CN105107374B - Flue gas desulfurization and denitration device utilizing proton membrane electrocatalysis - Google Patents

Abstract

The invention discloses a flue gas desulfurization and denitration device utilizing proton membrane electrocatalysis. The device is composed of a catalytic reaction absorption tower and an electrolytic reactor. The electrolytic reactor is communicated with the catalytic reaction absorption tower through a hydrogen gas opening (9) of a guide plate (10). A tower body shell (27) of the catalytic reaction absorption tower is internally provided with a baffle (28), a first desulfurization and denitration catalyst packing layer (2), an upper bearing plate (26), a carbon fixation catalyst packing layer (3), a middle bearing plate (25), a second desulfurization and denitration catalyst packing layer (4), a lower bearing plate (24), a solid-liquid separator (23), a flue gas distributor (6) and a hydrogen gas distributor (7) in sequence from the upper end to the position close to the lower end. The electrolytic reactor is internally provided with an electrolytic reaction chamber. The electrolytic reaction chamber is internally provided with anode plates (14) and cathode plates (12), and the anode plates (14) are separated from the cathode plates (12) through proton membranes (13). The flue gas desulfurization and denitration device has the advantages of being simple in structure, small in occupied area, low in investment and operation cost, high in flue gas purification efficiency and good in product recycling effect.

Description

A proton membrane electrocatalytic flue gas desulfurization and denitrification device

technical field

The invention belongs to the technical field of flue gas desulfurization and denitrification devices. Specifically relates to a proton membrane electrocatalytic flue gas desulfurization and denitrification device.

Background technique

With the continuous acceleration of industrialization and urbanization in our country, industry occupies an increasing proportion in the growth of the national economy, and human demand for energy is also increasing day by day. The consumption of natural resources such as coal, oil, and natural gas is increasing day by day, resulting in air pollution. A few days ago, the smog weather in many cities across the country has challenged the living environment of human beings. Harmful gases in the atmosphere have attracted much attention from all walks of life at home and abroad because of their characteristics of strong toxicity, wide spread and difficulty in control. Flue gas such as SO ₂ , NO _X and CO ₂ are the main pollutants. Among them, SO ₂ and NO _X will form acid rain and photochemical smog and other pollution phenomena, which will not only endanger people's respiratory system, but also destroy the normal growth of vegetation. ; and a large amount of CO ₂ released in the air seriously affects climate change and causes "greenhouse effect". Therefore, how to effectively control harmful flue gases such as SO ₂ , NO _X and CO ₂ has become an urgent environmental protection problem.

At present, the limestone-gypsum method is mainly used for the removal of flue gas SO _X. The limestone-gypsum method has achieved some results in research and environmental protection, but there are problems of complex equipment, large investment, and high operating costs. When the flue gas When the medium SO ₂ fluctuates greatly, the amount of limestone is difficult to control, and the generated CaSO ₃ and CaSO ₄ are easy to block pipelines and equipment. For the removal of flue gas _NOx , the catalytic reduction method is mainly used. Although the catalytic reduction method can reduce the _NOx emission concentration in the flue gas to a low level, it consumes a lot of NH ₃ and some fuel gas, resulting in a large economic loss. Among the methods for reducing CO ₂ concentration, the most studied reduction methods are thermochemical reduction and photocatalytic reduction, among which thermochemical reduction requires high temperature and high pressure, and CO ₂ will be generated during the reduction process; although photocatalytic reduction is environmentally friendly and energy-saving, But the yield is lower and the speed is slower.

The traditional process is mostly to install a denitrification device behind the desulfurization device or in front of the dust collector to achieve combined desulfurization and denitrification. This hierarchical treatment method has many disadvantages such as large area occupation, high investment and operating costs.

Contents of the invention

The present invention aims to overcome the defects of the prior art, and aims to provide a proton membrane electrocatalytic flue gas desulfurization and denitrification with simple structure, small footprint, low investment and operating costs, high flue gas purification efficiency and good product recovery and reuse effect. device.

In order to achieve the above object, the technical solution adopted by the present invention is: the device is composed of a catalytic reaction absorption tower and an electrolytic reactor, the lower end of the catalytic reaction absorption tower and the upper end of the electrolytic reactor are connected as a whole with the center line.

The structure of the catalytic reaction absorption tower is: the top cover and the tower body are fixedly connected with the center line through the flange, the longitudinal section of the top cover is arc-shaped, and the center of the top cover is provided with an exhaust port.

The structure of the tower body is: the tower body shell is a hollow cylinder, and the height and outer diameter ratio of the tower body shell is 3:1~5:1. In the tower shell, there are baffles, first desulfurization and denitrification catalyst packing layer, upper receiving plate, carbon fixation catalyst packing layer, middle receiving plate, second desulfurization and denitrification catalyst packing layer, lower receiving plate from the upper end to the lower end. plate, solid-liquid separator, flue gas diffuser and hydrogen diffuser.

Among them: the distance between the baffle plate and the upper receiving plate, the distance between the upper receiving plate and the middle receiving plate, and the distance between the middle receiving plate and the lower receiving plate are equal; the first desulfurization and denitrification catalyst packing layer, the carbon fixation catalyst packing layer and the second The filler filling rate of the second desulfurization and denitrification catalyst filler layer is 0.9 to 1 times. The solid-liquid separator is set on an inclined plane, the angle between the solid-liquid separator and the horizontal plane is 15-20°, and the solid-liquid separator is fixedly connected to the inner wall of the tower shell. There is a solid product discharge port on one side of the tower shell, which is the same side as the lowest position of the slope of the solid-liquid separator, and the solid product discharge port is close to the top of the solid-liquid separator. inclined plane. A flue gas inlet is opened on the other side of the tower shell, and the flue gas inlet is located between the flue gas diffuser and the hydrogen diffuser. The distance between the upper plane of the flue gas diffuser and the lower plane of the lower receiving plate is 0.3~0.4 times the inner diameter of the tower shell, and the distance between the upper plane of the hydrogen diffuser and the lower plane of the flue gas diffuser is the tower shell 0.2~0.3 times the internal diameter.

The structure of the electrolytic reactor is: the electrolytic reactor housing is cylindrical, the outer diameter of the electrolytic reactor housing is equal to the outer diameter of the tower body housing, and the ratio of the height of the electrolytic reactor housing to the outer diameter is 1.1: 1~1.3︰1. The uppermost end of the electrolytic reactor shell is provided with a drainage plate, which is set on an inclined plane, and the included angle between the drainage plate and the horizontal plane is 15-20°. There is a hydrogen port on the diversion plate, and the hydrogen port is located at the highest point of the slope of the diversion plate. One side of the electrolytic reactor shell is provided with a liquid product discharge port and an oxygen discharge port, and one side of the electrolytic reactor shell is the same side as the lowest position of the slope of the drain plate, and the liquid product discharge port is close to the drain plate On the upper slope, the oxygen outlet is close to the lower slope of the drainage plate.

An electrolytic reaction chamber is arranged inside the electrolytic reactor shell, and the electrolytic reaction chamber is located at the lower part of the electrolytic reactor shell, and a liquid inlet is opened between the bottom of the electrolytic reactor shell and the bottom of the electrolytic reaction chamber. The electrolytic reaction chamber is in the shape of a box, and there are 11 or 15 or 19 slots evenly opened on the inner wall of the box top plate, box bottom plate, box front side plate and box rear side plate, and each slot is in the shape of " "mouth", the plane where each slot is located is parallel to the left side panel of the cabinet. The proton membranes are embedded in the even-numbered slots, the anode plate (14) is embedded in the slots with the sequence numbers 1, 5, and 9, or the anode plate (14) is embedded in the slots with the sequence numbers 1, 5, 9, and 13 Anode plates (14), or slots with sequence numbers 1, 5, 9, 13 and 17 are embedded with anode plates, and the remaining slots are all embedded with cathode plates. There is a row of small holes evenly opened between the slots of the bottom plate of the cabinet and the top plate of the cabinet, each row of small holes is 12~30, and the diameter of the small holes is 5~8mm. The upper plane of the top plate of the box body is fixed with 3 to 5 strip-shaped slot plates. When fixing, the notch of each strip-shaped slot plate faces downward, and the air holes on both sides of the cathode plate are located in the slots of the strip-shaped slot plate. The strip slots communicate with each other, one end of the hydrogen pipeline communicates with the strip slots, and the other end of the hydrogen pipeline communicates with the hydrogen port.

The anode plate is connected to the positive pole of the battery through the positive pole lead, and the cathode plate is connected to the negative pole of the battery through the negative pole lead.

The thickness of the baffle is 1~3cm, and the outer diameter of the baffle is equal to the inner diameter of the tower shell; %; The baffle plate is the same as the upper receiving plate, the middle receiving plate and the lower receiving plate.

The filler of the first desulfurization and denitration catalyst filler layer is at least one of activated carbon, Cu/Mg/Al catalyst, CuO/Al ₂ O ₃ catalyst and CoMo/Al ₂ O ₃ catalyst, with a particle size of 4-6 mm.

The filler of the carbon-fixing catalyst filler layer is one or both of Cu/Al ₂ O ₃ catalyst and CuO/ZnO/Al ₂ O ₃ catalyst, with a particle size of 4-6 mm.

The filler of the second desulfurization and denitration catalyst filler layer is at least one of activated carbon, Cu/Mg/Al catalyst, CuO/Al ₂ O ₃ catalyst and CoMo/Al ₂ O ₃ catalyst, with a particle size of 4-6 mm.

The solid-liquid separator is composed of a stainless steel ring and a filter cloth, the stainless steel ring is oval, the filter cloth is fixed on the stainless steel ring, the material of the filter cloth is polypropylene or nylon, and the aperture is 0.045~0.15mm.

The thickness of the smoke diffuser is 5-15 cm, and the smoke diffuser is provided with small holes, the diameter of which is 1-5 mm, and the opening ratio is 30-50%.

The thickness of the hydrogen disperser is 5-15 cm, and the hydrogen disperser has small holes, the diameter of the small holes is 3-5 mm, and the opening ratio is 50-70%.

The material of the proton membrane is carbon nanofiber material.

Both ends of the strip groove plate are closed.

The device can purify SO ₂ , NO _X and CO ₂ in the mixed flue gas, and can also recycle the sulfur and methanol resources in the product. The specific steps are as follows:

Step 1: First pump water into the electrolysis reactor through the liquid inlet of the device, the voltage in the electrolysis reactor is 2.2V-3.5V, and then open the valve of the oxygen outlet and the valve of the hydrogen outlet. When the electrolysis reaction starts, water decomposes into H ⁺ and OH ^- under the action of an electric field, and OH ^- undergoes an oxidation reaction at the anode to generate O ₂ , and O ₂ enters the electrolysis reactor shell from the electrolysis reaction chamber through the small holes on both sides of the anode plate , and then discharged through the oxygen outlet; H ⁺ migrates from the anode through the proton membrane to the cathode for reduction reaction, and combines with electrons to generate H ₂ , H ₂ enters the strip slot plate through the small holes on both sides of the cathode plate, and then passes through The hydrogen pipeline enters the catalytic reaction absorption tower through the hydrogen disperser.

Step 2: When _H2 enters the catalytic reaction absorption tower, open the valve of the flue gas inlet, adjust the intake concentration of the flue gas through the valve, and send the flue gas after deoxygenation pretreatment into the catalytic reaction absorption tower. The flue gas after the deoxidation pretreatment is dispersed through the flue gas disperser, and then passes through the second desulfurization and denitration catalyst packing layer, the carbon fixation catalyst packing layer and the first desulfurization and denitration catalyst packing layer, so that it can fully contact with the catalyst in each packing layer, Desulfurization, denitrification and carbon fixation reactions are carried out to obtain sulfur, nitrogen and methanol.

Step 3, collecting and processing the products after flue gas purification. The nitrogen generated by the denitrification reaction is discharged through the exhaust port; the sulfur generated by the desulfurization reaction is retained on the filter cloth of the solid-liquid separator, and is discharged and collected from the solid product discharge port; the methanol generated by the carbon fixation reaction is collected through the liquid product discharge port as fuel use.

Owing to adopting above-mentioned technical scheme, the present invention has following positive effect compared with prior art:

1. This device adopts the proton membrane electrolysis water hydrogen production technology, which can provide sufficient reducing gas-hydrogen, and reduces investment and operating costs.

2. The device is equipped with a flue gas diffuser at the flue gas inlet, and a hydrogen gas diffuser at the hydrogen gas port, which greatly increases the contact area between flue gas, hydrogen and catalyst, and has high flue gas purification efficiency.

3. This device uses multiple catalysts to convert flue gas into sulfur and methanol while absorbing flue gas SO ₂ , NO _X and CO ₂ . The conversion efficiency reaches 95%, and the product recovery and reuse effect is good.

4. This device realizes the integrated catalytic absorption reaction of mixed flue gas, integrates desulfurization, denitration and carbon fixation reactions, occupies a small area, and has a simple structure, which provides convenience for industrial flue gas treatment.

Therefore, the device has the characteristics of simple structure, small floor space, low investment and operation costs, high flue gas purification efficiency and good product recovery and reuse effect.

Description of drawings

Fig. 1 is a kind of structural representation of the present invention;

Figure 2 is an enlarged schematic diagram of the A-A direction of Figure 1;

Fig. 3 is an enlarged cross-sectional schematic diagram of the strip groove plate (19) in Fig. 1 and Fig. 2 .

detailed description

The present invention will be described in further detail below in conjunction with the accompanying drawings and specific embodiments, without limiting its protection scope.

Example 1

A proton membrane electrocatalytic flue gas desulfurization and denitrification device. As shown in Figure 1, the device is composed of a catalytic reaction absorption tower and an electrolytic reactor, the lower end of the catalytic reaction absorption tower and the upper end of the electrolytic reactor are connected as a whole with the central line.

The structure of the catalytic reaction absorption tower is shown in Figure 1: the top cover 29 and the tower body 5 are fixedly connected with the center line through flanges, the longitudinal section of the top cover 29 is arc-shaped, and the center of the top cover 29 is provided with an exhaust port 1.

The structure of the tower body 5 is shown in FIG. 1 : the tower body shell 27 is a hollow cylinder, and the ratio of the height to the outer diameter of the tower body shell 27 is 3:1~4:1. Inside the tower shell 27, there are baffles 28, a first desulfurization and denitrification catalyst packing layer 2, an upper receiving plate 26, a carbon-fixing catalyst packing layer 3, a middle receiving plate 25, and a second desulfurization Denitration catalyst packing layer 4 , lower receiving plate 24 , solid-liquid separator 23 , flue gas diffuser 6 and hydrogen gas diffuser 7 .

Wherein: the distance between the baffle plate 28 and the upper receiving plate 26, the distance between the upper receiving plate 26 and the middle receiving plate 25 and the distance between the middle receiving plate 25 and the lower receiving plate 24 are equal, the first desulfurization and denitrification catalyst packing layer 2, The filler filling rate of the carbon-fixing catalyst packing layer 3 and the second desulfurization and denitrification catalyst packing layer 4 is 0.9 to 1 times. The solid-liquid separator 23 is arranged on a slope, the angle between the solid-liquid separator 23 and the horizontal plane is 15-20°, and the solid-liquid separator 23 is fixedly connected to the inner wall of the tower shell 27 . One side of the tower body shell 27 has a solid product discharge port 22, and one side of the tower body shell 27 is the same side as the lowest position of the slope of the solid-liquid separator 23, and the solid product discharge port 22 is close to the solid The upper slope of the liquid separator 23. A flue gas inlet 8 is opened on the other side of the tower shell 27 , and the flue gas inlet 8 is located between the flue gas diffuser 6 and the hydrogen diffuser 7 . The distance between the upper plane of the flue gas diffuser 6 and the lower plane of the lower receiving plate 24 is 0.3 to 0.4 times the inner diameter of the tower shell 27, and the distance between the upper plane of the hydrogen diffuser 7 and the lower plane of the flue gas diffuser 6 The distance is 0.2 to 0.3 times the inner diameter of the tower shell 27 .

The structure of the electrolytic reactor is as shown in Figure 1: the electrolytic reactor housing 18 is cylindrical, and the outer diameter of the electrolytic reactor housing 18 is equal to the outer diameter of the tower body housing 27, and the outer diameter of the electrolytic reactor housing 18 The ratio of height to outer diameter is 1.1︰1~1.2︰1. The uppermost end of the electrolytic reactor shell 18 is provided with a diversion plate 10, which is arranged on an inclined plane, and the included angle between the diversion plate 10 and the horizontal plane is 15-20°. A hydrogen port 9 is opened on the diversion plate 10 , and the hydrogen port 9 is located at the highest point of the slope of the diversion plate 10 . One side of the electrolytic reactor housing 18 has a liquid product discharge port 21 and an oxygen discharge port 20, and one side of the electrolytic reactor housing 18 is the same side as the lowest position of the slope of the drain plate 10, and the liquid product discharge port The outlet 21 is close to the upper slope of the drainage plate 10 , and the oxygen outlet 20 is close to the lower slope of the drainage plate 10 .

As shown in Figure 1, electrolytic reaction chamber is provided with electrolytic reaction chamber in the electrolytic reactor housing 18, and electrolytic reaction chamber is positioned at the bottom of electrolytic reactor housing 18, opens between the bottom of electrolytic reactor housing 18 and the bottom of electrolytic reaction chamber. Liquid inlet 16 is arranged. The electrolytic reaction chamber is in the shape of a box, and 11 slots are evenly opened on the inner wall of the box top, box bottom, box front side plate and box rear side plate, and each slot is in the shape of a "mouth". The plane where the two slots are located is parallel to the left side panel of the cabinet. Proton membranes 13 are embedded in slots with even numbers, anode plates 14 are embedded in slots with sequence numbers 1, 5, and 9, and cathode plates 12 are embedded in the remaining slots. A row of small holes is evenly opened between the slots on the bottom plate of the box body and the top plate of the box body. There are 12 small holes in each row, and the diameter of the small holes is 8mm. As shown in Figures 1 and 2, three strip-shaped groove plates 19 are fixed on the upper plane of the top plate of the box body; The two ends of slot plate 19 are closed. As shown in FIG. 1 and FIG. 2 , the air holes on both sides of the cathode plate 12 are located in the notch of the strip-shaped slot plate 19 . The strip slots 19 communicate with each other, one end of the hydrogen pipeline 11 communicates with the strip slot 19 , and the other end of the hydrogen pipeline 11 communicates with the hydrogen port 9 .

The anode plate 14 is connected to the positive pole of the battery through the positive pole lead 17 , and the cathode plate 12 is connected to the negative pole of the battery through the negative pole lead 15 .

The thickness of described baffle plate 28 is 1～3cm, and the outer diameter of baffle plate 28 is equal to the inner diameter of tower body shell 27; 45~65%; the baffle plate 28 is the same as the upper receiving plate 26, the middle receiving plate 25 and the lower receiving plate 24.

The filler of the first desulfurization and denitration catalyst filler layer 2 is at least one of activated carbon, Cu/Mg/Al catalyst, CuO/Al ₂ O ₃ catalyst and CoMo/Al ₂ O ₃ catalyst, with a particle size of 4-6 mm.

The filler of the carbon-fixing catalyst filler layer 3 is one or both of Cu/Al ₂ O ₃ catalyst and CuO/ZnO/Al ₂ O ₃ catalyst, with a particle size of 4-6 mm.

The filler of the second desulfurization and denitration catalyst filler layer 4 is at least one of activated carbon, Cu/Mg/Al catalyst, CuO/Al ₂ O ₃ catalyst and CoMo/Al ₂ O ₃ catalyst, with a particle size of 4-6 mm.

The solid-liquid separator 23 is composed of a stainless steel ring and a filter cloth, the stainless steel ring is oval, the filter cloth is fixed on the stainless steel ring, the material of the filter cloth is polypropylene or nylon, and the aperture is 0.045-0.15mm.

The thickness of the smoke diffuser 6 is 5-15 cm, and the smoke diffuser 6 has small holes, the diameter of which is 1-5 mm, and the opening ratio is 30-50%.

The thickness of the hydrogen diffuser 7 is 5-15 cm, and the hydrogen diffuser 7 has small holes, the diameter of the small holes is 3-5 mm, and the opening ratio is 50-70%.

The material of the proton membrane 13 is carbon nanofiber material.

Example 2

A proton membrane electrocatalytic flue gas desulfurization and denitrification device. Except following technical parameter, all the other are with embodiment 1:

The height and outer diameter ratio of the tower shell 27 is 4:1~5:1.

The ratio of the height to the outer diameter of the electrolytic reactor shell 18 is 1.2:1~1.3:1.

The electrolytic reaction chamber is in the shape of a box, and there are 15 slots uniformly opened on the inner wall of the top plate, bottom plate, front side plate and rear side plate of the box body, and each slot is in the shape of a “mouth”. The plane where the two slots are located is parallel to the left side panel of the cabinet. Proton membranes 13 are embedded in slots with even numbers, anode plates (14) are embedded in slots with sequence numbers 1, 5, 9 and 13, and cathode plates 12 are embedded in the remaining slots. A row of small holes is evenly opened between the slots on the bottom plate of the cabinet and the top plate of the cabinet, each row of small holes is 13~30, and the diameter of the small holes is 5~8mm. The upper plane of the top plate of the box body is provided with 4 strip groove plates 19 .

Example 3

A proton membrane electrocatalytic flue gas desulfurization and denitrification device. Except following technical parameter, all the other are with embodiment 2:

The electrolytic reaction chamber is in the shape of a box. There are 19 slots evenly opened on the inner wall of the box top, box bottom, box front side plate and box rear side plate. Each slot is in the shape of a "mouth". The plane where the two slots are located is parallel to the left side panel of the cabinet. Proton membranes 13 are embedded in slots with even numbers, anode plates 14 are embedded in slots with sequence numbers 1, 5, 9, 13 and 17, and cathode plates 12 are embedded in the remaining slots. The upper plane of the top plate of the box body is provided with 5 strip groove plates 19 .

The device can purify SO ₂ , NO _X and CO ₂ in the mixed flue gas, and can also recycle the sulfur and methanol resources in the product. The specific steps are as follows:

Step 1: First pump water into the electrolysis reactor through the liquid inlet 16 of the device, the voltage in the electrolysis reactor is 2.2V-3.5V, and then open the valve of the oxygen outlet 20 and the valve of the hydrogen outlet 9. When the electrolysis reaction starts, water decomposes into H ⁺ and OH ^- under the action of an electric field, and OH ^- undergoes an oxidation reaction at the anode to generate O ₂ , and O ₂ enters the electrolysis reactor shell from the electrolysis reaction chamber through the small holes on both sides of the anode plate 14 body 18, and then discharged through the oxygen discharge port 20; H ⁺ will migrate from the anode through the proton membrane 13 to the cathode to undergo a reduction reaction, and combine with electrons to generate H ₂ , and H ₂ enters the strip groove through the small holes on both sides of the cathode plate 12 In the plate 19, it enters the catalytic reaction absorption tower through the hydrogen gas disperser 7 through the hydrogen gas pipeline 11.

Step 2, when _H2 enters the catalytic reaction absorption tower, open the valve of the flue gas inlet 8, adjust the intake concentration of the flue gas through the valve, and send the flue gas after deoxidation pretreatment into the catalytic reaction absorption tower. The flue gas after the deoxidation pretreatment is dispersed through the flue gas disperser 6 and then passes through the second desulfurization and denitration catalyst packing layer 4, the carbon fixation catalyst packing layer 3 and the first desulfurization and denitration catalyst packing layer 2, so that it can be mixed with the The catalysts are fully contacted to perform desulfurization, denitrification and carbon fixation reactions to obtain sulfur, nitrogen and methanol.

Step 3, collecting and processing the products after flue gas purification. The nitrogen generated by the denitrification reaction is discharged through the exhaust port 1; the sulfur generated by the desulfurization reaction stays on the filter cloth of the solid-liquid separator 23, and is discharged and collected from the solid product discharge port 22; the methanol generated by the carbon fixation reaction passes through the liquid product discharge port 21 collected as fuel utilization.

Compared with the prior art, this specific embodiment has the following positive effects:

1. This device adopts the proton membrane electrolysis water hydrogen production technology, which can provide sufficient reducing gas-hydrogen, and reduces investment and operating costs.

2. The device is equipped with a flue gas diffuser 6 at the flue gas inlet 8, and a hydrogen gas diffuser 7 at the hydrogen gas port 9, which greatly increases the contact area between flue gas, hydrogen and catalyst, and has high flue gas purification efficiency.

3. This device uses multiple catalysts to convert flue gas into sulfur and methanol while absorbing flue gas SO ₂ , NO _X and CO ₂ . The conversion efficiency reaches 95%, and the product recovery and reuse effect is good.

4. This device realizes the integrated catalytic absorption reaction of mixed flue gas, integrates desulfurization, denitration and carbon fixation reactions, occupies a small area, and has a simple structure, which provides convenience for industrial flue gas treatment.

Therefore, the device has the characteristics of simple structure, small floor space, low investment and operation costs, high flue gas purification efficiency and good product recovery and reuse effect.

Claims (10)

1. a kind of proton membrane electro-catalysis flue gas desulfurization and denitrification device, it is characterised in that described device is by catalytic reaction absorption tower and electricity Solution reactor composition, the lower end on catalytic reaction absorption tower and the upper end of electrolysis reactor are connected as entirety with centrage；

The structure on catalytic reaction absorption tower is：Top cover (29) is fixedly connected with centrage by flange with tower body (5), top cover (29) Longitudinal section be in arc-shaped, the center position of top cover (29) is provided with air vent (1)；

The structure of tower body (5) is：Tower body housing (27) is hollow cylinder, and the height and external diameter ratio of tower body housing (27) are 31 ～51；In tower body housing (27), baffle plate (28), first desulphurization denitration catalyst are sequentially provided with lower end from upper end Packing layer (2), upper bearing plate (26), carbon sequestration catalyst filling layer (3), middle bearing plate (25), the second desulphurization denitration catalyst are filled out The bed of material (4), lower bearing plate (24), solid-liquid separator (23), flue gas disperser (6) and hydrogen disperser (7)；

Wherein：Distance between the distance, upper bearing plate (26) between baffle plate (28) and upper bearing plate (26) and middle bearing plate (25) and Distance between middle bearing plate (25) and lower bearing plate (24) is equal, the first desulphurization denitration catalyst filling layer (2), carbon sequestration catalyst The media-filling rate of packing layer (3) and the second desulphurization denitration catalyst filling layer (4) is 0.9～1；Solid-liquid separator (23) is oblique Face is arranged, and solid-liquid separator (23) is 15～20 ° with the angle of horizontal plane, and solid-liquid separator (23) is interior with tower body housing (27) Wall is fixedly connected；The side of tower body housing (27) is provided with solid product outlet (22), and the side of the tower body housing (27) is With the inclined-plane extreme lower position identical side of solid-liquid separator (23), solid product outlet (22) is close to solid-liquid separator (23) Ramp；Smoke air inlet (8) is provided with the opposite side of tower body housing (27), smoke air inlet (8) is positioned at flue gas disperser (6) and hydrogen disperser (7) between；The upper plane of flue gas disperser (6) to lower bearing plate (24) lower plane between distance be 0.3～0.4 times of tower body housing (27) internal diameter, between the lower plane of the upper plane of hydrogen disperser (7) to flue gas disperser (6) 0.2～0.3 times for tower body housing (27) internal diameter of distance；

The structure of the electrolysis reactor is：Electrolysis reactor housing (18) is cylindrical shape, electrolysis reactor housing (18) external diameter Equal with the external diameter of tower body housing (27), the height of electrolysis reactor housing (18) is 1.1 1～1.3 1 with the ratio of external diameter；Electricity Solution reactor shell (18) is topmost provided with drainage plate (10), and drainage plate (10) is inclined-plane setting, drainage plate (10) and horizontal plane Angle be 15～20 °；Hydrogen mouth (9), highest of the hydrogen mouth (9) positioned at drainage plate (10) inclined-plane are provided with drainage plate (10) Place；The side of electrolysis reactor housing (18) is provided with product liquid outlet (21) and oxygen discharge (20), and the electrolysis is anti- The side for answering device housing (18) is the inclined-plane extreme lower position identical side with drainage plate (10), and product liquid outlet (21) is tightly Patch drainage plate (10) ramp, oxygen discharge (20) are close to drainage plate (10) lower inclined plane；

Cell reaction room is provided with electrolysis reactor housing (18), cell reaction room is located under electrolysis reactor housing (18) Portion, is provided with inlet (16) between the bottom of the bottom and cell reaction room of electrolysis reactor housing (18)；Cell reaction room For case shape, the inwall of roof box, box bottom, cabinet front plate and casing back side panel be equably provided with 11 or 15 or 19 slots, each slot are in " mouth " shape, and the plane at each slot place is parallel with the left plate of casing；It is even in serial number Be embedded with proton membrane (13) in several slots, serial number be 1,5,9 slot in be embedded in positive plate (14), or serial number be 1,5, 9th, positive plate (14) is embedded in 13 slot, or in the slot that serial number is 1,5,9,13,17, is embedded in positive plate (14), remaining is inserted Groove is embedded with minus plate (12)；A row aperture is provided between the slot of box bottom and roof box equably, it is 12 often to arrange aperture ～30, small aperture is 5～8mm；The upper plane of roof box is fixed with 3～5 bar shaped frids (19), each bar shaped frid (19) down, the pore of minus plate (12) both sides is located in the notch of bar shaped frid (19) notch；Phase between bar shaped frid (19) Logical, one end of Hydrogen Line (11) is communicated with bar shaped frid (19), and the other end of Hydrogen Line (11) is communicated with hydrogen mouth (9)；

The positive plate (14) is connected with the positive pole of battery by positive wire (17), and the minus plate (12) is by cathode conductor (15) it is connected with the negative pole of battery.

2. proton membrane electro-catalysis flue gas desulfurization and denitrification device according to claim 1, it is characterised in that the baffle plate (28) Thickness be 1～3cm, the external diameter of baffle plate (28) is equal with the internal diameter of tower body housing (27)；Baffle plate (28) is provided with aperture, described little The aperture in hole is 1～3mm, and percent opening is 45～65%；The baffle plate (28) and upper bearing plate (26), middle bearing plate (25) and under Bearing plate (24) is identical.

3. proton membrane electro-catalysis flue gas desulfurization and denitrification device according to claim 1, it is characterised in that first desulfurization The filler of denitrating catalyst packing layer (2) is activated carbon, Cu/Mg/Al catalyst, CuO/Al₂O₃Catalyst and CoMo/Al₂O₃Urge One or more of agent, particle diameter are 4～6mm.

4. proton membrane electro-catalysis flue gas desulfurization and denitrification device according to claim 1, it is characterised in that the carbon sequestration catalysis The filler of agent packing layer (3) is Cu/Al₂O₃Catalyst and CuO/ZnO/Al₂O₃One or two in catalyst, particle diameter is 4～ 6mm。

5. proton membrane electro-catalysis flue gas desulfurization and denitrification device according to claim 1, it is characterised in that second desulfurization The filler of denitrating catalyst packing layer (4) is activated carbon, Cu/Mg/Al catalyst, CuO/Al₂O₃Catalyst and CoMo/Al₂O₃Urge One or more of agent, particle diameter are 4～6mm.

6. proton membrane electro-catalysis flue gas desulfurization and denitrification device according to claim 1, it is characterised in that the solid-liquid separation Device (23) is made up of stainless steel coil and filter net cloth, and stainless steel coil ovalize, filter net cloth are fixed on stainless steel coil, is filtered The material of screen cloth is polypropylene or nylon, and aperture is 0.045～0.15mm.

7. proton membrane electro-catalysis flue gas desulfurization and denitrification device according to claim 1, it is characterised in that the flue gas dispersion The thickness of device (6) is 5～15cm, and flue gas disperser (6) is provided with aperture, and the aperture of the aperture is 1～5mm, and percent opening is 30 ～50%.

8. proton membrane electro-catalysis flue gas desulfurization and denitrification device according to claim 1, it is characterised in that the hydrogen dispersion The thickness of device (7) is 5～15cm, and hydrogen disperser (7) is provided with aperture, and the aperture of the aperture is 3～5mm, and percent opening is 50 ～70%.

9. proton membrane electro-catalysis flue gas desulfurization and denitrification device according to claim 1, it is characterised in that the proton membrane (13) material is carbon nano-fiber material.

10. proton membrane electro-catalysis flue gas desulfurization and denitrification device according to claim 1, it is characterised in that the bar shaped frid (19) closed at both ends.