CN110776232A - Efficient sludge reduction coupling enhanced nitrogen and phosphorus removal device and method thereof - Google Patents
Efficient sludge reduction coupling enhanced nitrogen and phosphorus removal device and method thereof Download PDFInfo
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- CN110776232A CN110776232A CN201910909191.6A CN201910909191A CN110776232A CN 110776232 A CN110776232 A CN 110776232A CN 201910909191 A CN201910909191 A CN 201910909191A CN 110776232 A CN110776232 A CN 110776232A
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/06—Treatment of sludge; Devices therefor by oxidation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
- C02F11/122—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering using filter presses
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/023—Reactive oxygen species, singlet oxygen, OH radical
Abstract
The invention discloses a high-efficiency sludge decrement coupling enhanced nitrogen and phosphorus removal device and a method thereof. The decrement reaction tower is used for accommodating sewage, and the air source system comprises an air compressor, a rear cooler, an air storage tank, a drying mechanism and an air filter. The high-energy state oxygen generator is used for receiving the gas delivered by the air filter, and the excited state electronic system is used for carrying out electronic excitation on the gas in the high-energy state oxygen generator so as to generate high-energy state oxygen. And the powder feeding system is used for feeding a powder material into the decrement reaction tower, and the powder material consists of calcium carbonate powder, calcium hydroxide powder and calcium peroxide powder. The invention improves the biodegradability, the treated sludge supernatant can flow back, and the organic matters can be degraded, thereby reducing the sludge yield of the whole biochemical system and fundamentally realizing the aim of less sludge discharge or zero discharge.
Description
Technical Field
The invention relates to a nitrogen and phosphorus removal device in the technical field of sewage treatment, in particular to a high-efficiency sludge reduction coupling enhanced nitrogen and phosphorus removal device and a high-efficiency sludge reduction coupling enhanced nitrogen and phosphorus removal method.
Background
The sludge is organic matters, sediment substances such as microbial micelles and the like generated in the sewage treatment process of the sewage treatment plant, and floating foam and other residues floating on the sewage surface, wherein the sludge of the industrial sewage treatment plant contains a large amount of pathogenic bacteria, parasites, pathogenic microorganisms, dioxin, toxic heavy metals such as arsenic, copper, mercury, chromium and the like, and even toxic and harmful substances such as radioactive nuclide and the like which are difficult to degrade. The colloidal cell water property of the sludge causes high water content and large volume of the sludge, and brings difficulties to stacking, transportation and the like. If the sludge is randomly abandoned in mountain farmlands or is not subjected to standard landfill, huge potential threat is caused to the ecological environment.
The existing sewage treatment plant mainly removes the sludge from the sewage through the plate-and-frame desliming machine, but the water content of the sludge after being removed is still high and still 70% -85%, and meanwhile, the treatment mode can generate a large amount of residual sludge which also contains various harmful substances and organic matters, so that the treatment cost is high, and the harm to the environment is large. Therefore, it is necessary to perform a reduction treatment on the sludge, and the reduction treatment includes a high-temperature chemical reduction technology and a sludge chemical solidification, drying and incineration technology.
The high-temperature chemical decrement technology adopts a specific high-temperature and chemical method to degrade organic matters in the sludge, so that the organic matters are converted from a non-soluble polymer form into a water-soluble small molecule form, the existence conditions of gap water, surface water and combined water in the sludge are basically eliminated, the sludge and the water are easily separated, the residual small amount of sludge is easily dehydrated, and the reduction of the sludge volume is realized. However, the high investment and operation cost limit the wide application of the sludge in the industrial field, a large amount of energy is consumed in the high-temperature heat exchange process, the sludge needs to be subjected to dehydration treatment after treatment, and meanwhile, a large amount of byproducts are generated, so that the operation cost is increased.
The sludge medicament solidifying, drying and incinerating technology firstly converts sludge from a semi-solid state into a flowing state, then adds medicaments such as a precipitator, a stabilizer, a filter aid and the like, fixes toxic and harmful components such as heavy metal substances in the sludge, dries wet sludge into dry solid particles, simplifies the incineration treatment of the sludge in a hazardous waste center, immediately disperses the sludge by a large amount of moving high-temperature inert materials after the sludge is input into an incinerator by a feeding device and quickly mixes the sludge with hot sand grains, and can obtain better combustion efficiency. However, a large amount of primary energy is consumed in the using process, the investment and operation cost is high, the operation management is complex, and in the burning process, a strong carcinogen dioxin is generated, and a tail gas absorption device is required to be added.
Disclosure of Invention
Aiming at the prior technical problems, the invention provides a high-efficiency sludge reduction coupling enhanced nitrogen and phosphorus removal device and a method thereof, which solve the problems that the water content of the existing sludge after being removed is still very high, a large amount of residual sludge is generated, the sludge also contains various harmful substances and organic matters, the treatment cost is high, and the environmental harm is large.
The invention is realized by adopting the following technical scheme: a high-efficiency sludge decrement coupling enhanced nitrogen and phosphorus removal device comprises:
a decrement reaction tower for accommodating sewage;
the air source system comprises an air compressor, an after cooler, an air storage tank, a drying mechanism and an air filter; the air compressor is used for pressurizing the delivered air, and the after cooler is used for cooling the gas pressurized by the air compressor; the gas storage tank is used for storing the gas cooled by the after cooler and conveying the stored gas to the drying mechanism; the drying mechanism is used for removing moisture in the stored gas and conveying the gas after water removal to the air filter for dust removal and oil removal filtration;
a high energy state oxygen generator for receiving the gas delivered by the air filter;
an excited state electronic system for electronically exciting the gas in the high energy state oxygen generator to generate high energy state oxygen;
at least one aeration tray for aerating the high-energy oxygen-containing gas in the high-energy oxygen generator in the abatement reaction column; and
the powder feeding system is used for feeding powder materials into the decrement reaction tower; the powder material consists of calcium carbonate powder, calcium hydroxide powder and calcium peroxide powder.
As a further improvement of the scheme, the composition mass ratio of the calcium carbonate powder, the calcium hydroxide powder and the calcium peroxide powder is 3:5: 2.
As a further improvement of the above scheme, the nitrogen and phosphorus removal device further comprises:
a sludge tank for concentrating the sludge settled in the reduction reaction tower;
a wastewater adjusting tank for accommodating supernatant liquid returned from the sludge tank;
and the filter press is used for filter-pressing the concentrated sludge in the sludge tank to filter out a filter cake.
As a further improvement of the above scheme, the drying mechanism comprises a freeze dryer and an adsorption dryer; the freeze dryer is used for condensing and dewatering the stored gas, and the adsorption dryer is used for adsorbing and drying the gas dewatered by the freeze dryer.
As a further improvement of the above scheme, the nitrogen and phosphorus removal device further comprises:
the oxygen generator is used for absorbing the gas delivered by the air filter and correspondingly generating mixed gas with oxygen concentration reaching a preset oxygen concentration; wherein the excited state electron system electronically excites the mixed gas in the high energy state oxygen generator to generate the high energy state oxygen.
As a further improvement of the scheme, the nitrogen and phosphorus removal device is used for carrying out sludge reduction treatment on the sewage in the concentration tank; the nitrogen and phosphorus removal device also comprises:
and the diaphragm pump is used for pumping the sewage in the concentration tank into the decrement reaction tower.
As a further improvement of the above scheme, the powder adding system comprises a sludge agent adding tank, a pH adjusting tank and a flocculating agent adding tank which are all communicated with the decrement reaction tower; the sludge agent adding pool is used for adding calcium carbonate powder, calcium hydroxide powder and calcium peroxide powder into the reduction reaction tower to form a powder material; the pH adjusting tank is used for adjusting the pH value of the sewage in the reduction reaction tower, and the flocculating agent adding tank is used for adding a flocculating agent into the reduction reaction tower.
As a further improvement of the above scheme, the nitrogen and phosphorus removal device further comprises:
a tail gas treatment system for treating tail gas produced in the abatement reaction column.
As a further improvement of the above scheme, the nitrogen and phosphorus removal device further comprises:
a stirrer for stirring the sewage in the reduction reaction tower;
and the ultrasonic vibration equipment is used for carrying out ultrasonic vibration on the sewage in the decrement reaction tower.
The invention also provides a high-efficiency sludge reduction coupling enhanced nitrogen and phosphorus removal method which is applied to any high-efficiency sludge reduction coupling enhanced nitrogen and phosphorus removal device, and the nitrogen and phosphorus removal method comprises the following steps:
sequentially pressurizing, cooling, drying, dedusting, deoiling and filtering ambient air to remove moisture, dust, oil, hydrocarbon and hydrogen in the air to obtain excited gas;
electronically exciting the excited gas to generate high-energy-state oxygen;
feeding gas containing high-energy-state oxygen into sewage for aeration, and simultaneously putting powder materials into the sewage; the powder material consists of calcium carbonate powder, calcium hydroxide powder and calcium peroxide powder.
According to the efficient sludge reduction coupling enhanced nitrogen and phosphorus removal device and the method thereof, the air source system of the nitrogen and phosphorus removal device can pressurize, cool, dry, remove water and remove oil and dust from ambient air, so that impurities such as moisture, dust, oil, hydrocarbon and hydrogen in the air are removed, and if the impurities exist, the formation process of excited state electrons is adversely affected, so that smooth electron excitation can be ensured, and the electron excitation efficiency is improved.
The excited state electronic system of the invention excites gas electrons in the high-energy state oxygen generator to generate high-energy state oxygen, and the high-energy state oxygen and powder materials added by the powder adding system can generate a strong oxidation product-hydroxyl free radical without reaction selectivity under a special reaction environment. The newly generated strong oxidation hydroxyl free radical has extremely high oxidation potential, has oxidation capability stronger than most of oxidants, has very strong cell destruction capability, can generate catalytic oxidation reaction with sludge to degrade polysaccharide substances of microorganisms in the sludge, continuously oxidizes the microorganisms into carbon dioxide and water after wall breaking of the microorganism cells and release of organic matters, biological enzymes, RNA and the like in the cells, and promotes release of combined water in the sludge and water in the cells. Therefore, the water content of the treated sludge is reduced to be below 55 percent, the treated sludge is not re-dissolved, the solid content of the sludge is improved, the sludge and water are conveniently separated and dehydrated, the sludge reduction purpose is finally realized, the treatment cost can be reduced, and the harm to the environment is reduced.
Meanwhile, when the pH value of the added calcium ions in the powder material is more than 9.5, the calcium ions and phosphate radicals in the sludge supernatant undergo chemical combination reaction in the presence of hydroxyl free radicals to generate insoluble calcium hydroxy phosphate. In addition, the high molecular organic matters with the colloid bonding effect in the sludge can be thoroughly decomposed by an advanced oxidation method to be converted into water-soluble small molecular organic matters, the B/C ratio in the returned sludge supernatant can be effectively improved, the biodegradability is improved, the treated sludge supernatant can be returned, the degradable organic matters are released, the recessive growth effect is generated, the sludge yield of the whole biochemical system is reduced, and the aim of less sludge discharge or zero discharge of the sludge is fundamentally realized.
In addition, in the invention, the sludge becomes pure organic matters after wall breaking, the water content is low, the volume is reduced, the sludge discharge amount and the treatment capacity of the sludge are reduced, meanwhile, part of the sludge supernatant after wall breaking can flow back to the reduction reaction tower, and a large amount of substances which are subjected to wall breaking and oxidation dissolution are contained in the returned sludge supernatant, and the substances also provide a large amount of carbon sources which are easy to desorb for the whole device, so that the growth and the propagation of microorganisms are promoted, and the organic pollutants in water are treated more quickly and thoroughly, thereby more effectively realizing the sludge reduction of the whole wastewater treatment system.
Drawings
FIG. 1 is a system block diagram of an efficient sludge reduction coupling enhanced nitrogen and phosphorus removal apparatus in example 1 of the present invention;
FIG. 2 is a flow chart of AO + MBR + RO process corresponding to the high-efficiency sludge decrement coupling enhanced nitrogen and phosphorus removal device in FIG. 1;
FIG. 3 is a size diagram of the thickening tank of FIG. 2;
FIG. 4 is a size diagram of a sludge storage tank of the decrement reaction tower of the efficient sludge decrement coupling enhanced nitrogen and phosphorus removal device in FIG. 1;
FIG. 5 is a schematic diagram of the efficient sludge reduction coupling enhanced nitrogen and phosphorus removal apparatus in embodiment 2 of the present invention.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is described in further detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
Example 1
Referring to fig. 1 and fig. 2, this embodiment provides a high-efficiency sludge reduction coupling enhanced nitrogen and phosphorus removal device, which includes a reduction reaction tower, an air source system, a high-energy state oxygen generator, an excited state electronic system, an aeration tray, a powder adding system, and one or more components of an intelligent control system, an intelligent gas flow control system, a sludge tank, a wastewater adjusting tank, a filter press, a diaphragm pump, a tail gas treatment system, a stirrer (a sludge stirring and mixing system), an ultrasonic vibration device, a sludge conveying system, a control device, a sludge buffering and stabilizing tank, a sludge lifting pump, a sewage conveying water tank, a dried sludge conveying system, a dried sludge collection system, and a dried sludge conveying system. The embodiment is used for treating excess sludge generated by sewage treatment by adopting AO + MBR + RO processes. In the process, nitrifying liquid and MBR sludge inside an A/O tank flow back to the A tank, residual sludge is discharged to a sludge concentration tank, materialized sludge and biochemical sludge are discharged into the sludge concentration tank after advanced treatment (coagulating sedimentation), then concentration, membrane breaking, harmlessness, heavy metal passivation and filter pressing are sequentially carried out, the supernatant obtained by press filtration flows back to wastewater, and the sludge obtained by press filtration is subjected to low-temperature reduction drying and then is buried and recycled. The process generates a large amount of sludge, and the treatment cost is very high, so the nitrogen and phosphorus removal device of the embodiment can reduce the amount of the sludge.
In the embodiment, the nitrogen and phosphorus removal device is used for carrying out sludge reduction treatment on sewage in the existing concentration tank, and the concentration tank is communicated with the sludge collection tank. Wherein the amount of return sludge in the sludge collecting tank is assumed to be Q
1＝0.8×1.50463＝1.203704m
3/s＝4333.3m
3And h, the residual sludge amount is as follows:
Q
s＝524.76m
3/d＝21.865m
3/h
the total sludge amount is: q ═ Q
1+Q
s＝4333.3+21.865＝4355.165m
3/h
In this example, 5 (4 in 1) return sludge pumps and 2 (1 in 1) excess sludge pumps were used. The flow rate of each reflux pump is:
the effective volume of the mud collection pool of the pump room is calculated according to the water yield of 5 minutes of not less than the maximum pump (reflux pump), and then the effective water depth is set as h 2.0m, and the area of the mud collection pool is:
the size of the mud collecting pool is as follows: l × B is 8 × 6 m.
Referring to fig. 3, the concentration tank is a vertical flow concentration tank in an intermittent gravity concentration tank, and when activated sludge is concentrated, the concentration tank meets the following requirements:
1) the solid load of the sludge is preferably 30-60 kg/(m)
2·d)；
2) The concentration time is not shorter than 12 h;
3) when the water content of the sludge entering the sludge concentration tank from the secondary sedimentation tank behind the biological reaction tank is 99.2-99.6%, the water content of the concentrated sludge can be 97-98%;
4) the effective water depth is preferably 4 m.
When the concentration tank adopts a grid thickener, the linear speed of the outer edge of the thickener is generally preferably 1-2 m/min, and the slope of the tank bottom slope to the mud bucket is not preferably less than 0.05.
The concentration tank can be provided with a device for removing scum, gravity concentration is not required when the biological phosphorus removal process is adopted for sewage treatment, and design parameters are preferably determined according to experimental data or similar operation experience when mechanical concentration equipment is adopted for sludge concentration. In addition, the concentration tank can adopt an integrated machine for sludge concentration and dehydration, and facilities capable of discharging sludge water with different depths are arranged.
In this example, for the sake of convenience of explanation, it is assumed that the amount of excess sludge introduced into the thickening tank is 524.76m
3/d＝0.006m
3And/s, 2 concentration tanks are selected in the design, and the flow of a single tank is as follows: q
1＝0.003m
3And s. Assuming that the water content of the sludge before concentration is 99.3 percent and the water content of the sludge after concentration is P
197%. Wherein, the parameters in the concentration tank are as follows.
1. The area of the central mud inlet pipe is as follows:
the diameter of the central mud inlet pipe is as follows:
wherein A is the area of the sludge inlet pipe at the center of the concentration tank and the unit is m
2。v
0The flow speed of the mud inlet pipe for the center is generally less than 0.03m/s, d
0The diameter of the central mud inlet pipe is m. In this example, take v
00.03m/s, then
Further, it is possible to prevent the occurrence of,
get d
0400 mm. The actual flow rates inside the tubes were:
2. the gap height between the bell mouth of the central mud inlet pipe and the reflecting plate is as follows:
in the formula, h
3The height of a gap between a bell mouth of the central mud inlet pipe and the reflecting plate is m; v. of
1The sludge flows out from a gap between a bell mouth of the central sludge inlet pipe and the reflecting plate at a speed of 0.02-0.03 m/s; d
1For the diameter of the bell mouth, d is generally adopted
1＝1.35d
01.35 × 0.4-0.54 m. In this example, take v
10.025m/s, then
3. The amount of sewage separated after concentration is as follows:
4. the effective area of the concentration tank is as follows:
wherein F is the area of the water flow of the concentration tank and the unit is m
2(ii) a v is the ascending velocity of the sewage in the concentration tank, and is generally 0.00005-0.0001 m/s
5. The diameter of the concentration tank is as follows:
wherein the effective water depth is:
h
2＝vt
in the formula, h
2The effective water depth of the concentration tank is m; t is concentration time which is not less than 12 h. In this embodiment, when t is 12h, h is
2＝0.0001×12×3600＝4.32m。
6. The amount of the residual sludge after concentration is as follows:
7. sludge bucket volume of concentration tank
In this embodiment, the sludge hopper is arranged at the bottom of the concentration tank, and the sludge is discharged by gravity. Then there are:
h
5＝(r
2-r
1)·tanα
in the formula, h
6Is the height of the sludge bucket, and the unit is m; r is
2Is the radius of the concentration tank, and the unit is m; r is
1The radius of the bottom of the sludge bucket is generally 0.5m multiplied by 0.5m, α is the inclination angle of the sludge bucket, the inclination angle of the sludge bucket of the round tank is more than or equal to 55 degrees, in the embodiment, the inclination angle α of the sludge bucket is 60 degrees, and r is r
1＝0.30m，r
22.71m, then h
5＝(r
2-r
1) Tan α ═ (2.71-0.30) × tan60 ° -4.17 m, so the sludge hopper volume is:
8. the residence time of the sludge in the hopper is as follows:
wherein, the residence time is between 10 and 16, which meets the requirement.
9. The total height of the concentration tank is as follows:
H＝h
1+h
2+h
3+h
4+h
5
in the formula, h
1Is ultrahigh, unitIs m; h is
4Is the buffer layer height in m.
In this embodiment, take the super high h
10.3m, buffer layer height h
4When 0.4m, there are:
H＝h
1+h
2+h
3+h
4+h
5＝0.3+4.32+0.071+0.4+4.17＝9.161m
10. the overflow water of the concentration tank enters the water outlet groove through the overflow weir, and then flows into the water outlet pipe to be discharged. The flow q of the water outlet groove is 0.0023m
3And/s, the water flow rate is 0.31m/s when the water outlet tank width b is 0.15m and the water depth is 0.10 m.
Perimeter of the overflow weir: c ═ pi (D-2b) ═ 3.14 × (5.24-2 × 0.15) ═ 15.51m
The overflow weir adopts a 90-degree triangular water outlet weir on one side, the width of the weir is 0.16m, and the depth of the weir is 0.08 m. Therefore, each sedimentation tank has
The flow of each triangular weir is as follows:
the weir depth of the triangular weir is as follows:
and the water falls freely for 0.10m after the triangular weir, and the water head loss of the effluent weir is 0.10+ 0.01-0.11 m.
11. Sludge discharge pipe
The amount of the concentrated excess sludge is 0.0007m
3The mud amount is small, an intermittent mud discharging mode is adopted, and the volume of a mud hopper is 30.24m
3The sludge pipeline is a reinforced concrete pipe, the pipe diameter is DN200mm, the sludge discharge time is 0.5h each time, the sludge discharge is carried out 2 times every day, and the interval time is 12 h.
The sludge discharge amount each time:
flow velocity in the tube:
when the flow is not full, the flow rate is: v is 0.86m/s, slope: i is 6.8 per mill.
Referring to fig. 4, the decrement reaction tower is used to receive sewage, and the sewage in the concentration tank may be sucked by a sewage pump. The decrement reaction tower can adopt the existing sludge reaction tower, and provides a reaction place for the catalytic oxidation of the sludge. In this embodiment, the reduction reactor is provided with a sludge storage tank capable of storing sludge from the thickening tank. Q is 2Q
2＝0.0014m
3/s＝120.96m
3And d. Because the sludge amount is not large, the embodiment can adopt 1 sludge storage tank, and the sludge storage tank adopts a vertical flow sedimentation tank structure.
The volume of the mud storage pool is as follows:
in the formula, t is the mud storage time and is generally 8-12 h.
In this embodiment, when t is 8h, there are:
in addition, the design volume of the mud storage pool is as follows:
in the formula, V
Storage facilityThe volume is designed for the mud storage pool, and the unit is m
3(ii) a a is the side length of the sludge storage tank, and the unit is m; b is the length of the bottom side of the sludge hopper, and the unit is m; h is
6The effective water depth of the mud storage pool is m; h is
7The height of the sludge bucket is m, α is the inclination angle of the sludge bucket, and the inclination angle is 60 degrees generally.
In this embodiment, α is 60 °, a is 3.5m, and h is taken
62.5m, the bottom of the sludge hopper is square, the side length b is 1.0m, and then
2. The height of the mud storage pool is as follows:
H＝h
8+h
6+h
7
in the formula, h
8The mud storage pool is ultrahigh and has the unit of m.
In this embodiment, take h
80.3m, then
H＝0.3+2.5+2.17＝4.97m
The air source system comprises an air compressor, an aftercooler, an air storage tank, a drying mechanism and an air filter.
The air compressor is used for pressurizing the delivered air and can directly absorb the air outside the device. The air compressor feeds ambient air under pressure, typically in the form of a screw, and preferably of the oil-free type, such as the "mini" type, and must be rigorously oilless at the back stage. Wherein the maximum discharge pressure of the air compressor may be 0.7 MPa.
The aftercooler is used for cooling the gas pressurized by the air compressor. The after cooler cools compressed air containing saturated vapor with certain pressure discharged by an air compressor (namely the air compressor) through an external refrigerant, and discharges condensate to achieve a certain oil-water removing effect. The aftercooler is divided into a water-cooling type and an air-cooling type according to different refrigerants, and can be selected according to needs in practical application. The aftercooler is generally selected according to the displacement of the air compressor, and the rated processing capacity of the aftercooler is larger than the displacement of the air compressor.
The gas storage tank is used for storing the gas cooled by the rear cooler and conveying the stored gas to the drying mechanism. The air storage tank is a compressed air storage buffer device, belongs to a class of pressure containers, is generally selected according to the air displacement of the air compressor, generally requires volume to store 1-2 minutes of air because the excited state electronic excitation system has stable air consumption, and the design pressure of the air storage tank is higher than the highest exhaust pressure of the air compressor. The gas storage tank belongs to a class of pressure vessels, and accessories of the gas storage tank comprise a safety valve, a pressure gauge component, a blowdown/emptying valve and the like.
The drying mechanism is used for removing moisture in the stored air and conveying the dehydrated air to the air filter. In this embodiment, drying mechanism can include freeze dryer and adsorption drying machine, and freeze dryer is used for carrying out the condensation dewatering to the gas storage, and adsorption drying machine is used for carrying out adsorption drying to the gas after the freeze dryer dewatering.
The freeze dryer (i.e. the freeze dryer) is a device for cooling, condensing and dewatering compressed air under a saturated condition, and can remove about 80% of water in the compressed air under a normal working condition, so that the dewatering amount is large. And the low-temperature gas after water removal exchanges heat with the gas entering the equipment through the heat exchanger before being discharged from the equipment, so that the gas is precooled, and therefore, the energy consumption is low. Because the freezing point of water is 0 ℃, in order to prevent ice blockage, the setting temperature of an evaporator of an internal refrigeration system of the refrigeration dryer is above 0 ℃, so that the refrigeration dryer can only obtain a dew point of about minus 20 ℃ under normal pressure under rated pressure, and the shallow water removal is adopted. The processing gas quantity of the cold dryer generally takes the working pressure of 0.7MPa, the air inlet temperature of 42 ℃ and the ambient temperature of 38 ℃ as rated working conditions, and the modification should be carried out according to the modification coefficients under different working conditions during the model selection design. In addition, the higher the working pressure of the same cold dryer, the lower the air inlet temperature and the ambient temperature, and the better the air source treatment quality. Under the working conditions of low working pressure, high air inlet temperature and high working environment temperature, the setting personnel must correct the processing capacity of the refrigeration dryer. And when the model is selected, the actual handling capacity of the air dryer is generally slightly larger than the air displacement of the air compressor.
The adsorption type dryer is a dehumidification and purification device for adsorbing and drying compressed air by applying a pressure swing adsorption principle and a heatless regeneration or micro-heating regeneration method. The equipment adopts a double-tower structure, one tower absorbs moisture in air under certain pressure, the other tower uses a small part of dry air slightly higher than the atmospheric pressure to regenerate the drying agent in the absorption tower, and after a certain time, the two towers are switched to ensure the continuous supply of dry compressed air. Under normal operation conditions, the saturated air entering the dryer has enough contact time with the adsorbent bed at a certain flow rate, and the dew point (under pressure) of the treated air can be reduced to below-45 ℃ and can reach-70 ℃ at the lowest, which belongs to deep drying. The rated processing flow of the adsorption dryer, namely the rated inlet air flow, is the volume flow of air entering the dryer when the absolute pressure is 1atm, the temperature is 20 ℃, and the relative humidity is 0;
the working condition has great influence on the treatment effect of the adsorption dryer:
① the inlet air temperature is that the compressed air entering the dryer is generally in a saturated state, and under the same pressure and different temperatures, the moisture content is greatly different, the temperature is increased, the saturated moisture content is increased, and the load of the dryer is increased.
②, the moisture content and pressure of saturated compressed air are inversely proportional, when the working pressure is lower, the moisture content is higher, the required regeneration gas quantity is larger, and simultaneously, the air flow in the tower is accelerated due to the pressure reduction, thereby accelerating the abrasion of the adsorbent;
③ contamination of the oil mist the sorbent is very sensitive to contamination of the oil mist and when the oil mist contacts the sorbent, it covers its surface, which causes the sorbent to rapidly degrade, not only causing the dew point to rise, but also shortening the life of the sorbent.
④ A pre-filter is installed before the suction drier to remove liquid water, solid particles and oil mist possibly existing in the compressed air, so as to ensure the operation condition of the drier and the service life of the adsorbent.
⑤ when the adsorption dryer is classified into non-heat regeneration type and micro-heat regeneration type according to the regeneration mode, the latter uses a small part of heated dry air to regenerate the adsorbent, the average regeneration air flow rate (also called regeneration air consumption ratio) is reduced from about 15% to about 5%, and the magnitude of the regeneration air flow rate affects the air treatment effect under certain conditions.
The air filter is used for removing dust and oil from the gas after water removal. Air filters generally employ a classification method, including main pipe filtration, oil removal filtration, dust removal filtration, and the like. Air filters are typically installed according to the following rules: a main pipeline filter is arranged behind the air compressor, and the filtering aperture is 3-5 mu m; the adsorption dryer is provided with an oil removing filter in front, the filter aperture of the filter is at least 0.01 μm (preferably 0.01 μm plus 0.001 μm), and a 1 μm filter is generally arranged in front of the 0.01 μm filter; the adsorption dryer is followed by a dust removal filter with a filter pore size of at least 1 μm (preferably 1 μm plus 0.01 μm).
In this embodiment, the intelligent control system includes a pressure constant pressure system, a gas safety protection system and a gas flow control system, the pressure constant pressure system can stabilize the pressure of the gas filtered by the air filter, the gas safety protection system can ensure the safety of gas transportation, and the gas flow control system can detect the gas flow delivered to the high-energy state oxygen generator.
The high-energy state oxygen generator is used for receiving the gas delivered by the air filter. In this embodiment, the high-energy oxygen generator may have a high-energy oxygen yield of 240g/h and a flow rate of 10Nm
3H is used as the reference value. The excited state electronic system is used for carrying out electronic excitation on the gas in the high-energy state oxygen generator so as to generate high-energy state oxygen. The high-energy state oxygen generator may be a gaseous state electron generator and the excited state electronic system is a medium frequency high voltage power supply system capable of electronically exciting the gas in the high-energy state oxygen generator.
The number of the aeration discs is at least one, and the aeration discs are used for aerating the gas containing the high-energy oxygen in the high-energy oxygen generator in the decrement reaction tower. In this example, the number of aeration disks was 6, and the disk was of titanium metal structure, and the pore diameter of the pores was 0.02. mu.m. In this embodiment, the gas generated by the high-energy state oxygen generator can be delivered to the aeration disc through the gas flow intelligent control system, so that the gas flow entering the decrement reaction tower can be adjusted in real time, and the controllability of the reaction is ensured.
And the powder feeding system is used for feeding a powder material into the decrement reaction tower, and the powder material consists of calcium carbonate powder, calcium hydroxide powder and calcium peroxide powder. The composition mass ratio of the calcium carbonate powder, the calcium hydroxide powder and the calcium peroxide powder can be 3:5:2, of course, in other embodiments, the composition mass ratio of the three powders can be other ratios, and the specific numerical value can be set according to the type of the sludge. In this embodiment, the powder adding system includes a sludge agent adding tank, a pH adjusting tank, and a flocculant adding tank, all of which are communicated with the decrement reaction tower. The sludge agent feeding pool is used for feeding calcium carbonate powder, calcium hydroxide powder and calcium peroxide powder into the decrement reaction tower to form a powder material. The pH adjusting tank is used for adjusting the pH value of the sewage in the reduction reaction tower, and the flocculating agent adding tank is used for adding the flocculating agent into the reduction reaction tower.
In some embodiments, the flocculant may also be dosed via a dissolving tank having a volume of:
in the formula, V
1Volume of the dissolving tank in m
3N is the number of times of dispensing each day, N is the number of medicine dissolving tanks, and b is the concentration of the medicine, and is generally 1-2%. In this embodiment, if N is 1, N is 2, and b is 1%, the number of the N-b-N is 1%, the number of the N-b-N is equal to the number of the N-N
Moreover, the medicine dissolving tank can adopt JYB type glass fiber reinforced plastic medicine dissolving tank, the external dimension phi is 2000 multiplied by 1500, and the effective volume is 3.768m
3。
And the volume of the dissolving tank: v
2＝(0.2～0.3)V
1
In this example, 2 dissolving tanks are taken, and then
V
2＝0.25V
1＝0.25×3.63＝0.92m
3
The net size is then: phi 1100 x 1300.
The hydrolysis time is longer due to the difficulty of polyacrylamide solvent, and the hydrolysis time of the polyacrylamide in the embodiment is calculated as 24 h.
The sludge impoundment is arranged in the mud that subsides in the concentration decrement reaction tower, and the waste water equalizing basin is arranged in holding the supernatant of mud pond mesopelma, and the pressure filter is arranged in the mud of the concentrated play in the pressure filtration mud pond to filter out the filter cake. The filter press may employ one of a plate and frame filter press, a belt filter press, a vacuum drum filter press, and a centrifugal dehydrator, and in this embodiment, the filter press employs a plate and frame filter press. The diaphragm pump is used for pumping the sewage in the concentration tank into the decrement reaction tower.
The sludge amount after the filter press dehydration is as follows:
in the formula, P
2The water content of the dewatered sludge is shown.
In this embodiment, P
2＝75％
The weight of the dewatered dry sludge is as follows:
M＝q(1-P
2)×1000＝72.576×(1-75％)×1000＝18144kg/d＝756kg/h
the tail gas treatment system is used for treating tail gas generated in the decrement reaction tower. Odor is generated in the sludge dewatering process, and the tail gas treatment system can purify the air by adopting the mode of wood chips and a biological carbon filter bed. Of course, in this embodiment, the exhaust gas treatment system may include a gas collecting hood installed at an upper portion of each belt filter press and three sets of air cleaners, and the odor is supplied to the air cleaners by the ventilator.
The stirrer is used for stirring the sewage in the decrement reaction tower. Wherein, the required power of the stirrer is calculated according to the input power of 20W per cubic meter of the tank volume:
N＝20V
2＝20×0.93＝0.0186kW
total efficiency η of blender
1With 0.75, agitator drive efficiency η
2When 0.8 is adopted, the power of the motor required by the stirring shaft is
The ultrasonic vibration equipment is used for carrying out ultrasonic vibration on the sewage in the decrement reaction tower. The ultrasonic vibration equipment can adopt an ultrasonic generator, and a vibration rod is arranged in the sludge of the decrement reaction tower to vibrate the sludge and the powder material, so that the powder material is fully contacted with the sludge, and the powder material is uniformly mixed in the sludge.
In the embodiment, the control device can control the operation of each structure, and the automatic operation of the decrement device is realized. The sludge conveying system can convey sludge away, the sludge buffering and stabilizing tank can collect sludge, the sludge lifting pump can convey sludge to the filter press from the sludge buffering and stabilizing tank to perform filter pressing, the filtered sludge is collected in the sewage conveying water tank and further conveyed to the dried sludge collecting system through the dried sludge conveying system, and finally the dried sludge is conveyed out through the dried sludge conveying system.
In summary, the efficient sludge reduction coupling enhanced nitrogen and phosphorus removal device of the embodiment has the following advantages:
the excited state electronic system of the embodiment excites gas electrons in the high-energy state oxygen generator to generate high-energy state oxygen, and the high-energy state oxygen and powder materials added by the powder adding system can generate a strong oxidation product, namely hydroxyl free radicals without reaction selectivity in a special reaction environment. The newly generated strong oxidation hydroxyl free radical has extremely high oxidation potential, has oxidation capability stronger than most of oxidants, has very strong cell destruction capability, can generate catalytic oxidation reaction with sludge to degrade polysaccharide substances of microorganisms in the sludge, continuously oxidizes the microorganisms into carbon dioxide and water after wall breaking of the microorganism cells and release of organic matters, biological enzymes, RNA and the like in the cells, and promotes release of combined water in the sludge and water in the cells. Therefore, the water content of the treated sludge is reduced to be below 55 percent, the treated sludge is not re-dissolved, the solid content of the sludge is improved, the sludge and water are conveniently separated and dehydrated, the sludge reduction purpose is finally realized, the treatment cost can be reduced, and the harm to the environment is reduced.
Meanwhile, when the pH value of the added calcium ions in the powder material is more than 9.5, the calcium ions and phosphate radicals in the sludge supernatant undergo chemical combination reaction in the presence of hydroxyl free radicals to generate insoluble calcium hydroxy phosphate. In addition, the high molecular organic matters with the colloid bonding effect in the sludge can be thoroughly decomposed by an advanced oxidation method to be converted into water-soluble small molecular organic matters, the B/C ratio in the returned sludge supernatant can be effectively improved, the biodegradability is improved, the treated sludge supernatant can be returned, the degradable organic matters are released, the recessive growth effect is generated, the sludge yield of the whole biochemical system is reduced, and the aim of less sludge discharge or zero discharge of the sludge is fundamentally realized.
Moreover, in this embodiment, because become simple organic matter after the mud broken wall, the moisture content is low, the volume reduces, reduce mud play mud volume and handling capacity, the mud supernatant after the broken wall partly can flow back to in the decrement reaction tower simultaneously, the material that is broken the wall in a large number of quilt that contains in the supernatant of the mud of backward flow, the oxidation dissolves, these materials provide the carbon source of a large amount of easy desorption receipts again for whole device, promote the microorganism to grow and breed, organic pollutant in faster, more thorough processing water, thereby the mud decrement of whole waste water treatment system has been realized more effectively.
Example 2
Referring to fig. 5, the embodiment provides a high-efficiency sludge reduction coupling enhanced nitrogen and phosphorus removal device, which is added with an oxygen generator based on embodiment 1. The oxygen generator is used for absorbing the gas delivered by the air filter and correspondingly generating mixed gas with oxygen concentration reaching a preset oxygen concentration. Wherein the excited state electronic system performs electronic excitation on the mixed gas in the high-energy state oxygen generator to generate high-energy state oxygen. Therefore, the oxygen generator can remove a part of non-oxygen gas, so that the oxygen content in the mixed gas is greatly increased, the oxygen content in the unit volume of the excited gas is greatly increased, the content of high-energy-state oxygen is further increased, and the sludge reduction effect is improved.
Example 3
The embodiment provides a high-efficiency sludge reduction coupling enhanced nitrogen and phosphorus removal method, which is applied to the high-efficiency sludge reduction coupling enhanced nitrogen and phosphorus removal device in the embodiment 1 or the embodiment 2, and the nitrogen and phosphorus removal method comprises the following steps:
1. sequentially pressurizing, cooling, drying, dedusting, deoiling and filtering ambient air to remove moisture, dust, oil, hydrocarbon and hydrogen in the air to obtain excited gas;
2. electronically exciting the excited gas to generate high-energy-state oxygen;
3. feeding gas containing high-energy-state oxygen into sewage for aeration, and simultaneously putting powder materials into the sewage; the powder material consists of calcium carbonate powder, calcium hydroxide powder and calcium peroxide powder.
Example 4
The embodiment provides an MDP material for high-efficiency sludge reduction coupling enhanced nitrogen and phosphorus removal, which is the powder material in embodiment 1 or embodiment 2. The MDP material comprises calcium carbonate powder, calcium hydroxide powder and calcium peroxide powder. Wherein the mass ratio of the calcium carbonate powder, the calcium hydroxide powder and the calcium peroxide powder is 3:5:2, and the MDP material and the high-energy-state oxygen obtained by electronic excitation are matched in the sludge for use.
In this example, the MDP material was mixed in the sludge such that the pH of the mixed sludge supernatant was greater than 9.5. According to this criterion, a certain amount of MDP material can be selected for dosing, depending on the total amount of sludge. The MDP material of the present embodiment is used in combination with an excited gas containing high-energy oxygen. The dew point of the excited gas from the gas source is lower than minus 45 ℃, and the oil content is lower than 0.01mg/m
3The particle size of the impurities is less than 1 μm, the temperature is lower than 25 ℃, and the air pressure is greater than 0.1 MPa. It should be noted that the mass ratio of the calcium carbonate powder, the calcium hydroxide powder and the calcium peroxide powder can be other ratios, and the ratio can be determined according to the actual conditionsThe kind of the sludge of (2) is set.
Example 5
The embodiment provides a preparation method of a sludge reduction coupling enhanced nitrogen and phosphorus removal material, which is used for preparing the nitrogen and phosphorus removal material. Wherein, the nitrogen and phosphorus removal material comprises the MDP material in the embodiment 4. The preparation method of this example includes the following steps:
sequentially pressurizing, cooling, drying, dedusting and deoiling and filtering external air to obtain an air source with dew point lower than-45 ℃ and oil content lower than 0.01mg/m
3The particle size of the impurities is less than 1 μm, the temperature is lower than 25 ℃, and the air pressure is greater than 0.1 MPa; in this example, the source dew point of the energized gas is below-55 degrees Celsius and the oil content at 21 degrees Celsius is below 0.003/m
3The particle size of the impurities is less than 0.01 mu m;
electronically exciting the excited gas to generate an excited-state gas containing high-energy-state oxygen;
mixing calcium carbonate powder, calcium hydroxide powder and calcium peroxide powder according to the mass ratio of 3:5:2 to produce an MDP material;
adding the MDP material into the sludge, and aerating the excited gas in the sludge to enable the MDP material to react with high-energy oxygen to generate a nitrogen and phosphorus removal material; wherein the MDP material is mixed in the sludge, so that the pH value of the mixed sludge supernatant is more than 9.5;
after the MDP material is added and the excited gas is aerated, a polyacrylamide flocculant is added into the sludge to generate a nitrogen and phosphorus removal material; wherein the dosage of the polyacrylamide flocculant is 0.15 to 0.5 percent of the weight of the dry sludge in the sludge. In addition, the polyacrylamide flocculant can be added into the sludge through at least one drug dissolving tank. Wherein, the volume of dissolving the medicinal cupping is:
in the formula, W is the adding amount of the polyacrylamide flocculant, N is the dosage frequency per day, N is the number of the medicine dissolving tanks, and c is the concentration of the medicine.
In the steps, when the MDP is added into the sludge, the sludge is stirred and ultrasonically vibrated so as to fully mix and contact the sludge and the MDP material.
In some embodiments, the preparation method can be additionally provided with the following steps:
separating the excited gas by an oxygen generator to obtain a mixed gas with the oxygen concentration reaching a preset oxygen concentration; wherein the mixed gas is excited by electrons to generate an excited gas. Therefore, the oxygen generator can remove a part of non-oxygen gas, so that the oxygen content in the mixed gas is greatly increased, the oxygen content in the unit volume of the excited gas is greatly increased, the content of high-energy-state oxygen is further increased, and the sludge reduction effect is improved.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents and improvements made within the spirit and principle of the present invention are intended to be included within the scope of the present invention.
Claims (10)
1. The utility model provides a high-efficient mud decrement coupling nitrogen and phosphorus removal device that reinforces which characterized in that, it includes:
a decrement reaction tower for accommodating sewage;
the air source system comprises an air compressor, an after cooler, an air storage tank, a drying mechanism and an air filter; the air compressor is used for pressurizing the delivered air, and the after cooler is used for cooling the gas pressurized by the air compressor; the gas storage tank is used for storing the gas cooled by the after cooler and conveying the stored gas to the drying mechanism; the drying mechanism is used for removing moisture in the stored gas and conveying the gas after water removal to the air filter for dust removal and oil removal filtration;
a high energy state oxygen generator for receiving the gas delivered by the air filter;
an excited state electronic system for electronically exciting the gas in the high energy state oxygen generator to generate high energy state oxygen;
at least one aeration tray for aerating the high-energy oxygen-containing gas in the high-energy oxygen generator in the abatement reaction column; and
the powder feeding system is used for feeding powder materials into the decrement reaction tower; the powder material consists of calcium carbonate powder, calcium hydroxide powder and calcium peroxide powder.
2. The efficient sludge decrement coupling enhanced nitrogen and phosphorus removal device as claimed in claim 1, wherein the composition mass ratio of the calcium carbonate powder, the calcium hydroxide powder and the calcium peroxide powder is 3:5: 2.
3. The efficient sludge decrement coupling enhanced nitrogen and phosphorus removal device as claimed in claim 1, wherein the nitrogen and phosphorus removal device further comprises:
a sludge tank for concentrating the sludge settled in the reduction reaction tower;
a wastewater adjusting tank for accommodating supernatant liquid returned from the sludge tank;
and the filter press is used for filter-pressing the concentrated sludge in the sludge tank to filter out a filter cake.
4. The efficient sludge decrement coupling enhanced nitrogen and phosphorus removal device as claimed in claim 1, wherein the drying mechanism comprises a freeze dryer and an adsorption dryer; the freeze dryer is used for condensing and dewatering the stored gas, and the adsorption dryer is used for adsorbing and drying the gas dewatered by the freeze dryer.
5. The efficient sludge decrement coupling enhanced nitrogen and phosphorus removal device as claimed in claim 1, wherein the nitrogen and phosphorus removal device further comprises:
the oxygen generator is used for absorbing the gas delivered by the air filter and correspondingly generating mixed gas with oxygen concentration reaching a preset oxygen concentration; wherein the excited state electron system electronically excites the mixed gas in the high energy state oxygen generator to generate the high energy state oxygen.
6. The high-efficiency sludge decrement coupling enhanced nitrogen and phosphorus removal device as claimed in claim 1, wherein the nitrogen and phosphorus removal device is used for sludge decrement treatment of sewage in the concentration tank; the nitrogen and phosphorus removal device also comprises:
and the diaphragm pump is used for pumping the sewage in the concentration tank into the decrement reaction tower.
7. The efficient sludge decrement-coupling enhanced nitrogen and phosphorus removal device as claimed in claim 1, wherein the powder adding system comprises a sludge agent adding tank, a pH adjusting tank and a flocculating agent adding tank which are all communicated with the decrement reaction tower; the sludge agent adding pool is used for adding calcium carbonate powder, calcium hydroxide powder and calcium peroxide powder into the reduction reaction tower to form a powder material; the pH adjusting tank is used for adjusting the pH value of the sewage in the reduction reaction tower, and the flocculating agent adding tank is used for adding a flocculating agent into the reduction reaction tower.
8. The efficient sludge decrement coupling enhanced nitrogen and phosphorus removal device as claimed in claim 1, wherein the nitrogen and phosphorus removal device further comprises:
a tail gas treatment system for treating tail gas produced in the abatement reaction column.
9. The efficient sludge decrement coupling enhanced nitrogen and phosphorus removal device as claimed in claim 1, wherein the nitrogen and phosphorus removal device further comprises:
a stirrer for stirring the sewage in the reduction reaction tower;
and the ultrasonic vibration equipment is used for carrying out ultrasonic vibration on the sewage in the decrement reaction tower.
10. The high-efficiency sludge reduction coupling enhanced nitrogen and phosphorus removal method is applied to the high-efficiency sludge reduction coupling enhanced nitrogen and phosphorus removal device as claimed in any one of claims 1 to 9, and is characterized by comprising the following steps:
sequentially pressurizing, cooling, drying, dedusting, deoiling and filtering ambient air to remove moisture, dust, oil, hydrocarbon and hydrogen in the air to obtain excited gas;
electronically exciting the excited gas to generate high-energy-state oxygen;
feeding gas containing high-energy-state oxygen into sewage for aeration, and simultaneously putting powder materials into the sewage;
the powder material consists of calcium carbonate powder, calcium hydroxide powder and calcium peroxide powder.
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