Pilot scale system of denitration technology of catalytic reduction regeneration is absorbed in coordination to complex
Technical Field
The invention relates to the field of flue gas purification, in particular to a pilot-scale test system for a denitration process by complexing absorption, cooperating with catalytic reduction and regeneration.
Background
At present, a great amount of SOx, NOx and PM generated along with the combustion of fuel cause great pollution to the environment, and particularly, NOx can generate photochemical smog which brings serious harm to the work and life of people. It must be disposed of before being discharged. The SCR denitration technology is the mainstream technology for treating NOx at present, but the SCR catalyst produced in the industrialized production at present is sensitive to the requirement of the flue gas temperature and is divided into three intervals of high temperature, medium temperature and low temperature, and one catalyst can hardly cover all temperature intervals.
Disclosure of Invention
The invention provides a pilot-scale test system for a denitration process by complexing absorption and catalytic reduction regeneration, which adopts complexing liquid (Fe-EDTA) to complex and absorb NOx in flue gas without considering the temperature factor of the flue gas, and the absorbed complexing liquid can be recycled after catalytic reduction.
The pilot-scale system for the denitration process by complexing absorption, cooperating with catalytic reduction and regeneration provided by the embodiment of the invention comprises a denitration packed tower, a complexing liquid tank, catalytic reduction reaction equipment, an air compressor and a heat exchanger;
the denitration packed tower comprises: the device comprises a shell, wherein a smoke inlet is formed in the side surface of the shell, which is close to the bottom of the shell, and a smoke outlet is formed in the top of the shell; a spraying layer is arranged in the shell below the smoke outlet; a packing layer is arranged below the spraying layer; a liquid seal layer is arranged at the bottom of the shell;
the complex liquid tank is used for storing complex liquid, the complex liquid is pumped out of the complex liquid tank through a spray pump, and then the complex liquid is sprayed out of a spray layer in the denitration packed tower after heat exchange of a heat exchanger; falls to the packing layer below; NOx in the flue gas in the filler layer is fully contacted with the complexing liquid for absorption, the complexing liquid after absorbing the NOx is conveyed into a catalytic reduction reaction device through a pipeline for reduction and regeneration, the catalytic reduction reaction device utilizes a palladium-carbon catalyst, formic acid and sodium formate system to reduce and regenerate the complexing liquid, and a filter layer is arranged in the catalytic reduction reaction device and is used for filtering the reduced liquid to obtain reusable complexing liquid; the air compressor introduces the manufactured compressed gas into the catalytic reduction reaction equipment through a gas distributor arranged in the catalytic reduction reaction equipment, and the palladium-carbon catalyst and the complexing liquid are filtered by using pressure.
Wherein, NOx in the flue gas in the filler layer is fully contacted with the complexing liquid for absorption, and the method comprises the following steps:
the main equation for complex absorption is: fe2+EDTA+NO→Fe2+EDTA(NO)；
The main side reaction equation is: fe2+EDTA+O2→Fe3+EDTA。
Preferably, the complexing liquid is subjected to heat exchange to 40-50 ℃ through a heat exchanger.
Preferably, the liquid seal layer comprises a U-shaped bent pipe.
Wherein, the catalytic reduction reaction equipment utilizes a palladium-carbon catalyst, formic acid and sodium formate system to reduce and regenerate the complexing solution, and comprises:
the equation for the catalytic reduction reaction is:
Figure BDA0002074141680000021
Fe2+EDTA(NO)+[H]→Fe2+EDTA+N2↑+H2O、
Fe3+EDTA+[H]→Fe2+EDTA+H2O。
preferably, the filter layer comprises filter cloth with the pore diameter of 200-600 meshes.
Preferably, a heat-conducting oil coil heating system is arranged in the catalytic reduction reaction equipment, and the temperature of the heat-conducting oil coil heating system is 55-70 ℃.
In one embodiment, the catalytic reaction apparatus comprises:
the channel switching device comprises an input end and two output ends, and the input end is connected with a pipeline for conveying the complexing liquid after absorbing NOx;
the first catalytic reduction reactor is connected with one output end of the channel switching device;
and the second catalytic reduction reactor is connected with the other output end of the channel switching device.
Wherein the channel switching device includes: a first valve arranged at one of the outputs and a second valve arranged at the other output.
In one embodiment, the bottom end level of the denitration packed tower is higher than the top end level of the catalytic reduction reaction device; the bottom end horizontal surface of the catalytic reduction reaction equipment is higher than the top end horizontal surface of the complexing liquid tank.
In one embodiment, the pilot plant system for denitration process by complexing absorption in cooperation with catalytic reduction regeneration further comprises:
the gas flowmeter is arranged at a flue gas inlet of the shell and used for detecting the flow of flue gas entering the denitration packed tower;
the controller is connected with the gas flowmeter and the spray pump;
the controller obtains the flow of the flue gas through the gas flowmeter, and controls the spraying flow of the spraying pump to enable the liquid-gas ratio to be 1.5-4L/m3；
The controller calculates the staying time of the gas in the denitration packed tower according to the shell volume and the gas flow, and judges whether the staying time is within a preset range;
and when the air flow is not in the preset range, adjusting the air pumping speed of an air pump arranged at the front end of the gas flow meter.
Additional features and advantages of the invention will be set forth in the description which follows, and in part will be obvious from the description, or may be learned by practice of the invention. The objectives and other advantages of the invention will be realized and attained by the structure particularly pointed out in the written description and claims hereof as well as the appended drawings.
The technical solution of the present invention is further described in detail by the accompanying drawings and embodiments.
Drawings
The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention and not to limit the invention. In the drawings:
FIG. 1 is a schematic diagram of a pilot plant system of a denitration process by complex absorption in cooperation with catalytic reduction regeneration according to an embodiment of the present invention;
FIG. 2 is a schematic diagram of a denitration packed tower according to an embodiment of the present invention;
FIG. 3 is a schematic illustration of a catalytic reduction reactor according to an embodiment of the present invention;
FIG. 4 is a flow chart of a pilot plant system of a denitration process by complexing absorption in cooperation with catalytic reduction regeneration.
In the figure: 1. a complexing liquid tank; 2. a first valve; 3. a spray pump; 4. a second valve; 5. a heat exchanger; 6. a denitration packed tower; 7-1. a third valve; 7-2. a fifth valve; 8-1. a first catalytic reduction reactor; 8-2 a second catalytic reduction reactor; 9-1. a fourth valve; 9-2. a sixth valve; 10. a compressed air inlet; 11. a compressed air outlet; 14. an air compressor; 21. a housing; 22. a flue gas inlet; 23. a flue gas outlet; 24. a spray layer; 25. a filler layer; 26 liquid seal layer; 27. a complex liquid outlet; 31. a filter layer; 32. a heat conducting oil coil heating system; 33. a gas distributor.
Detailed Description
The preferred embodiments of the present invention will be described in conjunction with the accompanying drawings, and it will be understood that they are described herein for the purpose of illustration and explanation and not limitation.
The embodiment of the invention provides a pilot-scale system for a denitration process by complexing absorption and catalytic reduction regeneration, which comprises a denitration packed tower 6, a complexing liquid tank 1, catalytic reduction reaction equipment 8, an air compressor 14 and a heat exchanger 5, wherein the denitration packed tower is shown in figures 1, 2 and 3;
the denitration packed tower 6 comprises: the device comprises a shell 21, wherein a flue gas inlet 22 is formed in the side surface of the shell 21 close to the bottom, and a flue gas outlet 23 is formed in the top of the shell 21; a spraying layer 24 is arranged in the shell 21 below the smoke outlet 23; a packing layer 25 is arranged below the spraying layer 24; a liquid seal layer 26 is arranged at the bottom of the shell 21;
the complex liquid tank 1 is used for storing complex liquid, the complex liquid is pumped out of the complex liquid tank 1 through a spray pump 5, and then the complex liquid is sprayed out of a spray layer in the denitration packed tower 6 after heat exchange of a heat exchanger 5; falls to the packing layer 25 located below; the NOx in the flue gas in the filler layer 25 is fully contacted and absorbed with the complexing liquid, the complexing liquid after absorbing the NOx is conveyed into the catalytic reduction reaction device 8 through a pipeline for reduction and regeneration, the catalytic reduction reaction device 8 utilizes a palladium-carbon catalyst, formic acid and sodium formate system to reduce and regenerate the complexing liquid, and a filter layer 31 is arranged in the catalytic reduction reaction device 8 and is used for filtering the reduced liquid to obtain reusable complexing liquid; the air compressor 14 introduces the produced compressed gas into the catalytic reduction reaction device 8 through a gas distributor 33 arranged in the catalytic reduction reaction device 8, and filters the palladium-carbon catalyst and the complexing solution by using pressure.
Wherein, the sufficient contact absorption of NOx in the flue gas and the complexing liquid in the filler layer 25 comprises:
the main equation for complex absorption is: fe2+EDTA+NO→Fe2+EDTA(NO)；
The main side reaction equation is: fe2+EDTA+O2→Fe3+EDTA。
Preferably, the complexing liquid exchanges heat to 40-50 ℃ through a heat exchanger 5.
Preferably, the liquid seal layer 26 comprises a U-shaped bent pipe. One end of the U-shaped bend is arranged outside the catalytic reduction device and used for connecting a flue gas pipeline, the other end of the U-shaped bend is arranged below the liquid seal layer 26, and the height of the liquid seal layer 26 is positioned between two pipes of the U-shaped pipe; when the complexing liquid is used as the liquid seal layer 26, the height of the complexing liquid outlet 27 of the denitration packed tower 6 is higher than the smoke outlet of the U-shaped pipe. When the flue gas enters the denitration packed tower 6, the flue gas pushes out the liquid in the U-shaped pipeline, and after the flue gas enters the denitration packed tower 6, the liquid flows back into the U-shaped pipe; the flue gas is prevented from flowing back through the liquid seal.
Wherein, the catalytic reduction reaction device 8 uses palladium carbon catalyst, formic acid and sodium formate system to reduce and regenerate the complex liquid and comprises:
the equation for the catalytic reduction reaction is:
Figure BDA0002074141680000051
Fe2+EDTA(NO)+[H]→Fe2+EDTA+N2↑+H2O、
Fe3+EDTA+[H]→Fe2+EDTA+H2O。
preferably, the filter layer 31 includes filter cloth having a pore size of 200 to 600 meshes.
Preferably, a heat conduction oil coil heating system 32 is arranged in the catalytic reduction reaction equipment 8, and the temperature of the heat conduction oil coil heating system 32 is 55-70 ℃.
In one embodiment, the catalytic reaction apparatus comprises:
the channel switching device comprises an input end and two output ends, and the input end is connected with a pipeline for conveying the complexing liquid after absorbing NOx;
the first catalytic reduction reactor is connected with one output end of the channel switching device;
and the second catalytic reduction reactor is connected with the other output end of the channel switching device.
Wherein the channel switching device includes: a first valve arranged at one of the outputs and a second valve arranged at the other output.
The first valve is in an open state, the second valve is in a closed state, and the complex liquid absorbing NOx enters the first catalytic reduction reactor; the first valve is in a closed state, the second valve is in an open state, and the complexing liquid absorbing NOx enters the second catalytic reduction reactor. When the first catalytic reduction reactor receives the complex liquid after absorbing the NOx, the absorbed complex liquid in the second catalytic reduction reactor carries out catalytic reduction reaction. Similarly, the second catalytic reduction reactor performs a catalytic reduction reaction on the absorbed complex liquid that has been received in the first catalytic reduction reactor when receiving the complex liquid after absorbing NOx. The first catalytic reduction reactor and the second catalytic reduction reactor are used alternately to ensure the continuous operation of the system.
In one embodiment, the bottom end level of the denitration packed tower 6 is higher than the top end level of the catalytic reduction reaction device 8; the bottom end horizontal surface of the catalytic reduction reaction device 8 is higher than the top end horizontal surface of the complex liquid tank 1.
Through the arrangement, the complexing liquid can be transferred under the action of gravity, the use of a pump is reduced, and energy is saved.
In one embodiment, the pilot plant system for denitration process by complexing absorption in cooperation with catalytic reduction regeneration further comprises:
the gas flowmeter is arranged at a flue gas inlet of the shell 21 and used for detecting the flow of flue gas entering the denitration packed tower 6;
the controller is connected with the gas flowmeter and the spray pump 5;
the controller obtains the flow of the flue gas through the gas flowmeter, and controls the spraying flow of the spraying pump 5 to enable the liquid-gas ratio to be 1.5-4L/m3；
The liquid-gas ratio reaches the optimal state by adjusting the spraying flow, and the complexing liquid is not wasted on the basis of absorbing NOx in the flue gas.
The controller calculates the staying time of the gas in the denitration packed tower 6 according to the volume of the shell 21 and the gas flow meter, and judges whether the staying time is within a preset range (5-10 s);
and when the air flow is not in the preset range, adjusting the air pumping speed of an air pump arranged at the front end of the gas flow meter.
The retention time of the flue gas in the denitration packed tower 6 is ensured, so that NOx in the flue gas can fully react with the complexing liquid.
In one embodiment, a certain NOx-containing flue gas (temperature 450 ℃, gas amount 2000 m)3H), the denitration is processed by a pilot system of a complex absorption synergistic catalytic reduction regeneration denitration process, and the operation process comprises the following steps:
complexing solution tank 1 with complexing solution 4m34m of complexing liquid to be regenerated in the first catalytic reduction reactor 8-13；
Beginning to complex and absorb, spraying amount of complexing liquid is 6m3The flue gas and the complexing liquid are in countercurrent contact in a denitration packed tower 6, and the main reaction equation of complexing absorption is as follows:
Fe2+EDTA+NO→Fe2+EDTA(NO)，
the main side reaction equation is:
Fe2+EDTA+O2→Fe3+EDTA。
in order to ensure the best complexing absorption effect, the liquid-gas ratio of complexing absorption is 1.5-4L/m3The temperature is 40-50 ℃, and the residence time of the flue gas in the tower is 5-10 s.
In order to guarantee that the flue gas does not reveal, denitration tower bottom complex liquid outlet pipe way sets up the curved pipeline liquid seal of U type.
The valve 7-1 is opened and the valve 7-2 is closed, the absorbed complexing liquid flows into the first catalytic reduction reactor 8-1, the valve 7-1 is closed and the valve 7-2 is opened, and the complexing liquid absorbing NOx flows into the second catalytic reduction reactor 8-2;
the first catalytic reduction reactor 8-1 starts to react at the same time of complexing absorption according to 13kg/m3，3kg/m3Sodium formate and formic acid are added respectively, and an air compressor 14 is connected to a compressed air inlet 10 and is driven to rotate by 0.5-1 m3The gas quantity/min is blown into the reactor through a gas distributor (the compressed air outlet 11 opens into the flue gas inlet). Wherein the first catalytic reduction reactor is internally provided with a heat conducting oil coil heating system and a gas distributor, the aperture phi of the gas distributor is 2-4 mm, the regeneration temperature is 55-70 ℃, and the complexing liquid reacts for about 20min at the temperature of 55-70 ℃;
after the reaction is finished, pressurizing the catalytic reduction reactor 8-1 to 0.1-0.2 MPa, opening a valve 9-1 to start filtration, and filtering by adopting filter cloth with the aperture of 200-600 meshes to obtain regenerated complexing liquid with the particle size of 12m3The flow of the solution/h is added into the complex solution tank 1, and the reduction and regeneration process is about 20 min;
the equation for the catalytic reduction reaction is:
Figure BDA0002074141680000081
Fe2+EDTA(NO)+[H]→Fe2+EDTA+N2↑+H2O、
Fe3+EDTA+[H]→Fe2+EDTA+H2O。
the switching use of the two catalytic reduction reactors is realized by means of the switching of a valve.
The complex solution tank 1 is arranged below the first catalytic reduction reactor 8-1 or the second catalytic reduction reactor 8-2, and can transfer the complex solution by using gravitational potential energy and filter the palladium-carbon catalyst and the complex solution by using pressure.
At this time, the complex liquid tank 1 has 4m3Regenerated complexing liquid with 4m in the catalytic reduction reactor 8-23Completing the switching between the catalytic reduction reactors for the first time by using the complexing solution to be regenerated, and repeating the steps 2-4 so as to continuously carry out the reaction;
in the process, the complexing liquid c (Fe2+) before regeneration is 0.012mol/L, the efficiency of complexing and absorbing NOx is only about 30%, and the complexing liquid c (Fe2+) after regeneration is 0.058mol/L, and the efficiency of complexing and absorbing NOx can reach more than 85%.
When the first catalytic reduction reactor 8-1 is used for receiving the complexing liquid, the complexing liquid flows out of the complexing liquid tank 1, flows through the first valve 2, the spray pump 3, the second valve 4 and the heat exchanger 5, and enters the denitration packed tower 6; NOx in the flue gas is complexly absorbed in a denitration packed tower 6; and the effluent from the denitration complexing tower enters a first catalytic reduction reactor 8-1 through a third valve 7-1. After the first catalytic reduction reactor 8-1 reduces the complexing liquid, a fourth valve 9-1 is opened and the complexing liquid flows into the complexing liquid tank 1.
When the second catalytic reduction reactor 8-2 is used for receiving the complexing liquid, the complexing liquid flows out of the complexing liquid tank 1, flows through the second valve 2, the spray pump 3, the second valve 4 and the heat exchanger 5, and enters the denitration packed tower 6; NOx in the flue gas is complexly absorbed in a denitration packed tower 6; and the effluent from the denitration complex tower enters a second catalytic reduction reactor 8-2 through a fifth valve 7-2. And when the second catalytic reduction reactor 8-2 reduces the complexing solution, opening a sixth valve 9-2 and flowing the complexing solution into the complexing solution tank 1.
It will be apparent to those skilled in the art that various changes and modifications may be made in the present invention without departing from the spirit and scope of the invention. Thus, if such modifications and variations of the present invention fall within the scope of the claims of the present invention and their equivalents, the present invention is also intended to include such modifications and variations.

Claims (10)

1. A pilot-scale system for a denitration process by complexing absorption in cooperation with catalytic reduction regeneration is characterized by comprising a denitration packed tower, a complexing liquid tank, catalytic reduction reaction equipment, an air compressor and a heat exchanger;
the denitration packed tower comprises: the device comprises a shell, wherein a smoke inlet is formed in the side surface of the shell, which is close to the bottom of the shell, and a smoke outlet is formed in the top of the shell; a spraying layer is arranged in the shell below the smoke outlet; a packing layer is arranged below the spraying layer; a liquid seal layer is arranged at the bottom of the shell;
the complex liquid tank is used for storing complex liquid, the complex liquid is pumped out of the complex liquid tank through a spray pump, and then is sprayed out of a spray layer in the denitration packed tower after heat exchange of a heat exchanger and falls to a packing layer below the denitration packed tower; NOx in the flue gas in the filler layer is fully contacted with the complexing liquid for absorption, the complexing liquid after absorbing the NOx is conveyed into a catalytic reduction reaction device through a pipeline for reduction and regeneration, the catalytic reduction reaction device utilizes a palladium-carbon catalyst, formic acid and sodium formate system to reduce and regenerate the complexing liquid, and a filter layer is arranged in the catalytic reduction reaction device and is used for filtering the reduced liquid to obtain reusable complexing liquid; the air compressor introduces the manufactured compressed gas into the catalytic reduction reaction equipment through a gas distributor arranged in the catalytic reduction reaction equipment, and the palladium-carbon catalyst and the complexing liquid are filtered by using pressure;
the catalytic reduction reaction equipment adopts a palladium-carbon catalyst, formic acid and sodium formate system to reduce and regenerate complex liquid, and comprises the following components:
the equation for the catalytic reduction reaction is:
Figure FDA0003454713770000011
Fe2+EDTA(NO)+[H]→Fe2+EDTA+N2↑+H2O、
Fe3+EDTA+[H]→Fe2+EDTA+H2O。
2. the pilot-scale system of claim 1, wherein the step of fully contacting and absorbing NOx in flue gas in the packing layer with complexing liquid comprises:
the main equation for complex absorption is: fe2+EDTA+NO→Fe2+EDTA(NO)；
The main side reaction equation is: fe2+EDTA+O2→Fe3+EDTA。
3. The pilot plant system of the denitration process by complexing absorption with catalytic reduction regeneration of claim 1, wherein the complexing liquid exchanges heat to 40-50 ℃ through a heat exchanger.
4. The pilot plant system of claim 1, wherein the liquid seal comprises a U-bend pipe.
5. The pilot plant system of claim 1, wherein the filter layer comprises a filter cloth with a pore size of 200-600 meshes.
6. The pilot system of the denitration process by complexing absorption in coordination with catalytic reduction regeneration of claim 1, wherein a heat conducting oil coil heating system is arranged in the catalytic reduction reaction equipment, and the temperature of the heat conducting oil coil heating system is 55-70 ℃.
7. The pilot plant system for denitration process by complex absorption with catalytic reduction regeneration according to claim 1, wherein said catalytic reaction apparatus comprises:
the channel switching device comprises an input end and two output ends, and the input end is connected with a pipeline for conveying the complexing liquid after absorbing NOx;
the first catalytic reduction reactor is connected with one output end of the channel switching device;
and the second catalytic reduction reactor is connected with the other output end of the channel switching device.
8. The pilot plant system of claim 7, wherein the channel switching device comprises: a first valve arranged at one of the outputs and a second valve arranged at the other output.
9. The pilot-scale system of claim 1, wherein the horizontal plane of the bottom end of the denitration packed tower is higher than the horizontal plane of the top end of the catalytic reduction reaction device; the bottom end horizontal surface of the catalytic reduction reaction equipment is higher than the top end horizontal surface of the complexing liquid tank.
10. The pilot plant system for denitration process by complex absorption with catalytic reduction regeneration according to claim 1, further comprising:
the gas flowmeter is arranged at a flue gas inlet of the shell and used for detecting the flow of flue gas entering the denitration packed tower;
the controller is connected with the gas flowmeter and the spray pump;
the controller obtains the flow of the flue gas through the gas flowmeter, and controls the spraying flow of the spraying pump to enable the liquid-gas ratio to be 1.5-4L/m3；
The controller calculates the staying time of the gas in the denitration packed tower according to the shell volume and the gas flow, and judges whether the staying time is within a preset range;
and when the air flow is not in the preset range, adjusting the air pumping speed of an air pump arranged at the front end of the gas flow meter.
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Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101229474A (en) * 2007-10-23 2008-07-30 浙江大学 Method of biological reduction coupling chemisorbing purifying nitrogen oxide in smoke gas
CN101711943A (en) * 2009-09-15 2010-05-26 华东理工大学 Method for controlling pollutant waste gas containing NO through low-temperature liquid phase catalytic reduction

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101229474A (en) * 2007-10-23 2008-07-30 浙江大学 Method of biological reduction coupling chemisorbing purifying nitrogen oxide in smoke gas
CN101711943A (en) * 2009-09-15 2010-05-26 华东理工大学 Method for controlling pollutant waste gas containing NO through low-temperature liquid phase catalytic reduction

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
"Pd/C Synthesized with Citric Acid: An Efficient Catalyst for Hydrogen Generation from Formic Acid/Sodium Formate";Zhi-Li Wang et al.;《SCIENTIFIC REPORTS》;20120823;第2卷;第598页 *

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