CN219031892U - Sulfur autotrophic denitrification moving bed - Google Patents
Sulfur autotrophic denitrification moving bed Download PDFInfo
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- CN219031892U CN219031892U CN202222334113.8U CN202222334113U CN219031892U CN 219031892 U CN219031892 U CN 219031892U CN 202222334113 U CN202222334113 U CN 202222334113U CN 219031892 U CN219031892 U CN 219031892U
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Abstract
The utility model provides a sulfur autotrophic denitrification moving bed, which comprises a reactor water inlet end (2), a water inlet screen plate (4), a filler layer area (5), a spiral conveying rod piece (6) and a reactor water outlet end (7), wherein the bottom of the reactor moving bed is funnel-shaped; the spiral conveying rod piece (6) is positioned in the packing layer area, and the packing slowly moves from bottom to top in the rotating process of the spiral conveying rod piece by arranging the spiral conveying rod piece, and when the packing moves to the uppermost part of the threads, the packing falls back from a gap between the screw and the inner wall of the reactor. During this period, the filler particles are in mutual frictionThe nitrogen is continuously discharged in the friction process of the fillers, the fillers are not sticky and hardened, the thickness of the biological film can be effectively controlled, so that the main functional bacterial groups are directionally enriched, the mass transfer efficiency of the matrix and the actual contact residence time of sewage are effectively improved, the sewage treatment effect is improved, and the accumulation of nitrite and the greenhouse gas N are reduced 2 O is discharged. In addition, with the improvement of the denitrification efficiency, the filling material consumption, the occupied area and the ton water investment cost of the reaction tank body are correspondingly reduced.
Description
Technical Field
The utility model relates to the technical field of sewage deep denitrification, in particular to a sulfur autotrophic denitrification filling type bed filter denitrification method.
Background
In recent years, with the development of economy and the importance of water resource protection in China, the water treatment standards of the regulatory authorities and various industries are gradually improved, and the requirements on the quality of water supply and the discharge of wastewater are mainly met, so that the investment and the requirements on a water treatment system are greatly increased. Meanwhile, the discharge of various waste water and domestic sewage is continuously increased, and the water area environment is seriously polluted, so that the nutrient elements in the water areas such as rivers, lakes and the like are excessive, and the water areas tend to be eutrophicated. The eutrophication of the water body can cause algae malignant explosion events such as water bloom, red tide and the like, so that a series of problems such as water hypoxia, turbidity increase, malodor emission, algae toxin level improvement and the like are caused, and the water environment quality and the water ecological safety are seriously influenced. Wherein, the nitrogen pollutant is not only a key evaluation index of the nutrition level of the water body, but also a key cause of the water bloom explosion. Therefore, deep reduction of total nitrogen from the source is an important way for controlling eutrophication of urban water and guaranteeing safety of ecological water.
Along with the development of the water pollution control action plan, clear and time-limited requirements are provided for the water environment improvement and sewage treatment targets in China, and the urgency of deep removal of sewage nitrogen pollutants is highlighted.
The traditional denitrification filter adopts carriers such as quartz sand, ceramsite and the like as a film-forming medium of denitrification organisms, utilizes a proper amount of carbon source to carry out denitrification reaction, and simultaneously utilizes the interception effect of the filter medium to remove suspended matters and falling biological films in intercepted sewage. The working principle of the traditional denitrification filter is that the denitrification bacteria convert nitrate into nitrogen under the anoxic environment, and the reaction takes an organic carbon source as an electron donor. To obtain higher denitrification efficiency, the traditional method is to supplement carbon sources, but the cost of the agent is increased, which is disadvantageous to the operation of a sewage treatment plant in the long term.
The sulfur autotrophic denitrification is mainly a process of reducing nitrate into nitrogen by taking a sulfur extremely relevant reduced compound as an electron donor by sulfur autotrophic denitrification bacteria. Sulfur autotrophic denitrification is of great concern because it does not require an additional carbon source. The reaction does not need an external carbon source, has high denitrification efficiency, and is an important technology for low-carbon source wastewater denitrification. In the reaction process, sulfur particles are generally used as a filler to provide a sulfur source required by the reaction, and limestone is added to balance acid generated by the sulfur simple substance type autotrophic denitrification reaction. However, the addition of limestone in the traditional filler can cause the increase of the hardness of the effluent, and the consumption of alkali is larger, so that the waste of sulfur and limestone is caused; in recent years, the advent of some sulfur-based composite fillers, such as sulfur-iron composite fillers, well overcomes the problem of alkalinity consumption in the independent sulfur autotrophic denitrification process and the problem of alkalinity generation in the independent iron autotrophic denitrification process, and gradually realizes the engineering application of the sulfur autotrophic denitrification technology.
At present, the process reactor mainly adopts a fixed bed mode, in the fixed bed reactor, a solid particle material layer is always in a static state, and with continuous operation of the reactor, nitrogen is continuously generated to occupy gaps among fillers, so that the actual gaps of the reactor are reduced, the hydraulic retention time is shortened, the mass transfer efficiency of the reactor is reduced, and the reactor cannot be stably and efficiently operated. And the surface of the filler is continuously accumulated with sediment substances, the biological film is excessively thick and agglomerated, the proportion of live bacteria and dead bacteria is unbalanced, and the dead bacteria are increased, so that gaps among the fillers are gradually reduced, and the agglomeration is formed to cause blockage.
The prior method for solving the problems of the sulfur autotrophic denitrification fixed bed reaction system mainly comprises back flushing:
(1) Patent 202021404064.5 discloses a sulfur-iron composite double-layer filter material denitrification filter, which comprises a sulfur autotrophic denitrification layer, an intermediate water layer, an iron autotrophic denitrification layer and a pebble supporting layer which are sequentially distributed from top to bottom. The filter combines the sulfur autotrophic denitrification process and the iron autotrophic denitrification process, balances the alkalinity of the effluent water, and solves the problem of blockage of the filler after long-term use by respectively installing backwash pipes below the sulfur filler layer and the iron filler layer. The construction cost required by the method is overlarge, and the maintenance and operation of the backwash pipe are complex.
(2) Patent CN202110452114.X describes a percolating bed reaction device for denitrification of sulfur autotrophic organisms, a back flushing system is connected to the bottom end of a reaction tank, a packing layer is connected to the inside of the reaction tank, the problem of easy blockage after the packing is taken off the membrane is solved, and the back flushing process without stopping is realized. The method needs regular back flushing, but needs to additionally add a back flushing prompt device to remind workers of back flushing maintenance, thereby increasing construction cost and management cost.
(3) The literature (Wang Y, bott C, nerenberg R.Sulfur-based denitrification: effect of biofilm development on denitrification flows.Water Research,2016,100 (sep.1): 184-193.) describes an upflow reactor with sulphur flakes as support, experimental results show that as the biofilm continues to thicken, the mass transfer efficiency of the system decreases continuously, wherein the second reactor device appears to be evident, and after it has been run to 50d, the denitrification load begins to decrease.
In the practical filter maintenance application, the back flushing is often divided into three modes of air flushing, water flushing and air-water combined flushing. The strength of the common water washing is smaller, and the common water washing is generally used for removing nitrogen in a filler layer and mainly takes the effect of nitrogen removal; the impact of air washing on the filler is large, so that hardening can be effectively removed. Backwash is the main way to solve the hardening and nitrogen accumulation of deep bed filters at present, but there are also some negative effects on the packing: (1) The denitrification process is an anaerobic process, and the air washing can introduce a large amount of oxygen to destroy the existing anaerobic environment of the filter layer. (2) Due to the existence of the back flushing process, the operation mode and the structure of the filter tank can be changed, and the water yield of the filter tank is reduced. (3) The water flow and air bubbles generated by air washing and water washing can be preferentially communicated with the gaps with smaller resistance in the filtering material layer, and the gaps with smaller impact resistance can not be fully broken up, so that the back flushing of the deep bed filter tank can not be thorough.
Disclosure of Invention
Based on the technical background, the inventor makes a keen approach, and found that: by installing the spiral conveying rod piece in the filler layer of the sulfur autotrophic denitrification moving bed, the filler slowly moves from bottom to top under the rotation of the spiral conveying rod piece, when the filler moves to the effective end of the spiral conveying rod piece, the filler clings to the inner wall of the reactor around to fall back to form circulation, so that the accumulation of nitrogen bubbles generated by denitrification in the filler layer is effectively reduced, the thickness of a biological film in the filler layer is also reduced under the mutual friction among filler particles, the filler is prevented from hardening without backwashing, the substrate mass transfer efficiency and the actual contact residence time of sewage are improved, and the sewage treatment effect, the treatment efficiency and the nitrate nitrogen removal load are improved. Meanwhile, after negative effects caused by hardening of the filler are eliminated, along with friction among filler particles, the thickness of the biomembrane on the surface of the filler is effectively controlled, the update of the biomembrane is promoted by the reduction of the biomembrane, the proportion of effective living bacteria is improved, and the sulfur autotrophic denitrifying bacteria are more helped to become dominant bacteria. Simultaneously, nitrogen is continuously discharged in the friction process of the filler, so that the mass transfer efficiency of a matrix and the actual contact residence time of sewage are effectively improved, the sewage treatment effect is improved, and the accumulation of nitrite and the accumulation of greenhouse gas N are reduced 2 O is discharged. In addition, with the improvement of denitrification efficiency, the initial filling material consumption of the tank body volume is effectively reduced, the operation management cost is greatly reduced, and the method has good application prospect in the aspect of sewage treatment, thereby completing the utility model.
The first aspect of the utility model is to provide a sulfur autotrophic denitrification moving bed, which comprises a reactor water inlet end 2, a uniform water distribution pore plate 4, a bearing layer area 5, a packing layer area 6, a spiral conveying rod piece 7 and a reactor water outlet end 9;
the spiral conveying rod piece 7 is vertically arranged in the middle of the packing layer area 6 and comprises a straight rod and a spiral part, the spiral part is spiral, the straight rod is positioned in the middle of the spiral part, and the head end and the tail end of the spiral part are fixed on the straight rod.
Drawings
FIG. 1 shows a schematic view of a sulfur autotrophic denitrification moving bed according to a preferred embodiment of the present utility model;
FIG. 2 shows a schematic structural view of a pulsating bed reactor according to a preferred embodiment of the present utility model;
figure 3 shows a top view of a pulsed bed reactor according to a preferred embodiment of the present utility model.
Description of the reference numerals
1-a peristaltic pump for water inflow;
2-a water inlet end of the reactor;
3-a digital display pressure gauge;
4-a water inlet sieve plate;
5-a filler layer region;
6-spiral conveying rod pieces;
7-a reactor water outlet end;
8-a motor;
9-rotating speed modulator.
12-a water inlet end;
14-a water distribution plate;
15-a supporting layer;
16-a filler layer;
17-screw rod piece;
18-automatic guide rail;
19-water outlet pipe.
Detailed Description
The features and advantages of the present utility model will become more apparent and evident from the following detailed description of the utility model.
According to the utility model, a first aspect is to provide a sulfur autotrophic denitrification moving bed, which comprises a reactor water inlet end 2, a water inlet screen plate 4, a filler layer area 5, a spiral conveying rod piece 6 and a reactor water outlet end 7, wherein the water inlet screen plate 4 is positioned at the middle position of the bottom of the denitrification moving bed, the bottom of the denitrification moving bed is inclined downwards around the water inlet screen plate 4, and the whole denitrification moving bed is in a funnel shape, as shown in fig. 1, so that when the spiral conveying rod piece 6 rotates in the moving bed, filler positioned at the bottom of the moving bed flows, and the filler is prevented from hardening.
The included angle between the bottom of the denitrification moving bed and the side surface thereof is an obtuse angle, preferably the included angle is 95-150 degrees, more preferably 95-120 degrees.
In the traditional sulfur autotrophic denitrification fixed bed, along with the progress of denitrification, generated nitrogen can accumulate in gaps of a filler layer, organisms can continuously grow on the surface of the filler after film formation is successful, when the accumulation of the biological film is too thick, the diffusion of a matrix to the surface of the filler can be influenced, and meanwhile, the continuously grown biological films can be mutually connected to form hardening. The mass transfer of sewage and organisms is affected due to the hardening of the filler, so that the denitrification efficiency of the reactor is reduced. At the same time, as the biofilm thickens, the hardening accumulates in large amounts, and part of the bacteria are dead continuously due to the difficulty in contacting the surface of the sulfur-based filler, which also results in an increased proportion of dead bacteria in the biofilm.
The sulfur autotrophic denitrification moving bed is provided with the spiral conveying rod piece 6, the spiral conveying rod piece is spiral, is a mechanical device for pushing materials to convey, and is driven by a motor to rotate in a spiral mode, slow friction movement among fillers is realized, so that the fillers slowly flow, hardening of the fillers can be avoided, meanwhile, the thickness of biological films can be effectively controlled, the main functional flora is directionally enriched, nitrogen is continuously discharged in the friction process of the fillers, the mass transfer efficiency of a matrix and the actual contact residence time of sewage are effectively improved, and accumulation of nitrite and greenhouse gas N are reduced 2 O is discharged, so that the reaction system has higher denitrification load, and in addition, the spiral conveying rod piece has the advantages of simple structure, small cross-sectional area, good sealing performance, convenient operation and the like.
The reactor water inlet end 2 is positioned at the lowest end of the denitrification moving bed and is connected with the water inlet peristaltic pump 1, waste water to be treated is conveyed into the denitrification moving bed from the reactor water inlet end 2, the spiral conveying rod piece 6 is in a spiral shape and is vertically arranged at the middle position of the packing layer area 5, the reactor water outlet end 7 is positioned above the packing layer area 5, and the water inlet sieve plate 4 is positioned between the packing layer area 5 and the reactor water inlet end 2 to prevent packing from falling.
The vertical distance between the reactor water outlet end 7 and the packing layer region 5 is 5 to 300cm, preferably 7 to 200cm, more preferably 10 to 200cm.
The sulfur autotrophic denitrification moving bed adopts an upflow mode, and wastewater to be treated after operation flows into the moving bed from the water inlet end 2 of the reactor through the water inlet peristaltic pump 1, then flows into the filler layer area 5, and finally flows out from the water outlet end 7 of the reactor.
The upper end of the spiral conveying rod piece 6 is connected with a motor 8, the other end of the motor 8 is connected with a rotating speed modulator 9, the motor 8 drives the spiral conveying rod piece 6 to rotate, the filler slowly moves from bottom to top, when the filler moves to the effective end of the spiral conveying rod piece, the filler falls back to the periphery of the inner wall of the reactor to form circulation, accumulated nitrogen bubbles generated by denitrification are discharged from the water outlet end 7 of the reactor upwards along with the movement of the filler to the effective end of the spiral conveying rod piece, the excessively thick biological film on the filler is also discharged from the water outlet end 7 of the reactor after falling off and floating under the mutual friction among the filler particles, the biological film thickness is reduced, and the rotating speed modulator 9 is used for adjusting the rotating speed of the spiral conveying rod piece 6.
Experiments show that the rotation of the screw conveying rod piece 6 can also update the biological film in time, the mutual friction between the fillers can effectively remove excessively thick aged dead bacteria, the integral live bacteria proportion of the biological film is improved, and the proportion of related sulfur-adapting bacteria is improved, such as Thiobacillus denitrificans (Thiobacillus) and thiomonas hydrophila (Sulfuromonas) and the like.
The rotation speed of the screw conveying rod piece 6 is 1-30 r/min, preferably 5-20 r/min, and more preferably 6-10 r/min.
The spiral conveying rod piece 6 comprises a straight rod and a spiral part, the spiral part is spiral, the straight rod is positioned in the middle of the spiral part, and the head end and the tail end of the spiral part are fixed on the straight rod.
The material of the straight rod and the spiral part in the spiral conveying rod piece 6 is one or more selected from nylon, 304 stainless steel, 302 stainless steel and aluminum alloy, and is preferably 304 stainless steel. Under the same condition, the volume of the screw rod made of 304 stainless steel is smaller, which is more beneficial to filling of filler.
The pitch of the screw member of the screw conveyor bar 6 is 1 to 50mm, preferably 3 to 40mm, more preferably 5 to 35mm.
The inclination angle of the screw member is 5 to 20 °, preferably 8 to 15 °, more preferably 10 to 12 °.
The ratio of the diameter of the screw member to the diameter of the reactor is 1:1.05 to 1:5, preferably 1:1.2 to 1:4, more preferably 1:1.5 to 1:3. The packing material in the packing layer area of the reactor can flow under the stirring of the spiral conveying rod piece, enough gaps can be reserved between the screw rod and the inner wall of the reactor to ensure the packing material to flow through, and meanwhile, hardening of part of the packing material caused by incapability of stirring is avoided.
When the inclination angle of the spiral part is in the range, the filler can slowly move upwards under the rotation of the spiral part, and meanwhile, bubbles are continuously discharged in the rising process, so that the accumulation of nitrogen bubbles is reduced, and the hardening of the filler is prevented.
The filler layer region 5 comprises one or more of sulfur filler, pyrite filler and sulfur-containing composite filler, preferably comprises one or both of sulfur and pyrite composite filler, and more preferably comprises spherical sulfur filler of 2-8 mm.
The filling height of the filler layer region 5 is 20 to 500cm, preferably 30 to 200cm, more preferably 40 to 70cm.
The porosity of the filler layer region 5 is 37 to 42%, preferably 38 to 41%, more preferably 39 to 40%.
The second aspect of the utility model is to provide a method for sewage denitrification by adopting the sulfur autotrophic denitrification moving bed according to the first aspect of the utility model, which is characterized in that wastewater is conveyed into the sulfur autotrophic denitrification moving bed from the water inlet end 2 of the reactor, then conveyed to the filler layer area 5 through the water inlet screen plate 4, finally treated and discharged from the water outlet end 7 of the reactor, and the spiral conveying rod piece 6 is in an intermittent rotation state, preferably rotates for 0.1-8 h, stops rotating for 0.1-8 h, and more preferably rotates for 6h and stops rotating for 6h in the sewage treatment process.
The intermittent rotation mode can reduce sewage treatment cost, greatly improve sewage treatment effect and mass transfer effect.
Depending on the actual water quality nitrate nitrogen concentration removal requirements, the empty bed residence time is generally from 0.1 to 6 hours, preferably from 0.3 to 4 hours, more preferably from 0.5 to 2 hours.
The sewage treatment temperature is 10-40 ℃, preferably 20-35 ℃, more preferably 25-30 ℃. The above-mentioned treatment temperature is the most suitable temperature for the thiobacillus denitrificans.
The rotation speed of the screw conveying rod piece 6 is 1-30 r/min, preferably 5-20 r/min, and more preferably 6-10 r/min.
Experiments show that when the rotating speed of the screw conveying rod piece is in the range, the screw conveying rod piece is beneficial to avoiding hardening of the filler and discharging of nitrogen bubbles from the reactor, so that the nitrogen content of discharged water is effectively reduced, and the sewage treatment effect is improved.
A third aspect of the present utility model is to provide a pulsating bed reactor having a rectangular parallelepiped shape. The pulsating bed reactor comprises a spiral rod piece 17 and an automatic guide rail 18, wherein the automatic guide rail 18 is arranged at the top of the pulsating bed reactor, the spiral rod piece 17 is arranged on the automatic guide rail 18, the spiral rod piece 17 can reciprocate along the long side direction and the short side direction of the pulsating bed reactor along with the automatic guide rail 18, and as shown in fig. 2 and 3, the spiral rod piece 17 continuously rotates in the reciprocating movement process, so that local disturbance of filling materials can be realized, and the whole filling materials in the reactor can be fully moved, so that the reactor has better industrialized amplification application capability.
Experiments show that the mechanical stirring can effectively maintain the denitrification effect of the pulsating bed reactor, and simultaneously, the automatic guide rail is utilized to repeatedly move, so that each part of the filling material in the reactor is stirred more uniformly, the accumulation of nitrogen bubbles in the filling material layer is reduced, and the denitrification effect is improved.
The automatic guide rail 18 is installed at the top of the pulsating bed reactor, the automatic guide rail 18 is I-shaped, as shown in fig. 3, and comprises long guide rails installed along the long side of the reactor, short guide rails installed between the two long guide rails and perpendicular to the long guide rails, as shown in fig. 3, the long guide rails are parallel to the long side of the pulsating bed reactor, and the short guide rails are parallel to the short side of the pulsating bed reactor.
The rotational speed of the screw 17 is 5 to 40r/min, preferably 15 to 30r/min, more preferably 15 to 25r/min.
The horizontal moving speed of the screw 17 on the automatic guide 18 is 0.01 to 11cm/s, preferably 0.05 to 5.0cm/s, more preferably 0.1 to 1cm/s.
When the moving speed of the automatic guide rail is in the range, the whole packing can be fully moved, the phenomenon that all parts of the packing in the pulse bed are adhered and hardened is avoided, the biological film is updated in time, the biological film is kept at a lower thickness, and the denitrification moving bed has a higher denitrification load.
The ratio of the length of the long guide rail of the automatic guide rail 18 to the long side of the pulsating bed reactor is (1-1.3): 1, preferably the ratio is (1 to 1.2): 1, more preferably the ratio is (1 to 1.05): 1.
The ratio of the length of the short guide rail of the automatic guide rail 18 to the short side of the pulsating bed reactor is (1-1.3): 1, preferably the ratio is (1 to 1.2): 1, more preferably the ratio is (1 to 1.05): 1.
The inventor finds that when the ratio of the length of the long guide rail to the length of the short guide rail of the automatic guide rail to the long side to the short side of the pulsating bed reactor is in the above range, the spiral conveying rod piece can stir the filler in the whole pulsating bed to the greatest extent and update the biomembrane of the filler layer in time.
The pulsating bed reactor further comprises a water inlet end 12, a water outlet pipe 19, a supporting layer 15, a packing layer 16 and a water distribution plate 14, wherein the pulsating bed reactor adopts an upflow mode, the water inlet end 12 is positioned at the bottom of the pulsating bed reactor, the supporting layer 15 and the water distribution plate 14 are positioned between the packing layer 16 and the water inlet end 12, the supporting layer 15 is positioned between the packing layer 16 and the water distribution plate 14, a spiral rod piece 17 is in a spiral shape and is positioned in the packing layer 16, and the water outlet pipe 19 is positioned above the packing layer 16.
The screw member 17 includes a straight rod and a screw member, the screw member is in a spiral shape, the straight rod is located at a middle position of the screw member, and a head end and a tail end of the screw member are fixed on the straight rod.
The straight rod of the screw rod member 17 is made of one or two materials selected from nylon or 304 stainless steel, preferably 304 stainless steel. Under the same condition, the volume of the screw rod made of 304 stainless steel is smaller, which is more beneficial to filling of filler.
The spiral part is made of one or two materials selected from nylon or 304 stainless steel, and preferably 304 stainless steel.
The pitch of the screw member of the screw 17 is 1 to 50mm, preferably 3 to 40mm, more preferably 5 to 35mm.
The inclination angle of the screw member is 5 to 20 °, preferably 8 to 15 °, more preferably 10 to 15 °.
The screw rod piece 17 can reciprocate along the long side direction and the short side direction of the pulsating bed reactor along with the automatic guide rail 18, so that the influence of the screw rod piece 17 on each point of the filling material is ensured, the filling material in the reactor can be stirred in the maximum range, and the hardening of part of the filling material in the pulsating bed due to non-stirring is effectively avoided.
The material of the supporting layer 15 is one or more of cobblestones, stones, ceramsite and sand, preferably one or two of cobblestones and ceramsite, and more preferably cobblestones with the particle size of 3-8 mm.
The filling height of the supporting layer 15 is 3 to 150cm, preferably 5 to 120cm, more preferably 8 to 100cm.
The porosity of the supporting layer 15 is 30 to 50%, preferably 33 to 48%, more preferably 38 to 46%.
The filler layer 16 comprises one or more of a sulfur filler, a pyrite filler, and a sulfur-containing composite filler, preferably comprises sulfur, and more preferably comprises spherical sulfur having a particle size of 3 to 5mm.
The packing layer 16 has a packing height of 5 to 500cm, preferably 10 to 300cm, more preferably 12 to 250cm.
The porosity of the filler layer 16 is 37 to 42%, preferably 38 to 41%, more preferably 39 to 40%. When the porosity of the packing layer 16 is in the above range, the residence time of the wastewater to be treated in the pulsating bed is suitable, and the denitrification effect and denitrification efficiency are high.
The vertical distance between the water outlet pipe 19 and the filler layer 16 is 2 to 50cm, preferably 6 to 30cm, more preferably 8 to 20cm.
The short-handle filter heads are uniformly distributed and arranged on the water distribution plate 14, so that sewage flowing in from the water inlet end uniformly flows into the supporting layer 15 through the short-handle filter heads on the water distribution plate 14, and the handle diameter of the short-handle filter heads on the water distribution plate 14 is 0.5-50 mm, preferably 0.6-40 mm, more preferably 0.8-30 mm.
The distance between the adjacent short-handle filter heads on the water distribution plate 14 is equal, so that the installed short-handle filter heads can distribute water uniformly in the whole filter tank, and the distance between the adjacent short-handle filter heads is 0.1-10 cm, preferably 0.5-8 cm, and more preferably 1-6 cm.
According to a fourth aspect of the utility model, a method for denitrification of wastewater by using the pulsating bed reactor according to the third aspect of the utility model is provided, wherein wastewater to be treated is conveyed into a sulfur autotrophic denitrification pulsating bed from a water inlet end, passes through a uniform water distribution pore plate 14, a supporting layer 15 and a packing layer 16 from bottom to top, and finally flows out from a water outlet end 19 of the pulsating bed reactor.
The residence time of the empty bed depends on the nitrate nitrogen concentration of the sewage to be treated, and is usually 0.1 to 6 hours
The sewage treatment temperature is 8-40 ℃, preferably 15-35 ℃, more preferably 20-30 ℃.
The rotational speed of the screw 17 is 5 to 40r/min, preferably 15 to 30r/min, more preferably 15 to 25r/min. Continuous rotation or intermittent rotation.
The horizontal moving speed of the screw 17 on the automatic guide rail is 0.01 to 11cm/s, preferably 0.05 to 5.0cm/s, more preferably 0.1 to 1cm/s. Continuously reciprocating or intermittently rotating.
The utility model has the beneficial effects that:
(1) The denitrification moving bed system is characterized in that screw conveying rods are added into a mature fixed bed system, fluidization of the filler and mutual friction among the fillers can be realized through the addition of the device, even if nitrogen among the filler layers is discharged, the thickness of a biological film is reduced, the proportion of sulfur autotrophic denitrification bacteria on the surface of the filler is improved, and the high-efficiency and stable denitrification performance of the reaction system can be maintained. The denitrification moving bed system is used for sewage denitrification treatment, on one hand, the stability of sewage treatment can be improved, on the other hand, compared with a fixed bed system, the denitrification rate is remarkably improved, and because of the stable flow of the filler, the process does not need to rely on back flushing, and the problems of damage to a filler layer caused by oxygen during air flushing, reduced water yield caused by back flushing, uneven and incomplete back flushing and the like are avoided.
(2) Compared with a fixed bed process, the moving bed system of the utility model can obviously improve the denitrification load, and experiments prove that the overall improvement is nearly 50%, the smooth implementation of denitrification reaction also greatly reduces the intermediate product N 2 And the emission of O reduces the greenhouse effect. Under the same application scene condition, the initial filling material consumption of the tank body volume can be effectively reduced, the occupied area is reduced by 20-30%, and the ton water investment cost can be reduced by 30-40%, in addition, the utility model does not need to rely on back flushing, and the running management cost is greatly reduced.
(3) The pulsation bed reactor disclosed by the utility model is characterized in that the spiral conveying rod piece is arranged above the filter tank and is matched with the braking track, when the pulsation bed reactor is developed for large-scale filter tank amplification, the local circulating fluidization of the filler can be realized, the integral flow of the filler can be realized through the arrangement of the track, and the pulsation bed reactor is different from the existing air flushing technology, and can be used for more effectively solving the problems of low backwash water yield, overlarge pipe diameter of a backwash pipeline, operation stop of the filter tank during backwash and the like caused by the amplification of the existing fixed bed technology.
(4) Aiming at the problems of low denitrification load, dependence on back flushing, lack of controlled adjustment of denitrification efficiency and the like of a fixed bed reaction system in the prior art, the utility model creatively provides a moving bed process driven by a spiral conveying rod, is expected to break through in the aspect of new process technology, and provides powerful support for solving the urgent need of total nitrogen depth reduction of sewage treatment plants in China.
Examples
The utility model is further illustrated by the following specific examples, which are intended to be illustrative of the utility model and are not intended to limit the scope of the utility model.
Example 1
The sulfur autotrophic denitrification moving bed comprises a reactor water inlet end 2, a water inlet screen plate 4, a packing layer area 5, a spiral conveying rod piece 6 and a reactor water outlet end 7, wherein the water inlet screen plate 4 is positioned at the middle position of the bottom of the denitrification moving bed, the bottom of the denitrification moving bed is inclined downwards around the water inlet screen plate 4 and is in a funnel shape, the included angle between the bottom of the denitrification moving bed and the side face of the denitrification moving bed is 100 degrees, the reactor water inlet end 2 is positioned at the bottommost end of the denitrification moving bed and is connected with a water inlet peristaltic pump 1, the packing layer area 5 is positioned between the reactor water outlet end 7 and the reactor water inlet end 2, the spiral conveying rod piece 6 is in a spiral shape and is vertically arranged at the middle position of the packing layer area 5, and the reactor water outlet end 7 is positioned above the packing layer area 5.
The filler layer area 5 of the sulfur autotrophic denitrification moving bed adopts 3-5 mm sulfur spherical particles, the filling height is 50cm, the porosity is 40%, and the water outlet end 7 of the reactor is 5cm higher than the filler layer area. The spiral conveying rod piece 6 comprises a straight rod and a spiral component, the spiral component is made of 304 stainless steel, the pitch of the spiral component is 30mm, the inclination angle of the spiral component is 10 degrees, the diameter of the spiral component and the diameter ratio of the reactor are 1:2, the rotating speed of the spiral conveying rod piece 6 is 10r/min, the motor power is 60W, the empty bed residence time is 1h, the inflow velocity is 39.25ml/min, and the simulated wastewater comprises the following components: NO (NO) 3 - -N 20mg·L -1 、NH 4 + -N 2mg·L -1 、KH 2 PO 4 -P 0.5mg·L -1 、NaHCO 3 0.3mg·L -1 、MgCl 2 ·6H 2 O 0.4mg·L -1 、Na 2 S 2 O 3 50mg·L -1 Adding trace element liquid and vitamin liquid according to the proportion of 1mL/L, inoculating anaerobic tank sludge according to the volume of 1000mg/L of the filler layer, starting the process, continuously feeding water for 5 days, adjusting the residence time of an empty bed to 0.5h, lifting the water feeding flow rate to 78.5mL/min, and removing Na in the water after 5 days 2 S 2 O 3 And (3) operating until the effluent is stable, controlling the sewage treatment temperature to be 30 ℃, and considering that the starting is successful after the nitrate nitrogen and the nitrite nitrogen in the effluent of the reactor are stable.
Example 2
The pulsating bed reactor comprises a water inlet end 12, a water distribution plate 14, a supporting layer 15, a packing layer 16, a spiral rod piece 17, an automatic guide rail 18 and a water outlet pipe 19, wherein the water inlet end 12 is positioned at the bottom of the pulsating bed reactor and connected with a water inlet peristaltic pump, the supporting layer 15 and the water distribution plate 14 are positioned between the packing layer 16 and the water inlet end 12, the supporting layer 15 is positioned between the packing layer 16 and the water distribution plate 14, the spiral rod piece 17 is in a spiral shape and positioned in the packing layer 16, the water outlet end 19 is positioned above the packing layer 16, the automatic guide rail 18 is arranged at the top of the pulsating bed reactor, the spiral rod piece 17 is arranged on the automatic guide rail 18, the automatic guide rail 18 is I-shaped and comprises long guide rails arranged along the long side of the reactor, two sides of the top of the reactor, and a short guide rail arranged between the two long guide rails, the short guide rail is perpendicular to the long guide rail, the long guide rail is parallel to the long side of the pulsating bed reactor, and the short guide rail is parallel to the short side of the pulsating bed reactor.
The supporting layer 15 of the pulsating bed reactor comprises cobbles with the diameter of 3-5 mm, the filling height of the supporting layer 15 is 10cm, the porosity of the supporting layer is 44%, the filling layer 16 adopts sulfur spherical particles with the diameter of 3-5 mm, the filling height is 30cm, the porosity of the supporting layer is 40%, and the water outlet pipe 19 is higher than the filling layer 16 by 15cm. The stem diameter of the short handle filter heads on the water distribution plate 14 is 3cm, the distance between the adjacent short handle filter heads is 5cm, the spiral rod piece 17 comprises a straight rod and a spiral part, the straight rod and the spiral part are made of 304 stainless steel, the pitch of the spiral part is 30mm, the inclination angle of the spiral part is 15 degrees, the ratio of the diameter of the spiral part to the width of the pulsating bed reactor is 0.533, and the ratio of the length of the long guide rail of the automatic guide rail 18 to the long side of the pulsating bed reactor is 1:1, the ratio of the length of the short guide rail of the automatic guide rail 18 to the short side of the pulsating bed reactor is 1:1, the rotating speed of the screw rod piece 17 is 23r/min, the horizontal moving speed of the screw rod piece 17 on the automatic guide rail 18 is 0.5cm/s, the motor power is 70W, the empty bed residence time is 1h, the water inflow velocity is 9000ml/min, and the simulated wastewater components are: NO (NO) 3 - -N 20mg·L -1 、NH 4 + -N 2mg·L -1 、KH 2 PO 4 -P 0.5mg·L -1 、NaHCO 3 0.3mg·L -1 、MgCl 2 ·6H 2 O 0.4mg·L -1 、Na 2 S 2 O 3 50mg·L -1 Pressing againAdding microelement liquid and vitamin liquid at a ratio of 1mL/L, inoculating anaerobic tank sludge according to a filler layer volume of 1000mg/L, starting the process, continuously feeding water for 5 days, adjusting the empty bed residence time to 0.333h, lifting the water feeding flow rate to 2250mL/min, and removing Na in the water after 5 days 2 S 2 O 3 And (3) operating until the effluent is stable, controlling the sewage treatment temperature to be 30 ℃, and considering that the starting is successful after the nitrate nitrogen and the nitrite nitrogen in the effluent of the reactor are stable.
Comparative example
Comparative example 1
Sewage denitrification was performed in a similar manner to example 1, except that: the sulfur autotrophic denitrification moving bed does not include the screw conveyor bars 7.
Comparative example 2
Sewage denitrification was performed in a similar manner to example 2, except that: the pulsating bed does not comprise a screw 17 and a robot 18.
Experimental example
Experimental example 1 Denitrification Effect test
Effluent nitrate nitrogen, nitrite nitrogen, N of comparative example 1 and comparative example 1 2 The O concentration was measured and the dynamic nitrate nitrogen concentration of the effluent is shown in table 1 below.
As can be seen from Table 1, when the effluent of example 1 and comparative example 1 were stabilized, the effluent samples were taken for 10 days, the effluent nitrate nitrogen removal concentration of example 1 was stabilized at about 18mg/L, the removal rate was about 81%, which was much higher than the effluent nitrate nitrogen difference of comparative example 1 by about 11mg/L, the removal rate was about 61%, and the effluent nitrate nitrogen concentration of comparative example 1 was also continuously increased while the effluent nitrate nitrogen of example 1 remained stable, with continued operation of the denitrification moving bed.
TABLE 1
Also, there was almost no accumulation of nitrite in example 1, whereas nitrite could be clearly detected in the effluent in comparative example 1, since the denitrification process occurring in example 1 was smoother, and thus the nitrite accumulation in example 1 was low.
Therefore, the sulfur autotrophic denitrification moving bed has higher nitrate nitrogen removal load.
Experimental example 2 Denitrification Effect test
The effluent nitrate nitrogen, nitrite nitrogen, DO value (dissolved oxygen) lowering concentrations of example 2 and comparative example 2 were tested, and the dynamic nitrate nitrogen concentrations of the effluent are shown in Table 2 below.
As can be seen from Table 2, when the effluent of example 2 and comparative example 2 were stabilized, the effluent samples were taken for 10 days, the effluent nitrate nitrogen removal concentration of example 2 was stabilized at about 6mg/L at the same flow rate of the effluent, which is 4mg/L higher than the effluent nitrate nitrogen difference of comparative example 2, and the effluent nitrate nitrogen concentration of comparative example was also increased continuously while the effluent nitrate nitrogen of example 2 remained stable as the denitrification pulsating bed was operated continuously.
TABLE 2
Also, there was little accumulation of nitrite in example 2, whereas nitrite could be detected in the effluent clearly in comparative example 2, since the denitrification process occurring in example 2 was smoother, and thus the effluent nitrite concentration in example 2 was lower.
Therefore, the sulfur autotrophic denitrification pulsating bed has higher nitrate nitrogen removal load.
Experimental example 3 analysis of degree of bed blocking
The nitrogen accumulation rates of the moving beds of example 1 and comparative example 1 were tested, and the nitrogen accumulation rates and actual residence times are shown in table 3:
TABLE 3 Table 3
In Table 3, the nitrogen accumulation rate of the bed in example 1 was 14.02%, the nitrogen accumulation rate of the bed in comparative example 1 was 48.46%, and the nitrogen accumulation rate of the bed in example 1 was far lower than that of the bed in comparative example 1. Accordingly, the average actual residence time in example 1 was 0.264h, and the average actual residence time in comparative example 1 was only 0.154h. The effective porosity of example 1 was 1.668 times that of comparative example 1, and the actual residence time was 1.714 times that of comparative example 1, indicating that the nitrogen accumulation rate of the moving bed described in this application was reduced and the sewage residence time was prolonged.
Experimental example 4 biofilm thickness test
The biofilm thickness of the fillers of example 1 and comparative example 1 was tested, and after the reactor was stably operated, the biofilm thickness of the fillers was sampled and detected, and the test is shown in table 4:
TABLE 4 Table 4
From Table 4, the biofilm thickness in comparative example 1 is much higher than that of example 1, and the biofilm in comparative example 1 grows too much during sewage treatment, which shows that the moving bed of the utility model can effectively reduce the biofilm thickness by arranging a screw conveying rod.
Experimental example 5 live bacteria ratio analysis
The test was carried out on the staining of living and dead cells in the fillers of example 1 and comparative example 1, and after the reactor was stably operated, samples were taken to examine the surface organisms of the fillers, and the test is shown in table 5:
TABLE 5
As can be seen from Table 5, the biofilm live bacteria ratio in comparative example 1 is much lower than that in example 1, while from the bacteria as a whole, comparative example 1 is much higher than that in example 1, so that it can be seen that comparative example 1 is much biomass, meaning that dead bacteria of comparative example 1 are also much larger than that of example 1, which brings about greater mass transfer resistance for denitrification reaction, indicating that the denitrification moving bed of the present utility model can effectively reduce the ratio of dead bacteria and reduce mass transfer resistance.
The utility model has been described in detail in connection with the specific embodiments and exemplary examples thereof, but such description is not to be construed as limiting the utility model. It will be understood by those skilled in the art that various equivalent substitutions, modifications or improvements may be made to the technical solution of the present utility model and its embodiments without departing from the spirit and scope of the present utility model, and these fall within the scope of the present utility model. The scope of the utility model is defined by the appended claims.
Claims (6)
1. The sulfur autotrophic denitrification moving bed is characterized by comprising a reactor water inlet end (2), a water inlet screen plate (4), a filler layer area (5), a spiral conveying rod piece (6) and a reactor water outlet end (7), wherein the water inlet screen plate (4) is positioned at the middle position of the bottom of the denitrification moving bed, and the bottom of the denitrification moving bed is inclined downwards around the water inlet screen plate (4) and is in a funnel shape;
the spiral conveying rod piece (6) is vertically arranged in the middle of the packing layer area (5) and comprises a straight rod and a spiral part, the spiral part is spiral, the straight rod is positioned in the middle of the spiral part, and the head end and the tail end of the spiral part are fixed on the straight rod.
2. A sulfur autotrophic denitrification moving bed according to claim 1, wherein,
the water inlet end (2) of the reactor is positioned at the lowest end of the denitrification moving bed and is connected with a water inlet peristaltic pump (1), and the water outlet end (7) of the reactor is positioned above the packing layer area (5).
3. A sulfur autotrophic denitrification moving bed according to claim 1, wherein,
the pitch of the spiral component of the spiral conveying rod piece (6) is 1-50 mm;
the inclination angle of the spiral part is 5-20 degrees.
4. A sulfur autotrophic denitrification moving bed according to claim 1, wherein,
the ratio of the diameter of the spiral part to the diameter of the reactor is 1:1.05-1:5.
5. A sulfur autotrophic denitrification moving bed according to claim 2, wherein,
the vertical distance between the water outlet end (7) of the reactor and the packing layer area (5) is 5-300 cm.
6. A sulfur autotrophic denitrification moving bed according to claim 2, wherein,
the filling height of the filling layer area (5) is 20-500 cm, and the porosity of the filling layer area (5) is 37-42%.
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