CN111013354A - Sludge drying tail gas treatment system and method - Google Patents
Sludge drying tail gas treatment system and method Download PDFInfo
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- CN111013354A CN111013354A CN201911377959.6A CN201911377959A CN111013354A CN 111013354 A CN111013354 A CN 111013354A CN 201911377959 A CN201911377959 A CN 201911377959A CN 111013354 A CN111013354 A CN 111013354A
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Abstract
The invention discloses a sludge drying tail gas treatment system and a method thereof, wherein the sludge drying tail gas treatment system comprises a sludge drying machine, an induced draft fan, a cyclone separator, a spray tower, a blower, a sewage storage tank, a nitrification tank, a denitrification tank and an active carbon absorption tower; the sludge drier, the induced draft fan, the cyclone separator and the spray tower are sequentially connected in series; the spray tower is communicated with the nitrification tank through a blower; the sewage storage tank, the denitrification tank, the nitrification tank and the activated carbon absorption tower are connected in series in sequence. The invention also correspondingly provides a sludge drying tail gas treatment method, which comprises the steps of carrying out chemical oxidation treatment on the tail gas, carrying out biochemical degradation, and finally carrying out activated carbon adsorption and then discharging. The invention finally achieves the technical effects of treating waste by waste and cooperatively treating the tail gas and the waste water, realizes the standard discharge of the sludge drying tail gas and the waste water, saves energy, protects environment, does not generate secondary pollution, and simultaneously has the advantages of saving the occupied area of equipment and the maintenance workload of the equipment and reducing the comprehensive operation cost of the equipment.
Description
Technical Field
The invention relates to the technical field of environmental protection, in particular to a treatment system and a treatment method applicable to sludge drying tail gas.
Background
Sludge drying is an important technical means for realizing sludge reduction and subsequent treatment, the treatment modes of sludge drying can be divided into direct contact heat drying and indirect non-contact heat drying, and heat sources adopted by sludge drying mainly comprise solar energy, electric energy, methane gas, steam, waste heat and the like. The direct contact heat drying treatment is that the sludge is directly contacted with a heat medium, and the heat transfer efficiency and the heat energy utilization rate are high, so the direct contact heat drying treatment is commonly used in the sludge drying technology.
The anaerobic sludge digestion technology realizes the recovery of energy in sludge by recovering carbon energy in sludge and converting the carbon energy into methane gas; and the methane gas is reused for heat drying treatment of digested sludge dewatered mud cakes so as to achieve sludge reduction and heat energy recycling. After the sludge is subjected to anaerobic digestion treatment, macromolecular nitrogen-containing compounds are degraded into micromolecular ammonia nitrogen, free ammonia and other substances, and the digested sludge is mechanically dehydrated to obtain dehydrated sludge cakes. The dehydrated sludge cake can generate tail gas containing components such as high-concentration ammonia gas, organic volatile gas, carbon dioxide and the like in the process of direct contact heat drying treatment, and along with the rise of the sludge drying operation temperature, the pollutant content in the tail gas is also increased along with the rise, the components of pollutants are more complex, the treatment difficulty of the sludge drying tail gas is increased, and serious environmental pollution is caused if the sludge drying tail gas is discharged without effective treatment. Therefore, the cleanliness of the sludge drying tail gas becomes an important pollution emission control index in the sludge treatment technology.
The existing sludge drying tail gas treatment technology mainly has the following defects:
(1) the current sludge drying tail gas treatment technology which is more generally applied comprises a mode of combining a biological deodorization box body or a chemical deodorization and biological deodorization box body, and mainly utilizes a special deodorization strain which is adsorbed and grown on the surface of a filler in the biological deodorization box body to adsorb and degrade pollutants in waste gas. The method has the defects of low treatment load, single pollutant treatment type, unstable treatment effect, large occupied area and inconvenient maintenance, and more importantly, the circulating wastewater generated in the tail gas treatment process needs additional treatment and has the defect of secondary pollution.
(2) The deodorization technologies such as UV, catalytic oxidation and the like can also be applied to the sludge drying tail gas treatment, but the method has limited effect on the sludge drying tail gas treatment, and is difficult to treat the sludge drying tail gas with high concentration, complex components and fluctuating components until the emission reaches the standard.
It is worth noting that in the existing sludge drying tail gas treatment technology, a spray tower and a biological deodorization box are mainly adopted to cool and deodorize the tail gas, the thorough biochemical degradation of pollutants in the tail gas is not realized, and the facility occupies a large area and is inconvenient to maintain. In view of this, it is needed to develop a sludge drying tail gas co-treatment system and method thereof with good treatment effect, low cost, strong practicability and good environmental protection in view of the characteristics of the sludge drying tail gas and the characteristics of the sewage biochemical denitrification treatment process.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provide the sludge drying tail gas cooperative treatment system and the method thereof, which have the advantages of good treatment effect, low cost, strong practicability and no secondary pollution.
In order to solve the technical problems, the invention adopts the following technical scheme:
a sludge drying tail gas treatment system comprises a sludge drying machine, a draught fan, a cyclone separator, an acidic spray tower, an alkaline spray tower, a blower, a sewage storage tank, a nitrification tank, a denitrification tank and an activated carbon absorption tower; the sludge drier, the induced draft fan, the cyclone separator, the acidic spray tower and the alkaline spray tower are sequentially connected in series; the acid spray tower and the alkaline spray tower are respectively communicated with a sewage storage pool; the alkaline spray tower is communicated with the nitrification tank through a blower; the sewage storage tank, the denitrification tank, the nitrification tank and the activated carbon absorption tower are sequentially connected in series.
As a further improvement of the invention, the nitrification tank comprises a first-stage nitrification tank and a second-stage nitrification tank, and the denitrification tank comprises a first-stage denitrification tank and a second-stage denitrification tank; a reflux pump is arranged between the nitrification tank and the denitrification tank.
As a further improvement of the invention, the top of the nitrification tank and the denitrification tank is in a totally-enclosed form.
As a further improvement of the invention, the top parts of the acid spray tower and the alkaline spray tower are provided with anti-blocking spiral nozzles, an outlet pipe at the top of the spray tower is provided with a demister, the spray tower is internally provided with a circulating water tank, and the circulating water tank is provided with a water replenishing pipe.
As a further improvement of the invention, the top of the alkaline spray tower is provided with a gas outlet which is communicated with aeration branch pipes arranged at the bottoms of the primary nitrification tank and the secondary nitrification tank through a blower.
As a further improvement of the invention, the aeration device adopted by the aeration branch pipe is a microporous aeration disk or a microporous aeration pipe.
As a further improvement of the invention, the blower is any one of a Roots blower, a centrifugal blower and a screw blower; the blower is controlled by adopting variable frequency; and a one-way valve is arranged at the outlet of the blower.
As a further improvement of the invention, the blower is respectively connected with a waste gas branch air pipe and an air main air pipe.
As a further improvement of the invention, the exhaust gas branch air pipe and the air main air pipe respectively convey the pre-treatment drying tail gas and air, and the ratio of the pre-treatment drying tail gas to the air flow is controlled to be 0.1-1: 1.
As a further improvement of the invention, the activated carbon absorption tower is provided with a discharge pipe and a detection probe.
As a further improvement of the invention, the detection probe comprises an ammonia gas detection probe and a hydrogen sulfide detection probe.
As a further improvement of the invention, the processing system also comprises a dosing pump and a medicine storage box; and the chemical oxidation medicament in the medicament storage box is conveyed to the acid spray tower and the alkaline spray tower by the medicament feeding pump.
As a further improvement of the invention, the acid spray tower and the alkaline spray tower are provided with a pH sensor and a foam sensor which are interlocked with the PLC and the dosing pump.
As a general technical concept, the invention also provides a method for treating the sludge drying tail gas, which comprises the following steps:
s1, drying the dewatered sludge cake after anaerobic digestion in a sludge drier, and feeding the generated sludge drying tail gas into a cyclone separator for tail gas dust removal;
s2, allowing the dedusted sludge drying tail gas to enter an acidic spray tower, and contacting and reacting with an acidic oxidizing agent for 2-10S;
s3, allowing the sludge drying tail gas after acidic oxidation to enter an alkaline spray tower, and allowing the sludge drying tail gas to contact and react with an alkaline oxidation agent for 2-10S;
s4, conveying the sludge drying tail gas subjected to alkaline oxidation in the step S3 and air to a nitrification tank according to a flow ratio of 0.1-1: 1, and performing biochemical degradation on the sludge drying tail gas;
s5, feeding the sludge drying tail gas after biochemical degradation into an active carbon tower, contacting with active carbon for adsorption for 2-10S, and discharging;
s6, the wastewater generated in the spray tower in the steps S3 and S4 enters a wastewater storage tank, is mixed with the wastewater generated by sludge dehydration and sludge drying, is conveyed to a nitrification and denitrification wastewater biochemical denitrification system, and is discharged after two-stage nitrification and denitrification treatment.
As a further improvement of the invention, in step S1, the dewatered sludge cake is dried by direct contact heat drying, and the heat source for drying the dewatered sludge cake is generated by burning methane gas generated by an anaerobic digestion system.
In a further improvement of the invention, in step S2, the acidic oxidizing agent is obtained by mixing dilute sulfuric acid and hydrogen peroxide, the mass fraction of sulfuric acid in the acidic oxidizing agent is 10% -30%, the mass fraction of hydrogen peroxide is 1% -5%, and the pH value in the acidic spray tower is 2-4.
In a further improvement of the present invention, in step S3, the alkaline oxidizing agent is obtained by mixing liquid alkali and sodium hypochlorite, the mass fraction of sodium hydroxide in the alkaline oxidizing agent is 5% to 10%, the mass fraction of sodium hypochlorite is 1% to 2%, and the pH value in the alkaline spray tower is 10 to 12.
As a further improvement of the present invention, in step S6, the method further includes: mixed wastewater discharged from the sewage storage tank firstly enters a denitrification tank and then enters a nitrification tank, mixed liquid in the nitrification tank flows back to the denitrification tank through a reflux pump, and the reflux ratio is controlled to be 100-400%; the DO value of the nitrification tank is 0.5 mg/L-2.5 mg/L, and the DO value of the denitrification tank is 0.1 mg/L-0.5 mg/L, MLSS, and the DO value is 5 g/L-20 g/L.
The innovation points of the invention are as follows:
aiming at the defects that the tail gas is only cooled and deodorized by adopting a spray tower and a biological deodorization box in the prior sludge drying tail gas treatment technology, the thorough biochemical degradation of pollutants in the tail gas is not realized, and the occupied area is large and the maintenance is inconvenient, the invention combines the components and the characteristics of the sludge drying tail gas and adopts a method combining the secondary chemical oxidation treatment, the secondary nitrification and denitrification sewage biochemical denitrification treatment and the activated carbon adsorption to carry out the comprehensive and thorough biochemical degradation treatment on the sludge drying tail gas and the wastewater generated in the tail gas treatment process. In the technical scheme of the invention, after the sludge drying tail gas is simply dedusted, the sludge drying tail gas is subjected to secondary acid-base oxidation pretreatment by a chemical oxidation technology to reduce pollutant components and concentration in the sludge drying tail gas; then, a secondary nitrification and denitrification sewage biochemical denitrification system is used for carrying out efficient biochemical degradation on pollutant components in the sludge drying tail gas, meanwhile, waste water generated in the chemical oxidation treatment process is mixed with waste water generated in sludge dehydration and sludge drying and then conveyed to a denitrification tank and a nitrification tank, and carbon-containing inorganic substances and organic components in the sludge drying tail gas and the mixed waste water are used for supplementing inorganic carbon sources and organic carbon sources required by active floras in the nitrification and denitrification system, so that the sludge drying tail gas and the mixed waste water are subjected to synergistic treatment; and finally, adsorbing the sludge drying tail gas subjected to the biochemical denitrification treatment by using activated carbon to finally meet the requirement of pollutant emission limit in the emission Standard of malodorous pollutants (GB14554-93), and performing ultrafiltration treatment on the drainage of the biochemical denitrification system to obtain water for a spray tower or further purifying for other purposes. The technical scheme of the invention finally achieves the technical effects of treating waste by waste and cooperatively treating the tail gas and the waste water, realizes the standard discharge of the sludge drying tail gas and the waste water, saves energy, protects environment, does not generate secondary pollution, and simultaneously has the advantages of saving the occupied area of equipment and the maintenance workload of the equipment and reducing the comprehensive operation cost of the equipment.
Compared with the prior art, the invention has the advantages that:
1. according to the sludge drying tail gas treatment system disclosed by the invention, the acidic spray tower, the alkaline spray tower, the sewage storage tank, the nitrification tank and the denitrification tank are arranged, so that on one hand, the spray tower is utilized to carry out chemical oxidation treatment on the sludge drying tail gas, and the pollutant components and concentration in the tail gas are reduced; on the other hand, the wastewater generated in the chemical oxidation treatment process is mixed with the wastewater generated in the sludge dehydration and sludge drying process and then is conveyed into the denitrification tank and the nitrification tank, and the inorganic carbon source and the organic carbon source required by the active flora in the nitrification and denitrification system are supplemented by the carbon-containing inorganic substances and the organic components in the sludge drying tail gas and the mixed wastewater, so that the nitrification and denitrification reaction efficiency is improved, namely the biochemical denitrification efficiency of the sludge drying tail gas in the nitrification tank and the denitrification tank is promoted. Finally, the technical effects of treating waste by waste and cooperatively treating the tail gas and the waste water are achieved, the sludge drying tail gas and the waste water are discharged up to the standard, the sludge drying tail gas and the waste water are energy-saving and environment-friendly, secondary pollution is avoided, and the sludge drying tail gas and the waste water have the advantages of saving the occupied area of equipment and saving the maintenance workload of the equipment.
2. The sludge drying tail gas treatment system disclosed by the invention is provided with a secondary nitrification and denitrification system, so that nitrogen-containing waste gas in the sludge drying tail gas is firstly converted into nitrite nitrogen and nitrate nitrogen under the conditions of aeration and inorganic carbon sources (such as carbonate, bicarbonate and the like) by nitrifying bacteria, and then nitrogen is generated under the conditions of oxygen deficiency and organic carbon sources by denitrifying bacteria, so that denitrification and organic matter degradation are completed. Compared with the traditional biological deodorization box, the nitrification and denitrification system has the advantages of wide pool volume, long contact reaction time, various floras, strong activity, high reaction efficiency and the like as the sewage treatment process with wide existence range and mature application. The method is applied to the sludge drying tail gas treatment, has important application value and strong operability for realizing the thorough biochemical degradation of pollutants in the sludge drying tail gas and the high-efficiency treatment of the waste water generated by the tail gas oxidation treatment.
3. The sludge drying tail gas treatment system disclosed by the invention utilizes the pH sensor and the foam sensor which are arranged in the spray tower and are interlocked with the PLC and the dosing pump, so that the chemical reaction progress in the spray tower can be better monitored, the chemical agent conveying amount can be automatically controlled, and the purpose of effectively reducing the consumption of the chemical agent can be realized.
4. The sludge drying tail gas treatment method disclosed by the invention carries out comprehensive and thorough degradation treatment on the sludge drying tail gas, waste water generated in the tail gas treatment process and waste water generated in the sludge dewatering and sludge drying treatment process by a method combining 'secondary chemical oxidation treatment, secondary nitrification and denitrification sewage biochemical denitrification and activated carbon adsorption', organically combines waste gas treatment and waste water treatment, achieves the effect of cooperatively treating pollutants in the tail gas and the waste water, realizes standard discharge of the tail gas and the waste water, and obviously reduces the comprehensive operation cost.
Drawings
FIG. 1 is a schematic structural diagram of a sludge drying tail gas treatment system according to the present invention.
FIG. 2 is an electrical control schematic diagram of the sludge drying tail gas treatment system of the present invention.
The reference numerals in the figures denote:
1. a sludge drier; 2. an induced draft fan; 3. a cyclone separator; 4. an acid spray tower; 5. an alkaline spray tower; 6. a filler layer; 7. an evacuation valve; 8. a dosing pump; 9. a medicine storage box; 91. an acidic reagent tank; 92. an alkaline kit; 10. a pH sensor; 12. a foam sensor; 13. a PLC controller; 14. a blower; 15. a waste gas branch air pipe; 16. a main air duct; 17. a sewage storage tank; 181. a first-stage nitrification tank; 182. a secondary nitrification tank; 191. a first-stage denitrification tank; 192. a secondary denitrification tank; 20. a reflux pump; 21. an aeration branch pipe; 22. an ultrafiltration device; 23. an activated carbon absorption tower; 24. a discharge pipe; 25. and (6) detecting the probe.
Detailed Description
The invention is further described below with reference to the drawings and specific preferred embodiments of the description, without thereby limiting the scope of protection of the invention.
As shown in fig. 1, the sludge drying tail gas treatment system of the present invention comprises: the system comprises a sludge drier 1, an induced draft fan 2, a cyclone separator 3, an acidic spray tower 4, an alkaline spray tower 5, a blower 14, a sewage storage tank 17, a nitrification tank, a denitrification tank and an active carbon absorption tower 23; the sludge drier 1, the induced draft fan 2, the cyclone separator 3, the acid spray tower 4 and the alkaline spray tower 5 are connected in series in sequence; the acid spray tower 4 and the alkaline spray tower 5 are respectively communicated with a sewage storage tank 17; the alkaline spray tower 5 is communicated with the nitrification tank through a blower 14; the sewage storage tank 17, the denitrification tank, the nitrification tank and the activated carbon absorption tower 23 are connected in series in sequence.
In this embodiment, a waste gas outlet at the top of the sludge drying machine 1 is connected with a gas inlet of the cyclone separator 3 through the induced draft fan 2, a gas outlet of the cyclone separator 3 is connected to the bottom of the acidic spray tower 4, a gas outlet at the top of the acidic spray tower 4 is connected to the bottom of the alkaline spray tower 5, a gas outlet at the top of the alkaline spray tower 5 is connected to the bottoms of the primary nitrification tank 181 and the secondary nitrification tank 182 through the blower 14, and the top of the secondary nitrification tank 182 is provided with the activated carbon adsorption tower 23.
In this embodiment, the bottoms of the acidic spray tower 4 and the alkaline spray tower 5 are connected to the sewage reservoir 17 through the emptying valve 7, and the sewage reservoir 17, the primary denitrification tank 191, the primary nitrification tank 181, the secondary denitrification tank 192 and the secondary nitrification tank 182 are sequentially connected in series. Furthermore, the top of the nitrification tank and the denitrification tank is in a totally-enclosed form. It can be understood that, in this embodiment, the secondary nitrification and denitrification treatment process is adopted, and the denitrification tank is placed in front of the nitrification tank, so that the carbon source in the sewage can be directly utilized, the carbon source can be saved, and the alkalinity required by the nitrification reaction can be supplemented by the alkali generated by denitrification.
Further, in order to enable the sludge drying tail gas to be in contact reaction in the spray tower more fully, chemical agents in the medicine storage box 9 are conveyed into the spray tower through the medicine feeding pump 8. During working, a chemical agent is atomized into small droplets through a nozzle arranged at the top of the spray tower, a liquid film is formed on the surface of the filler layer 6, and the liquid film of the chemical agent and the sludge drying tail gas are in countercurrent contact reaction in the filler layer 6. It will be appreciated that in order to improve the spraying efficiency of the spray nozzle and prevent it from clogging, the spray nozzle at the top of the spray tower may be provided as an anti-clogging screw nozzle or other spray nozzle capable of achieving efficient spraying. In addition, in order to improve the working efficiency of the spray tower, a demister is further arranged on an outlet pipe at the top of the spray tower, and a water replenishing pipe is arranged on a circulating water tank (not shown in fig. 1) at the bottom of the spray tower.
As shown in fig. 2, in order to better monitor the progress of the chemical reaction in the spray tower and control the chemical agent delivery rate, a pH sensor 10 and a foam sensor 12 are disposed in the circulating water tank at the bottom of the spray tower, and the sensors are interlocked with the PLC controller 13 and the dosing pump 8, so as to achieve the purpose of automatically controlling the chemical agent delivery rate and effectively reducing the chemical agent consumption. It will be appreciated that in order to prevent foam from overflowing from the spray tower, a defoaming agent may be added to the spray tower.
In this embodiment, the sludge drying tail gas is sent to the nitrification tank through the blower 14 after being subjected to the acidic spraying treatment and the alkaline spraying treatment. In order to improve the biochemical degradation efficiency of the sludge drying tail gas in the nitrification tank, fresh air is also conveyed into the nitrification tank through the air blower 14. Specifically, the sludge drying tail gas from the alkaline spray tower 5 is compressed by the blower 14 and then enters the waste gas branch air pipe 15, the fresh air is compressed by the blower 14 and then enters the main air pipe 16, the sludge drying tail gas and the fresh air are mixed and then are conveyed to the bottoms of the primary nitrification tank 181 and the secondary nitrification tank 182, and the biochemical bacteria in the nitrification tanks are used for performing biochemical degradation on the sludge drying tail gas. The biochemically degraded sludge drying tail gas is absorbed by an activated carbon absorption tower 23 arranged at the top of the secondary nitrification tank 182 and then discharged. It can be understood that in order to better control the gas delivery amount entering the bottom of the nitrification tank and the flow ratio of the sludge drying tail gas to the fresh air, the blower 14 can adopt variable frequency control, and a one-way valve is installed at the outlet of the blower 14. Further, the blower 14 in the present embodiment may be specifically a roots blower, a centrifugal blower, or a screw blower, and any blower that can meet the gas delivery control requirements may be applied to the present invention.
Furthermore, in order to improve the solubility and the biochemical degradation rate of the sludge drying tail gas in the nitrification tank, aeration branch pipes 21 are arranged at the bottoms of the primary nitrification tank 181 and the secondary nitrification tank 182. It is understood that the aeration device type of the aeration branch pipe 21 may be a micro-porous aeration disk or a micro-porous aeration pipe in order to disperse the sludge drying tail gas more uniformly in the nitrification tank.
Further, in order to monitor the cleanliness of the finally discharged sludge drying tail gas, the air inlet of the activated carbon absorption tower 23 is communicated with the surface of the secondary nitrification tank 182, the air outlet of the activated carbon absorption tower 23 is communicated with the discharge pipe 24, and the finally discharged sludge drying tail gas is detected by arranging the detection probe 25 on the discharge pipe 24. It is understood that the detection probe 25 may include an ammonia gas detection probe and a hydrogen sulfide detection probe for more accurately detecting the components of the discharged sludge drying tail gas. And a corresponding gas detection probe can be arranged according to the actual detection requirement.
In this embodiment, the acidic spray tower 4 and the alkaline spray tower 5 discharge the salt-containing wastewater in the spray towers into the sewage reservoir 17 through the emptying valve 7, and mix the salt-containing wastewater with the wastewater generated in the sludge dewatering and sludge drying treatment processes. The salt-containing wastewater in the wastewater storage tank 17 is first transferred to the primary denitrification tank 191 for denitrification treatment. Further, in order to more thoroughly realize the biochemical degradation of wastewater, a reflux pump 20 is arranged between the first-stage nitrification tank 181 and the first-stage denitrification tank 191 and between the second-stage nitrification tank 182 and the second-stage denitrification tank 192, and nitrate formed in the nitrification tank is refluxed to the denitrification tank through the reflux pump 20.
In this embodiment, the water outlet of the secondary nitrification tank 182 is communicated with the ultrafiltration device 22, the wastewater after the two-stage nitrification and denitrification treatment is discharged from the water outlet of the secondary nitrification tank 182, and after being filtered by the ultrafiltration device 22, the ultrafiltration product water can be used for replenishing water in an acidic spray tower and an alkaline spray tower, and can also be further purified for other purposes; the ultra-filtered sludge can flow back to the denitrification tank to continue to participate in denitrification reaction.
In addition, the embodiment also provides a method for treating the sludge drying tail gas, which comprises the following steps:
s1, drying the dewatered sludge cake after anaerobic digestion in a sludge drier, and feeding the generated sludge drying tail gas into a cyclone separator for tail gas dust removal;
s2, allowing the dedusted sludge drying tail gas to enter an acidic spray tower, and contacting and reacting with an acidic oxidizing agent for 2-10S;
s3, allowing the sludge drying tail gas after acidic oxidation to enter an alkaline spray tower, and allowing the sludge drying tail gas to contact and react with an alkaline oxidation agent for 2-10S;
s4, conveying the sludge drying tail gas subjected to alkaline oxidation in the step S3 and air to a nitrification tank according to a flow ratio of 0.1-1: 1, and performing biochemical degradation on the sludge drying tail gas;
s5, feeding the sludge drying tail gas after biochemical degradation into an active carbon tower, contacting with active carbon for adsorption for 2-10S, and discharging;
s6, the wastewater generated in the spray tower in the steps S3 and S4 enters a wastewater storage tank, is mixed with the wastewater generated by sludge dehydration and sludge drying, is conveyed to a nitrification and denitrification wastewater biochemical denitrification system, and is discharged after two-stage nitrification and denitrification treatment.
Specifically, in step S1, the sludge drying machine 1 dries the digested and dewatered sludge cake by direct contact heat drying, and the heat source for drying the dewatered sludge cake is generated by burning methane gas generated by an anaerobic digestion system. Tail gas discharged by the sludge drier 1 is conveyed to the cyclone separator 3 through the draught fan 2 for tail gas dust removal, and granular sludge, dust and the like collected in the cyclone separator 3 are conveyed to a discharge port of the sludge drier 1 and mixed with dried sludge for subsequent treatment.
In step S2, the dedusted sludge drying tail gas enters the bottom of the acidic spray tower 4 through the outlet of the cyclone separator 3, and is in countercurrent contact reaction with the acidic oxidation agent sprayed from the top of the spray tower in the packing layer 6. Further, the dosing pump 8 conveys the oxidizing agent in the acidic oxidizing agent box 91 into the acidic spray tower 4, and the oxidizing agent is atomized into small droplets through an anti-clogging spiral nozzle arranged at the top of the acidic spray tower 4, so that a liquid film is formed on the surface of the filler layer 6. Further, the oxidizing agent in the acidic agent tank 91 is obtained by mixing sulfuric acid and hydrogen peroxide. Specifically, the mass fraction of sulfuric acid in the acidic oxidizing agent is 10%, and the mass fraction of hydrogen peroxide is 1%. In order to more fully realize the acid oxidation of the sludge drying tail gas, the contact reaction time of the sludge drying tail gas and the acid oxidizing agent in the packing layer 6 is set to be 4 s.
In step S3, the sludge drying tail gas after acid oxidation enters the bottom of the alkaline spray tower 5 through the demister at the top of the acid spray tower 4, and contacts and reacts with the alkaline oxidizing agent sprayed from the top of the spray tower in the packing layer 6 in a countercurrent manner. Further, the chemical feeding pump 8 conveys the oxidizing agent in the alkaline oxidizing agent box 92 into the alkaline spray tower 5, and the oxidizing agent is atomized into small droplets through an anti-clogging spiral nozzle arranged at the top of the alkaline spray tower 5, so that a liquid film is formed on the surface of the filler layer 6. Further, the oxidizing agent in the alkaline agent tank 92 is obtained by mixing sodium hydroxide and a sodium hypochlorite solution. Specifically, the alkaline oxidizing agent contains 5% by mass of sodium hydroxide and 1% by mass of sodium hypochlorite. In order to more fully realize the alkaline oxidation of the sludge drying tail gas, the contact reaction time of the sludge drying tail gas and the alkaline oxidation agent in the packing layer 6 is set to be 4 s.
It will be appreciated that in order to prevent foam in the spray tower from overflowing, a defoaming agent may be introduced into the tank 9 and delivered into the spray tower together with the oxidizing agent by the dosing pump 8. In order to better monitor the chemical reaction progress in the spray tower and control the delivery amount of the oxidizing agent, a pH sensor 10 and a foam sensor 12 are arranged in a circulating water tank at the bottom of the spray tower, and the sensors are interlocked with a PLC (programmable logic controller) 13 and a dosing pump 8. Specifically, the pH in the acidic spray tower was set to 4, and the pH in the alkaline spray tower was set to 10.
After the two-stage chemical oxidation treatment, gas components which are high in solubility and easy to oxidize in the dried sludge tail gas react with an oxidizing agent to generate substances such as ammonium sulfate, sodium sulfate and sodium carbonate, so that the gas components in the tail gas can be effectively reduced, and the subsequent treatment difficulty for performing biochemical degradation on the tail gas is reduced.
In step S4, the sludge drying tail gas after alkaline oxidation is discharged through a demister at the top of the alkaline spray tower 5, and enters the waste gas branch air duct 15 after being compressed by the roots blower, the fresh air enters the main air duct 16 after being compressed by the roots blower, and the sludge drying tail gas in the waste gas branch air duct 15 is mixed with the fresh air in the main air duct 16 and then is conveyed to the primary nitrification tank 181 and the secondary nitrification tank 182. Specifically, the mixed gas is uniformly distributed to the liquid level from the bottom of the nitrification tank through the microporous aeration discs on the aeration branch pipes 21 at the bottom of the nitrification tank, carbon-containing inorganic substances and organic components in the sludge drying tail gas are dissolved and biochemically degraded by utilizing active biochemical flora with rich types and high concentration in the nitrification tank and the denitrification tank while carrying out aeration and oxygen supply on the nitrification tank, carbon sources required by the active biochemical flora in the nitrification tank and the denitrification tank are supplemented, and the efficiency of biochemical degradation reaction is effectively improved. Further, in order to control the oxygen content entering the nitrification reactor, the gas flow ratio of the waste gas branch air pipe 15 to the air main air pipe 16 is set to be 0.5: 1.
In step S5, the biochemically degraded sludge drying tail gas is absorbed by the activated carbon absorption tower 23 disposed at the top of the secondary nitrification tank 182 and then discharged. Further, an air inlet of the activated carbon absorption tower 23 is communicated with the surface of the secondary nitrification tank 182, an air outlet of the activated carbon absorption tower 23 is communicated with the discharge pipe 24, and the finally discharged sludge drying tail gas is detected by arranging the detection probe 25 on the discharge pipe 24. Specifically, the contact time of the sludge drying tail gas and the activated carbon is 2s, the adsorbed tail gas is discharged through the discharge pipe 24, and the content of hydrogen sulfide and ammonia gas is detected by using the detection probe 25 arranged on the discharge pipe 24, and the result shows that the sludge drying tail gas discharged in the embodiment meets the pollutant discharge limit requirement in the odor pollutant discharge standard (GB 14554-93).
In step S6, salt in the spray liquid in the spray tower is continuously accumulated along with the increase of the spraying operation time in steps S3 and S4, and when the salt in the spray liquid is saturated, the acidic spray tower 4 and the alkaline spray tower 5 discharge the salt-containing wastewater into the sewage storage tank 17 through the emptying valve 7. In addition, the sewage reservoir 17 also stores wastewater generated by sludge dewatering and sludge drying. Specifically, the mixed wastewater in the wastewater storage tank 17 is first transferred to the primary denitrification tank 191 for denitrification. Further, in order to more thoroughly realize the biochemical degradation of wastewater, a reflux pump 20 is provided between the first-stage nitrification tank 181 and the first-stage denitrification tank 191, and between the second-stage nitrification tank 182 and the second-stage denitrification tank 192, and nitrate formed in the nitrification tank is refluxed to the denitrification tank by the reflux pump 20. Furthermore, the nitrate reflux ratio is controlled at 200%, DO in the nitrification tank is 2.0mg/L, and DO in the denitrification tank is 0.5mg/L, MLSS and is 10 g/L.
In this embodiment, the wastewater after the two-stage nitrification and denitrification treatment is discharged from the water outlet of the two-stage nitrification tank 182, and filtered by the ultrafiltration device 22 to reach the relevant water reuse standard or discharge standard. Specifically, the ultrafiltration produced water can be used for replenishing water in an acid spray tower and an alkaline spray tower, and can also be used for other purposes after further purification treatment; the ultra-filtered sludge can flow back to the denitrification tank to continue to participate in denitrification reaction.
Although the present invention has been described with reference to the preferred embodiments, it is not intended to be limited thereto. Those skilled in the art can make numerous possible variations and modifications to the present invention, or modify equivalent embodiments to equivalent variations, without departing from the scope of the invention, using the teachings disclosed above. Therefore, any simple modification, equivalent change and modification made to the above embodiments according to the technical spirit of the present invention should fall within the protection scope of the technical scheme of the present invention, unless the technical spirit of the present invention departs from the content of the technical scheme of the present invention.
Claims (10)
1. The utility model provides a sludge drying tail gas processing system which characterized in that: comprises a sludge drier (1), a draught fan (2), a cyclone separator (3), an acid spray tower (4), an alkaline spray tower (5), a blower (14), a sewage storage tank (17), a nitrification tank, a denitrification tank and an active carbon absorption tower (23); the sludge drier (1), the draught fan (2), the cyclone separator (3), the acid spray tower (4) and the alkaline spray tower (5) are sequentially connected in series; the acid spray tower (4) and the alkaline spray tower (5) are respectively communicated with a sewage storage pool (17); the alkaline spray tower (5) is communicated with the nitrification tank through a blower (14); the sewage storage tank (17), the denitrification tank, the nitrification tank and the activated carbon absorption tower (23) are connected in series in sequence.
2. The sludge drying tail gas treatment system of claim 1, wherein: the nitrification tank comprises a first-stage nitrification tank (181) and a second-stage nitrification tank (182), and the denitrification tank comprises a first-stage denitrification tank (191) and a second-stage denitrification tank (192); a reflux pump (20) is arranged between the nitrification tank and the denitrification tank.
3. The sludge drying tail gas treatment system according to claim 2, characterized in that: the top of the alkaline spray tower (5) is provided with a gas outlet which is communicated with aeration branch pipes (21) arranged at the bottoms of the primary nitrification tank (181) and the secondary nitrification tank (182) through a blower (14).
4. The sludge drying tail gas treatment system according to any one of claims 1 to 3, wherein: and the active carbon absorption tower (23) is provided with a discharge pipe (24) and a detection probe (25).
5. The sludge drying tail gas treatment system according to any one of claims 1 to 3, wherein: the treatment system also comprises a dosing pump (8) and a medicine storage box (9); the chemical oxidation medicament in the medicament storage box (9) is conveyed to the acid spray tower (4) and the alkaline spray tower (5) by the medicament feeding pump (8).
6. The sludge drying tail gas treatment system of claim 5, wherein: and the acid spray tower (4) and the alkaline spray tower (5) are provided with a pH sensor (10) and a foam sensor (12) which are interlocked with the PLC (13) and the dosing pump (8).
7. A sludge drying tail gas treatment method is characterized by comprising the following steps: comprises the following steps of (a) carrying out,
s1, drying the dewatered sludge cake after anaerobic digestion in a sludge drier, and feeding the generated sludge drying tail gas into a cyclone separator for tail gas dust removal;
s2, allowing the dedusted sludge drying tail gas to enter an acidic spray tower, and contacting and reacting with an acidic oxidizing agent for 2-10S;
s3, allowing the sludge drying tail gas after acidic oxidation to enter an alkaline spray tower, and allowing the sludge drying tail gas to contact and react with an alkaline oxidation agent for 2-10S;
s4, conveying the sludge drying tail gas subjected to alkaline oxidation in the step S3 and air to a nitrification tank according to a flow ratio of 0.1-1: 1, and performing biochemical degradation on the sludge drying tail gas;
s5, feeding the sludge drying tail gas after biochemical degradation into an active carbon tower, contacting with active carbon for adsorption for 2-10S, and discharging;
s6, the wastewater generated in the spray tower in the steps S3 and S4 enters a wastewater storage tank, is mixed with the wastewater generated by sludge dehydration and sludge drying, is conveyed to a nitrification and denitrification wastewater biochemical denitrification system, and is discharged after two-stage nitrification and denitrification treatment.
8. The sludge drying tail gas treatment method according to claim 7, characterized in that: in the step S1, the anaerobic digestion dehydrated mud cake is dried by adopting a direct contact heat drying mode, and the heat source for drying the dehydrated mud cake is generated by burning methane gas generated by an anaerobic digestion system.
9. The sludge drying tail gas treatment method according to claim 7, characterized in that: in the step S2, the acidic oxidizing agent is obtained by mixing sulfuric acid and hydrogen peroxide, wherein the mass fraction of the sulfuric acid in the acidic oxidizing agent is 10% -30%, the mass fraction of the hydrogen peroxide is 1% -5%, and the pH value in the acidic spray tower is 2-4; in the step S3, the alkaline oxidation agent is obtained by mixing sodium hydroxide and sodium hypochlorite, the mass fraction of the sodium hydroxide in the alkaline oxidation agent is 5% -10%, the mass fraction of the sodium hypochlorite is 1% -2%, and the pH value in the alkaline spray tower is 10-12.
10. The sludge drying tail gas treatment method according to claim 7, 8 or 9, characterized in that: in step S6, the method further includes: mixed wastewater discharged from the sewage storage tank firstly enters a denitrification tank and then enters a nitrification tank, mixed liquid in the nitrification tank flows back to the denitrification tank through a reflux pump, and the reflux ratio is controlled to be 100-400%; the DO value of the nitrification tank is 0.5 mg/L-2.5 mg/L, and the DO value of the denitrification tank is 0.1 mg/L-0.5 mg/L, MLSS, and the DO value is 5 g/L-20 g/L.
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