CN209989208U - SCR regeneration denitration catalyst effluent disposal system - Google Patents
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Abstract
The utility model discloses a SCR regeneration denitration catalyst effluent disposal system, include: the device comprises a first-stage reaction sedimentation tank, a second-stage reaction sedimentation tank, a third-stage reaction sedimentation tank, a cooling tower, a hydrolysis acidification tank, a sludge tank, a first aerobic aeration tank, a second aerobic aeration tank, an MBR membrane bioreactor, a discharge water tank and a plate-and-frame filter press. Wherein, waste water can pass through one-level reaction sedimentation tank, second grade reaction sedimentation tank, tertiary reaction sedimentation tank, cooling tower, hydrolysis-acidification tank, sludge impoundment, first good oxygen aeration tank, good oxygen aeration tank of second and MBR membrane bioreactor in proper order, and the accessible discharges away in the pond after final water quality testing is up to standard. All the components are connected and installed in sequence according to the wastewater trend, and the plate-and-frame filter press is installed behind a sludge tank; the system has the advantages of small occupied area, high daily water treatment capacity, high treatment efficiency and low environmental pollution, and can effectively treat wastewater generated in the process of regenerating the SCR denitration catalyst.
Description
Technical Field
The invention belongs to the field of environmental protection, and particularly relates to a SCR (selective catalytic reduction) regenerated denitration catalyst wastewater treatment system.
Background
The SCR denitration catalyst is the core for removing nitrogen oxides in flue gas of a thermal power plant, the performance of the SCR denitration catalyst directly influences the efficiency of flue gas denitration, the service life of a common denitration catalyst is only 3 years, and the catalyst is eliminated and buried or further regenerated. In 2013, 8 and 11 months, the State Council issues an opinion on accelerating the development of energy-saving and environment-friendly industries, and particularly points out that preparation and regeneration of a denitration catalyst, a selective catalytic reduction technology, a selective waste catalytic reduction technology and equipment thereof need to be vigorously developed. The method is a clear indication for preparing and regenerating the denitration catalyst for the first time in China.
The regeneration and cleaning of the catalyst generally comprises the steps of physical ash removal, bubbling cleaning, chemical cleaning, ultrasonic cleaning, chemical neutralization, microscopic iron removal, pure water rinsing and the like, wastewater generated in the processes can generate a large amount of heavy metals (such as iron, vanadium, aluminum and the like) and non-heavy metals (such as phosphorus, sulfur, arsenic and the like), the research on the regeneration wastewater of the SCR denitration catalyst in China is still in a starting stage at present, bentonite is mostly adopted for adsorption in the conventional wastewater treatment, the heavy metals and organic matters in the wastewater cannot be effectively treated, the treatment cost is high, and secondary pollution is more likely to be brought to the ecological environment. Therefore, in order to properly treat the wastewater generated in the regeneration process and make the wastewater reach the national laws and regulations, an efficient wastewater treatment system for the SCR regeneration denitration catalyst needs to be researched urgently.
Disclosure of Invention
The utility model discloses the technical problem that needs to solve can produce a large amount of heavy metals (like iron, vanadium, aluminium etc.) and non-heavy metal (like phosphorus, sulphur, arsenic etc.) in the SCR denitration catalyst regeneration waste water, and the biodegradability is poor, and the processing degree of difficulty is high, consequently need provide an efficient SCR regeneration denitration catalyst effluent disposal system, can accomplish to take up an area of for a short time, and the treatment effeciency is high and secondary pollution effect such as little.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
an SCR regeneration denitration catalyst effluent disposal system, comprising: the system comprises a first-stage reaction sedimentation tank, a second-stage reaction sedimentation tank, a third-stage reaction sedimentation tank, a cooling tower, a hydrolysis acidification tank, a sludge tank, a first aerobic aeration tank, a second aerobic aeration tank, an MBR (membrane bioreactor), a discharge water tank and a plate-and-frame filter press; wherein, the first-stage reaction sedimentation tank, the second-stage reaction sedimentation tank, the third-stage reaction sedimentation tank, the cooling tower, the hydrolysis acidification tank, the first aerobic aeration tank, the second aerobic aeration tank, the MBR membrane bioreactor and the discharge water tank are sequentially connected and installed according to the wastewater trend, and the plate-and-frame filter press is installed behind the sludge tank; the first-level reaction sedimentation tank, the second-level reaction sedimentation tank, the third-level reaction sedimentation tank and the hydrolysis acidification tank are connected with the sludge tank through a first sludge discharge pipe, and the first aerobic aeration tank and the second aerobic aeration tank are connected with the sludge tank through a second sludge discharge pipe.
And the wastewater enters the system through a sewage inlet pipe.
The effective volume of the hydrolysis acidification tank is 50m3The hydraulic retention time is 0.8-1.2 hours.
The effective volumes of the first aerobic aeration tank and the second aerobic aeration tank are 65m3And aeration was continued for 24 hours.
The waste water of production SCR regeneration denitration catalyst can pass through one-level reaction sedimentation tank, second grade reaction sedimentation tank, tertiary reaction sedimentation tank, cooling tower, hydrolysis acidification tank, sludge impoundment, first good oxygen aeration tank, the good oxygen aeration tank of second and MBR membrane bioreactor in proper order, and the accessible discharges away in the accessible discharge water tank after final water quality testing is up to standard.
And the sludge produced by the wastewater for producing the SCR regenerated denitration catalyst is discharged into a sludge tank through a first sludge discharge pipe after passing through the first-stage reaction sedimentation tank, the second-stage reaction sedimentation tank, the third-stage reaction sedimentation tank and the hydrolysis acidification tank, and the sludge produced by the first aerobic aeration tank and the second aerobic aeration tank is discharged into the sludge tank through a second sludge discharge pipe.
Before the wastewater enters the system through the wastewater inlet pipe, sulfuric acid or sodium hydroxide needs to be added to adjust the pH of the wastewater to be neutral.
The reagents added into the first-stage reaction sedimentation tank are sulfuric acid (H) in sequence2SO4) Hydrogen peroxide (H)2O2) Ferrous sulfate (FeSO)4) Sodium hydroxide (NaOH) and polypropylene millstone (PAM), wherein the stirring reaction time is controlled to be 0.8-1 hour, and the sludge settling time is controlled to be 1-1.2 hours. The concentration of each agent is adjusted according to different items, wherein H is used2SO4And NaOH 60% and 32% by mass, respectively.
The agents added into the secondary reaction sedimentation tank are sequentially NaOH and FeSO4PAM, the stirring reaction time is controlled to be 0.5-0.6 hour, and the sludge settling time is controlled to be 1-1.2 hours. The concentration of each drug can be adjusted appropriately according to different items.
The agents added into the three-stage reaction sedimentation tank are sequentially NaOH, recapture agent and FeSO4、PAM、H2SO4The stirring reaction time is controlled to be 1-1.5 hours, and the sludge settling time is controlled to be 1-1.2 hours. The concentration of each drug can be adjusted appropriately according to different items.
The heavy-duty agent is organic sulfur TMT-15, has strong chelating capacity, stable precipitate, small and stable sludge amount, simple post-treatment, no secondary pollution and no damage to ecology.
The cooling tower needs to control the temperature of the wastewater after the three-stage reaction within 40-45 ℃ so as to facilitate the subsequent hydrolysis and acidification of the sewage.
The MBR membrane bioreactor and the MBR membrane bioreactor are used in parallel. The adopted membrane is a hollow fiber membrane, the operation mode is constant pressure, the filtration time of the membrane is 100 minutes, the back washing time is 4 minutes, and the system is automatically controlled by a PLC to operate.
The effective volume of the sludge tank is 70m3The sludge in the pond is compressed into a sludge cake by a plate-and-frame filter press and then is transported to be qualifiedAnd performing professional treatment by a hazardous waste treatment unit.
And sludge generated in the reaction process of the MBR membrane bioreactor can completely flow back to the first aerobic aeration tank.
Has the advantages that:
(1) the wastewater treatment system equipment adopts ground integrated type and can be connected in sequence in a limited space, so that the installation is convenient, the occupied area is small, and the daily sewage treatment capacity can reach 200m3。
(2) The system adopts three-stage reaction to treat sewage, the removal rate of heavy metal can reach 70%, the removal rate of Chemical Oxygen Demand (COD) can reach 65%, and the treatment efficiency of the three-stage reaction is higher.
(3) The invention has less equipment, so even if the device runs for 24 hours, less medicaments need to be added and less staff need to be arranged, thereby effectively saving manpower and material resources.
(4) The removal rate of metal and nonmetal in the final discharged water reaches 85%, the removal rate of Chemical Oxygen Demand (COD) can reach 90%, and other various indexes can reach the national legal discharge standard.
Drawings
FIG. 1 is a diagram of a wastewater treatment system for SCR regeneration denitration catalyst.
Wherein, 1-a first-stage reaction sedimentation tank, 2-a second-stage reaction sedimentation tank, 3-a third-stage reaction sedimentation tank, 4-a cooling tower, 5-a hydrolysis acidification tank, 6-a sludge tank, 7-a first aerobic aeration tank, 8-a second aerobic aeration tank, 9, 10-MBR membrane bioreactor, 11-a discharge water tank, 12-a plate and frame filter press, 13-a sewage inlet pipe, 14-a first water outlet (the first-stage reaction sedimentation tank enters the second-stage reaction sedimentation tank), 15-a second water outlet (the second-stage reaction sedimentation tank enters the third-stage reaction sedimentation tank), 16-a third water outlet (the second-stage reaction sedimentation tank enters the cooling tower), 17-a fourth water outlet (the hydrolysis acidification tank enters the aerobic aeration tank 1), and 18-a fifth water outlet (the first aerobic aeration tank enters the MBR membrane bioreactor), 19-a sixth water outlet, 20-a first sludge discharge pipe (sludge in the first, second and third-stage reaction sedimentation tanks and the hydrolysis acidification tank enters the sludge tank through the first sludge discharge pipe), 21-a second sludge discharge pipe (sludge in the aerobic aeration tank enters the sludge tank through the second sludge discharge pipe), and 22-a sludge discharge port.
Detailed Description
The invention is described in further detail below with reference to the figures and the detailed description, without limiting the invention.
Example 1
An SCR regeneration denitration catalyst effluent disposal system, comprising: the system comprises a first-stage reaction sedimentation tank, a second-stage reaction sedimentation tank, a third-stage reaction sedimentation tank, a cooling tower, a hydrolysis acidification tank, a sludge tank, a first aerobic aeration tank, a second aerobic aeration tank, an MBR (membrane bioreactor), a discharge water tank and a plate-and-frame filter press; wherein, the first-stage reaction sedimentation tank, the second-stage reaction sedimentation tank, the third-stage reaction sedimentation tank, the cooling tower, the hydrolysis acidification tank, the first aerobic aeration tank, the second aerobic aeration tank, the MBR membrane bioreactor and the discharge water tank are sequentially connected and installed according to the wastewater trend, and the plate-and-frame filter press is installed behind the sludge tank; the first-level reaction sedimentation tank, the second-level reaction sedimentation tank, the third-level reaction sedimentation tank and the hydrolysis acidification tank are connected with the sludge tank through a first sludge discharge pipe, and the first aerobic aeration tank and the second aerobic aeration tank are connected with the sludge tank through a second sludge discharge pipe. The effective volume of the hydrolysis acidification tank is 50m3The effective volumes of the first aerobic aeration tank and the second aerobic aeration tank are 65m3The effective volume of the sludge tank is 70m3。
The treatment method of the wastewater treatment system comprises the following steps:
the initial COD value in the waste water is 1197mg/L and contains a large amount of metals and non-metals by using a plate type catalyst which runs 24000H in a certain power plant of the Datang group.
(1) The wastewater enters a first-stage reaction sedimentation tank 1 through a wastewater inlet pipe 13, the pH value of the water is adjusted to 3.0 by adding sulfuric acid, and hydrogen peroxide (H) is added2O2) Ferrous sulfate (FeSO)4) And the molar ratio of the two is 6:1, after flocculation stirring reaches 0.4H, NaOH is added, the pH value of the wastewater is adjusted back to be neutral of 7.0, so that iron salt generates alum floc, PAM (the mass fraction is 0.01%) is continuously added, and the alum floc is enlarged and forms a large amount of flocculent precipitates through the flocculation effect of the PAM.The sediment enters a sludge tank 6 through a first sludge discharge pipe 20, and the wastewater is further lifted to enter a secondary reaction sedimentation tank 2;
(2) after the wastewater enters a secondary reaction sedimentation tank, adding sodium hydroxide (NaOH) to adjust the pH value of the water to 10.9 to be alkaline, and then continuously adding FeSO4PAM, wherein, FeSO4And PAM in the amount of 0.4 wt% and 0.004 wt% in the volume ratio of 1 to 1, and the first stage reaction is treated to precipitate residual floccule. The sediment enters a sludge tank through a first sludge discharge pipe, and the wastewater enters a third-stage reaction sedimentation tank after being lifted;
(3) further adding NaOH to accurately regulate the pH value to about 10.5, and then adding a heavy metal capture agent and FeSO4Carrying out a reaction by using a heavy metal trapping agent and FeSO4Respectively accounting for 1.2 percent and 1.3 percent in mass percent and accounting for 2:3 in volume ratio, adding PAM (accounting for 0.004 percent in mass percent) after the precipitate is formed, enlarging alum blossom and accelerating the precipitation so as to further remove pollutants in water. The sediment enters a sludge tank through a first sludge discharge pipe, and the wastewater enters a cooling tower after being lifted;
(4) starting a cooling tower, and after the wastewater enters, enabling the temperature of the discharged water to be lower than 40 ℃, and then enabling the wastewater to further enter a hydrolysis acidification pool; if the temperature after the three-stage reaction is lower and does not affect the subsequent biological reaction, the wastewater can not flow through the cooling tower.
(5) The hydrolysis acidification function converts non-soluble organic matters in the original wastewater into soluble organic matters, and for industrial wastewater, mainly converts organic matters which are difficult to biodegrade into organic matters which are easy to biodegrade, so that the biodegradability of the wastewater is improved, hydrolysis acidification bacteria need to be cultured in advance, are purchased from a certain sewage treatment plant and have the function of promoting the removal of Chemical Oxygen Demand (COD) in the water, and the wastewater can enter an aerobic tank after staying for 1.2H in a hydrolysis acidification tank;
(6) in order to prolong the hydraulic retention time of the wastewater in the aerobic aeration tank, 2 aerobic tanks with the length of 65m are arranged3And aerating for 24 hours, wherein the hydraulic retention time of the wastewater in the aerobic tank is 10H, and then the wastewater can be further aeratedAnd (4) entering an MBR (membrane bioreactor).
(7) The MBR membrane has good interception effect, the sludge-water separation can be effectively realized after the wastewater is filtered by the membrane module, the quality of the effluent water is obviously improved, the treated water can enter a discharge water tank after reaching the standard through detection, and then can be discharged through a municipal pipe network, and can also be further used as reclaimed water for industrial utilization.
As can be seen from tables 1 and 2 in example 1, the removal rate of COD in the plate type catalyst wastewater by the system can reach 90%, and the final water quality discharge water can reach the national legal requirements, so that the system can effectively treat the SCR regeneration denitration catalyst wastewater.
TABLE 1 COD measured values of wastewater in each plant of the system
| Measured value of COD | Blank space | First-stage reaction sedimentation tank | Two-stage reaction sedimentation tank | Three-stage reaction sedimentation tank | Hydrolysis acidification pool | |
|
MBR membrane bioreactor |
| mg/L | 362.54 | 115.54 | 123.50 | 143.42 | 153.38 | 175.29 | 151.39 | 32.84 |
TABLE 2 Water quality indexes and detection values of discharged water pools
| Detecting items | Detection value (mg/L) | Emission limit (mg/L) |
| pH | 7.06 | 6-9 |
| Chemical Oxygen Demand (COD) | 32.84 | 100 |
| Ammonia nitrogen | 4.6 | 40 |
| Total phosphorus | 0.22 | 2.0 |
| Suspended Substance (SS) | 28 | 70 |
| Total zinc | 0.41 | 2.0 |
| Total copper | 0.10 | 0.3 |
| Total cadmium | 0.02 | 0.1 |
| Total chromium | 0.27 | 1.5 |
| Hexavalent chromium | 0.18 | 0.5 |
| Total vanadium | 0.24 | 1.0 |
| Total lead | 0.17 | 0.5 |
| Total arsenic | 0.04 | 0.2 |
| Total mercury | 0.01 | 0.03 |
Example 2
The regenerated waste catalyst of the batch is derived from a honeycomb catalyst which is operated by 24000H of a power plant of national electrical group. The initial COD value in the wastewater is 1508mg/L, and the wastewater also contains a large amount of metals and nonmetals.
The wastewater treatment system was operated in a similar manner to example 1.
As can be seen from tables 3 and 4, the system can achieve 91% of COD removal rate in the plate type catalyst wastewater, and each detection index of the final water quality is lower than the emission limit value, so that the process is also effective in treating the honeycomb type catalyst.
TABLE 3 COD measured values of the wastewaters in the respective facilities of the system
| Measured value of COD | Blank space | First-stage reaction sedimentation tank | Two-stage reaction sedimentation tank | Three-stage reaction sedimentation tank | Hydrolysis acidification pool | |
|
MBR membrane biological reactionDevice for cleaning the skin |
| mg/L | 462.35 | 139.44 | 115.54 | 151.39 | 147.41 | 175.29 | 139.44 | 43.78 |
TABLE 4 Water quality indexes and detection values of discharged water pool
| Detecting items | Detection value (mg/L) | Emission limit (mg/L) |
| pH | 6.87 | 6-9 |
| Chemical Oxygen Demand (COD) | 43.78 | 100 |
| Ammonia nitrogen | 9.4 | 40 |
| Total phosphorus | 0.18 | 2.0 |
| Suspended Substance (SS) | 31 | 70 |
| Total zinc | 0.18 | 2.0 |
| Total copper | 0.02 | 0.3 |
| Total cadmium | 0.04 | 0.1 |
| Total chromium | 0.63 | 1.5 |
| Hexavalent chromium | 0.16 | 0.5 |
| Total vanadium | 0.37 | 1.0 |
| Total lead | 0.29 | 0.5 |
| Total arsenic | 0.01 | 0.2 |
| Total mercury | 0.01 | 0.03 |
Example 3
The waste catalyst regenerated in the batch is derived from a corrugated catalyst which is operated by 24000H in a certain power plant of the Datang group. The initial COD value in the wastewater is 1353mg/L, and the wastewater also contains a large amount of metals and nonmetals.
The wastewater treatment system was operated in a similar manner to example 1.
As can be seen from tables 5 and 6, the removal rate of COD in the plate type catalyst wastewater by the system can reach 92%, and each detection index of the final water quality is lower than the emission limit value, which indicates that the system is also effective in treating the corrugated catalyst.
TABLE 5 COD measured values of the wastewaters in the respective facilities of the system
| Measured value of COD | Blank space | First-stage reaction sedimentation tank | Two-stage reaction sedimentation tank | Three-stage reaction sedimentation tank | Hydrolysis acidification pool | |
|
MBR membrane bioreactor |
| mg/L | 332.49 | 79.06 | 90.92 | 126.49 | 205.56 | 209.51 | 167.48 | 28.16 |
TABLE 6 Water quality indexes and detection values of discharged water pool
| Detecting items | Detection value (mg/L) | Emission limit (mg/L) |
| pH | 7.14 | 6-9 |
| Chemical Oxygen Demand (COD) | 32.16 | 100 |
| Ammonia nitrogen | 10.4 | 40 |
| Total phosphorus | 0.28 | 2.0 |
| Suspended Substance (SS) | 19 | 70 |
| Total zinc | 0.17 | 2.0 |
| Total copper | 0.07 | 0.3 |
| Total cadmium | 0.03 | 0.1 |
| Total chromium | 0.43 | 1.5 |
| Hexavalent chromium | 0.04 | 0.5 |
| Total vanadium | 0.31 | 1.0 |
| Total lead | 0.18 | 0.5 |
| Total arsenic | 0.04 | 0.2 |
| Total mercury | 0.01 | 0.03 |
Claims (7)
1. The utility model provides a SCR regeneration denitration catalyst effluent disposal system which characterized in that: including one-level reaction sedimentation tank (1), second grade reaction sedimentation tank (2), tertiary reaction sedimentation tank (3), cooling tower (4), hydrolysis-acidification tank (5), sludge impoundment (6), first good oxygen aeration tank (7), second good oxygen aeration tank (8), MBR membrane bioreactor (9, 10), discharge pond (11) and plate and frame filter press (12), wherein: the device comprises a primary reaction sedimentation tank (1), a secondary reaction sedimentation tank (2), a tertiary reaction sedimentation tank (3), a cooling tower (4), a hydrolysis acidification tank (5), a first aerobic aeration tank (7), a second aerobic aeration tank (8), MBR membrane bioreactors (9, 10) and a discharge water tank (11), which are sequentially connected and installed according to the wastewater trend, wherein a plate and frame filter press (12) is installed behind a sludge tank (6); the bottom of the first-stage reaction sedimentation tank (1), the bottom of the second-stage reaction sedimentation tank (2), the bottom of the third-stage reaction sedimentation tank (3) and the bottom of the hydrolysis acidification tank (5) are connected with the sludge tank (6) through a first sludge discharge pipe (20), and the first aerobic aeration tank (7) and the second aerobic aeration tank (8) are connected with the sludge tank (6) through a second sludge discharge pipe (21).
2. The SCR regeneration denitration catalyst wastewater treatment system of claim 1, wherein: the wastewater enters the system through a wastewater inlet pipe (13).
3. The SCR regeneration denitration catalyst wastewater treatment system of claim 1, wherein: the effective volume of the hydrolysis acidification tank (5) is 50m3Hydraulic retention time of 08-1.2 hours.
4. The SCR regeneration denitration catalyst wastewater treatment system of claim 1, wherein: the effective volumes of the first aerobic aeration tank (7) and the second aerobic aeration tank (8) are 65m3And aeration was continued for 24 hours.
5. The SCR regeneration denitration catalyst wastewater treatment system of claim 1, wherein: the MBR membrane bioreactors (9 and 10) are used in parallel, the adopted membrane is a hollow fiber membrane, the operation mode is constant pressure, and the system is automatically controlled by a PLC to operate.
6. The SCR regeneration denitration catalyst wastewater treatment system of claim 1, wherein: the effective volume of the sludge tank is 70m3。
7. The SCR regeneration denitration catalyst wastewater treatment system of claim 1, wherein: and sludge generated in the reaction process of the MBR membrane bioreactor can completely flow back to the first aerobic aeration tank.
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